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1. Liquid Volume Flow barrel day Heat Flow Btu hr Material Streams J Include Sub Flowsheets J Show Name Only Number of Hidden Objects 0 Completed 3 26 You can toggle the palette open or closed by pressing F4 or by choosing Open Close Object Palette from the Flowsheet menu Save Icon a Lar Open Case Icon When you choose to open an existing case by clicking the Open Case bution or by selecting Open Case from the File menu HYSYS allows you to retrieve backup bk and HYSIM sim files in addition to standard HYSYS hsc files If you enter a name that already exists in the current directory HYSYS will ask you for confirmation before over writing the existing file Chemicals Tutorial There are several things to note about the Main Simulation environment In the upper right corner the Environment has changed from Basis to Case Main A number of new items are now available on the Menu and Toolbar and the Workbook and Object Palette are open on the Desktop These two latter objects are described below Features Workbook Description A multiple tab view containing information about the objects streams and unit operations in the simulation case By default the Workbook has four tabs namely Material Streams Compositions Energy Streams and Unit Ops You can edit the Workbook by adding or deleting tabs and changing the info
2. Default Fluid Pkg Basis 1 x a Components Fluid Pkgs Hypotheticals OilManager Reactions Component Maps UserProperty Enter Simulation Environment The list of Current Fluid Packages now displays the new Fluid Package Basis 1 and shows the number of components NC and property package PP The new Fluid Package is assigned by default to the main flowsheet as shown in the Flowsheet Fluid Pkg Associations group Now that the Basis is defined you can install streams and operations in the Main Simulation environment To leave the Basis environment and enter the Simulation environment do one of the following e Click the Enter Simulation Environment button on the Simulation Basis Manager view e Click the Enter Simulation Environment icon on the tool bar Steady State Simulation 1 2 4 Entering the Simulation Environment When you enter the Simulation environment the initial view that appears depends on your current Session Preferences setting for the Initial Build Home View Three initial views are available 1 PFD 2 Workbook 3 Summary Any or all of these can be displayed at any time however when you first enter the Simulation environment only one appears In this example the initial Home View is the PFD HYSYS default setting Figure 1 19 md 4807 GASPLANT SS hsc HYSYS 3 1 File Edit Simulation Flowsheet PFD Tools Window Help Os anag e YF ow Ae snare sess a
3. Composition Controls Erase Normalize Cancel 3 Click the OK button and HYSYS accepts the composition The stream is now completely defined so HYSYS flashes it at the conditions given to determine its remaining properties Figure 1 27 Worksheet lols Fractions el aT a aA Conditions OTOUOU 0 600000 Properties EE 0 200000 _ Composition EATA 0 040000 K Value 0 040000 User Variables eae Notes If you want to delete a Geet PERETE a stream click on it in the o PFD then press the DELETE Edit Edit Properties Basis key HYSYS will ask for confirmation before deleting You can also delete the Worksheet Dynamics stream using the Delete See ER button on that stream s Delete Define from Other Stream ee view 4 Close this view then return to the Workbook by clicking on the Workbook button 1 26 Gas Processing Tutorial 1 27 5 Ensure that the Material Streams tab is active The properties of Feed 1 appear below The values you specified are a different colour blue than the calculated values black Figure 1 28 Workbook Case Main apour Fraction emperature F ressure psia Molar Flow MMSCFD Mass Flow lb hr iquid Yolume Flow barrel day 3012 Heat Flow Btu hr __ 2 553e 007 Material Streams Energy Streams Unit Ops Production Faed 1 C
4. cccccseeeeeeeeseeees 136 2 3 5 Monitoring in Dynamics sessar a 142 2 1 2 2 2 2 Refining Refining Tutorial 2 1 Introduction You will build the Refining simulation using the following basic steps 1 Create a unit set 2 Choose a property package 3 Select the non oil components 4 Characterize the Oil 5 Create and specify the preheated crude and utility steam streams 6 Install and define the unit operations in the pre fractionation train 7 Install and define the crude fractionation column This complete case has also In this tutorial crude oil is processed in a fractionation facility to sian ey produce naphtha kerosene diesel atmospheric gas oil and your HYSYS Samples atmospheric residue products Preheated crude from an upstream directory preheat train is fed to a pre flash drum where vapours are separated from the liquids which are heated in a furnace The pre flash vapours bypass the furnace and are recombined with the hot crude from the furnace The combined stream is then fed to the atmospheric crude column for fractionation The main flowsheet for this process appears below Figure 2 1 Naphtha _ WasteH20 PreFlashVap PreFlash Kerosene Preheat i Crude Furnace Diesel L PreFlashLiq HotCrude gt Residue CrudeDuty CondDuty 2 3 2 4 2 4 Introduction The crude column consists of a refluxed absorber with three side strippe
5. 15 00 4 369e 005 2 006e 003 35 94 115 4 1361 4 701e 006 eat Flow Btu hr 9 656e 007 apour Fraction RecyProds 0 0000 Reactor Prods 1 393e 008 1 869e 008 2 534 0 0000 emperature F 1 082e 004 1 971e 004 618 5 20 78 2 803e 007 38 75 8 714e 007 Heat Flow Btu hr 5 700e 007 u Material Streams Energy Streams Unit Ops Main TS Condenser L Show Name Only Number of Hidden Objects 0 2 When you are finished in the column environment return to the Main Flowsheet by clicking the Enter Parent Simulation Environment icon 3 Open the PFD for the Main Flowsheet and select Auto Position All from the PFD menu HYSYS arranges your PFD in a logical manner Chemicals Tutorial 3 65 Moving Objects and Labels in a PFD The PFD below has been customized by moving some of the stream icons To move an icon simply click and drag it to the new location You can also move a stream or operation label name 1 Right click on the label you want to move 2 From the menu that appears select Move Size Label A box appears around the label 3 Click and drag the label to a new location or use the arrow keys to move it Figure 3 86 Reactor Vent CondDuty Reactor MIX 100 Reactor Prods RecyProds RebDuty Glycol 3 65 3 66 Steady State Simulation 3 2 8 Viewing Resu
6. Mass Flows C Lig Volume Flows Erase Normalize Cancel o 10020000 bh E E R A EE E Composition Controls a ey Sane ee 3 34 Chemicals Tutorial 3 35 26 Since this stream has no other components click the Normalize button The other component mass flows are forced to zero Figure 3 42 Nil Input Composition for Stream Water Feed E assFlo m Composition Basis 2030 xide Mole Fractions 20 a A baie ene C Liq Volume Fractions C Mole Flows Mass Flows C Lig Volume Flows Composition Controls Erase Normalize Cancel o 100020000 bh 27 Click the OK button to close the view and return to the stream property view HYSYS performs a flash calculation to determine the unknown properties of Water Feed and the status bar displays a green OK message Use the horizontal scroll bar in the table to view the compositions of each phase Figure 3 43 Water Feed Worksheet LA ques Phase 12C30xide io it Conditions Properties Composition K Value User Variables Notes gt l Cost Parameters Total f 100 00000 lb hr Edit Properties Basis Worksheet Attachments Dynamics BR Delete Define from Other Stream 3 35 3 36 Steady State Simulation The compositions currently appear in Mass Flow but you can change this by clicking th
7. Figure R1 10 Side Stripper Summary mae a 9_ ManTS 8_MainTS lt empty gt lt empty gt Diesel_ Ss s 17_ManTS 16_Main TS lt empty gt lt empty gt AGO_SS 3 22 Main TS 21__ Main TS lt empty gt lt empty gt 2 Main TS 1_MainTS lt empty gt lt empty gt lt empty gt lt empty gt 17_MainTS 16_MainTS lt empty gt lt empty gt lt empty gt lt empty gt amp 22_MainTS 21_MainTS lt empty gt lt empty gt lt empty gt lt empty gt fF R1 14 Atmospheric Crude Tower Fisid units are weed tor 6 In the Atmos Tower Column view specify the column information column preferences below Column Atms Tower Tab Page In this celh Enter Parameters Profiles Specifications e On the Monitor page of the Design tab input the following values into the default set of specifications supplied with the pre built 3 Side Stripper Column e Change the Pump Around delta T specification to a Duty specification e Change the Basis of each Pump Around Rate specification to Volume Basis before entering the values 1 Delete the Kero SS BoilUp Ratio and the Residue Rate specs click the View button then click Delete in the specification property view 2 Specify the Reflux Ratio spec to have a value of 1 Uncheck the Reflux Ratio Active checkbox and make it an Estimate only 3
8. Refining Tutorial 2 Select the Peng Robinson property package by doing one of the following e Type Peng Robinson HYSYS finds the match to your input e Use the up and down arrow keys to scroll through the list of available property packages until Peng Robinson is selected e Use the vertical scroll bar to scroll through the list until Peng Robinson becomes visible then click on it The Fluid Package Basis 1 view appears as shown below Figure 2 14 Fluid Package Basis 1 m Property Package Selection l EOS Enthalpy Method Specificatiorr General NATL Property Package Fiter Equation of State ce Alpe wie Lee Kesler Plocker C EOSs C Activity Models Chao Seader Models Vapour Press Models C Miscellaneous Types Peng Robinson Options HYSYS Standard Use EOS Density J Smooth Liquid Density Advanced Thermodynamics Component List Selection COMThermo Hegressic mai Component List 1 View a Expo L E Eror Set Up Parameters Binary Coeffs StabTest Phase Order Axns Tabular Notes Delete Name Basie Property Pkg Peng Robinson Ed Prope The Property Pkg indicator now indicates Peng Robinson is the current property package for this fluid package Alternatively you could have selected the EOSs radio button in the Property Pkg Filter group The list would then display only those property packages that are Equations of State Pe
9. 8 To add the third utility stream do any one of the following Cc e Press F11 e From the Flowsheet menu select Add Stream Material Stream icon e Double click the Material Stream icon on the Object Palette e Click the Material Stream icon on the Object Palette then click ae on the Palette s Add Object icon Add Object icon Each of these four methods displays the property view for the new stream which is named according to the Auto Naming setting in your Preferences The default setting names new material streams with numbers starting at 1 and energy streams starting at Q 100 9 Inthe stream property view click in the Stream Name cell and rename the stream AGO Steam 10 Press ENTER 2 44 Refining Tutorial 2 45 Both of the temperature and 11 In the Temperature cell enter 300 pressure parameters are in the default units so you do not need to change the unit with the values Do not enter a flow it is eee E oix Composition page 12 In the Pressure cell enter 50 Worksheet Stream Name AGO Steam Vapour Phase Fraction lt empty gt eee Temperature F 300 00 Properties Pressure psia 50 000 YP sempi pai Mass Flow lb hr lt empty gt K Value Std Ideal Lig Vol Flow barrel day lt empty gt User Variables Molar Enthalpy Btu lbmole lt empty gt Molar Entropy Btu Ibmole F lt empty gt Notes He
10. Outlet Towerlnlet Design Parameters Delta P 363 psi 34 Close the valve property view You can use the scroll bars to 35 Click the Attach Mode icon then connect the TowerlIn stream to the navigate around the PFD You exit of the MIX 101 unit operation Exit the attach mode can also use the PAGE UP and a PAGE DOWN keys to zoom in 36 Install a Heater operation and position it near the Tower Valve and and out of the PFD the DePropanizer respectively e Inthe Object Palette click once on the Heater icon e Inthe PFD click where you want to insert the heater 37 Open the heater property view and specify the following connections Tab Page In this cell Enter Inlet Towerlnlet Design Parameters Delta P 38 In the heater property view click the Worksheet tab then select the Conditions page 1 103 1 104 Dynamic Simulation 39 In the Temperature cell of the TowerFeed stream enter 24 73 E Figure 1 130 Worksheet Towerlnlet TowerFeed Heater Q re 0 2633 0 3967 lt empty gt Conditions 6 448 24 73 lt empty gt Properties 212 0 lt empty gt 310 6 310 6 lt empty gt 1 162e 004 1 162e 004 lt empty gt PF Specs 1742 1742 lt empty gt 4 963e 004 4 832e 004 lt empty gt 26 18 29 00 lt empty gt 1 542e 007 1 501e 007 4 064e 005 Composition When considering pieces of 40 Close the Heater property view equipme
11. You can modify any of the default sizing parameters in the Unknown Sizes tab Once you modify a sizing parameter the piece of equipment is automatically sized and the volume Cv or k value displayed 7 For each page in the Unknown Sizes tab ensure that all the recommendations are active Tab Page Recommendation Unit Operation OK Checkbox Unknown Sizes Vessel Sizing Chiller Volumes Gas Gas Tube 1 Active Gas Gas Shell 2 Unknown Sizes Heat Exchanger Chiller k values Sizing Gas Gas Tube Active GasGas Shel 8 Click the Tray sections tab The Tray sections tab identifies tray sections and streams whose total steady state pressure drops are inconsistent with the total pressure drop calculated according to the dynamics rating model For the purpose of this tutorial recommendations on this tab will be ignored 1 116 Gas Processing Tutorial 117 Processing Tutorial 1 117 9 Click the Other tab Figure 1 146 Ni Dynamics Assistant Other Make the following miscellaneous specification changes Muc loinc Name Description OK Component Splitter MIx 101 Equal pressures option active Vv r The Other tab contains a list of Tell me why miscellaneous changes that should to be made in order for General Streams Pressure Flow Specs Unknown Sizes Tray sections Other User Items the Dynamic simulation case Analyze Again Make Changes _ Cancel to run effectivel
12. 3 39 340 Steady State Simulation Steady State Simulation The status indicator displays a green OK indicating that the operation and attached streams are completely calculated The Connections page is now complete 12 Click the Parameters page 13 In the Automatic Pressure Assignment group keep the default setting of Set Outlet to Lowest Inlet Figure 3 49 MIX 100 Design Connections Parameters User Variables Notes lt E Design Rating Automatic Pressure Assignment C Equalize All Set Outlet to Lowest Inlet Worksheet Dynamics 14 Click the Worksheet tab in the MIX 100 property view to view the calculated outlet stream This tab is a condensed Workbook tab displaying only those streams attached to the operation HYSYS has calculated the outlet stream by combining the two inlets and flashing the mixture at the lowest pressure of the inlet streams In this case both inlets have the same pressure 16 17 psia so the outlet stream is set to 16 17 psia 3 40 Figure 3 50 15 MIX 100 Worksheet Conditions Properties Composition PF Specs i Design Rating Worksheet TEE Close the MIX 100 property view to return to the Workbook apour 0 0000 Water Feed Mixer Out 0 0000 0 0000 emperature F 75 00 75 00 75 00 ressure psia 16 17 16 17 16 17 Molar Flow Ibmole hr 150 0 61
13. 8 561e 007 2 331e 008 Temperature F 457 5 496 8 571 6 Pressure psia 29 84 Molar Flow Ibmole hr Mass Flow lb hr 1 115e 005 701 9 30 99 1114 2 425e 005 31 70 200 4 5 945e 004 Liquid Volume Flow barrel day 9300 1 925e 004 4500 Heat Flow Btu hr 8 098e 007 1 722e 008 3 882e 007 Ba 5 Material Streams ProductBlock_Kerosene Atms Tower Energy Streams Unit Ops J Include Sub Flowsheets J Show Name Only Number of Hidden Objects 0 Workbook Case Atms Tower Atmospheric Crude Tower RI Crude Tower R1 19 The material stream results for the Workbook Case Atms Tower appear below Figure R1 16 Name Reflux ToCondenser Main Steam Residue 4 OffGas Water draw Vapour Fraction 0 0000 1 0000 1 0000 0 0000 0 6122 1 0000 0 0000 Temperature F 107 3 274 6 375 0 669 1 622 2 107 3 107 3 Pressure psia 13 70 28 70 150 0 32 70 65 00 19 70 19 70 Molar Flow Ibmole hr 2010 59532 416 3 1397 6214 4 473e 005 700 3 Mass Flow lb hr ___1 763e 008 4 363e 008 7500 6 216e 005 1 282e 006 2 304e 003 1 263e 004 Liquid Yolume Flow barrel day 1 638e 004 4 025e 004 514 6 4 398e 004 1 000e 005 2 612e 004 866 4 Heat Flow Btu hr 1 6
14. SalesGas Sales Gas Production TowerFeed Add Available Strip Charts DataLoggerl Molar Flow Ce Liquid Production Liquid Percent Level Molar Flow Liquid Percent Level Utility Outlet Temp LiquidProd LTS Delete und InletSep Setup sw Heater Q iz Variables Process Data Tables Strip Charts Data Recorder Case Studies If required add more strip charts by repeating steps 7and 8 To access a strip chart view select the strip chart name then click the Strip Chart button Minimize the Databook view Before starting the integrator open the property view for the Ovhd stream in the Column sub flowsheet Click the Dynamics tab then select the Specs page Gas Processing Tutorial 16129 Processing Tutorial 1 129 14 In the Dynamic Specifications group ensure that the Pressure specification checkbox is Active and the Molar Flow specification checkbox is Inactive 15 Close the Ovhd stream view 16 Arrange both strip chart views so you can see them Ta pi 17 Start the Integrator by clicking the Start Integrator icon in the tool Start Integrator icon green bar and observe as the variables line out on the strip charts 18 Click the Stop Integrator icon to stop the process 19 To use the Databook feature for analysis manipulate the stream and operation variables via their property views click the Start Integrator icon again a
15. ae ba haa 7 7 7 A e Material Streams 0 0000 1 0000 0 0000 0 0000 1 0000 T 1 0000 0 6040 165 3 267 1 657 2 165 3 165 3 375 0 641 6 19 70 28 70 32 70 19 70 19 70 150 0 65 00 1153 5701 882 8 1491 1 002e 004 416 3 3814 1 563e 005 4 135e 005 5 535e 005 2 021e 005 6 769e 003 7500 1 144e 006 1 546e 004 3 924e 004 4 503e 004 2 000e 004 122e 004 514 6 1 000e 005 1 356e 008 WasteH20 5 664e 008 KeroSS_ Draw 2 839e 008 KeroSS_ Return 1 754e 008 Kerosene 7 052 Kero55_BoilUp 4 222e 007 KeroSS_ToRek 5 787e 008 AGOSS Draw 0 0000 0 0000 1 0000 0 0000 1 0000 0 0000 0 0000 165 3 387 5 418 8 450 3 435 0 600 9 19 70 29 84 29 84 29 84 29 84 31 70 3058 746 3 79 56 666 7 1022 428 9 508e 004 1 549e 005 1 374e 004 1 412e 005 2 123e 005 1 518e 005 3779 1 429e 004 1294 1 300e 004 6595 1 9602 004 1 333e 004 3 702e 008 AGOSS Returr 1 126e 008 AGO 6 845e 006 AGO Steam 9 624e 007 4 263e 007 DieselSS Draw DieselSS_Retui 1 464e 008 Diesel 8 532e 007 Diesel Steam 1 0000 0 0000 1 0000 0 0000 1 0000 0 0000 1 0000 537 6
16. Figure 1 35 Feed 2 Worksheet Stream Name Vapour Phase me Yapour Phase Fraction 0 90127 0 09873 dca Temperature F porate Ee rr ay eee N Pressure psia 600 00 ta a Sore ect K Value Std Ideal Lig Vol Flow barrel day 1983 1 User Variables Molar Enthalpy Btu Ibmole 3706e 004 3553e 004 5 096e 004 Molar Entropy Btu Ibmole F 35 562 36 628 25 726 Notes Heat Flow Btu hr __ 1 6276e 07 1 4066e 07 2 2096e 06 Cost Parameters Liq Vol Flow Std Cond barrel day _ lt empty gt lt empty gt Fluid Package __ Basis 1_ Liquid Phase Properties Composition lt Worksheet Dynamics a Delete Define from Other Stream Viewing a Phase Diagram You can view a phase diagram for any material stream using the HYSYS Envelope Utility 1 On the property view for stream Feed 2 click the Attachments tab then select the Utilities page 2 To create a phase envelope for the stream click the Create button The Available Utilities view appears displaying a list of HYSYS utilities Gas Processing Tutorial BT Processing Tutorial 1 31 1 31 Steady State Simulation 3 Do one of the following e Select Envelope and click the Add Utility button e Double click on Envelope Figure 1 36 Available Utilities Of x BP Curves CO2 Solids Cold Properties Critical Property Depressuring Hydrate Formation Pipe Sizi
17. gt MIX 100 Design Connections Parameters User Variables Notes Automatic Pressure Assignment C Equalize All f Set Outlet to Lowest Inlet a z Design Rating Worksheet Dynamics NS ono 1 37 1 38 Steady State Simulation 14 To view the calculated outlet stream click the Worksheet tab then click on the Conditions page Figure 1 45 The Conditions page is a condensed Workbook page displaying only those streams attached to the selected operation MIX 100 Worksheet Conditions Properties Composition PF Specs Temperature F Molar Flow MMSCFD Mass Flow lb hr Std Ideal Lig Yol Flow barrel day Molar Enthalpy Btu Ibmole Molar Entropy Btu Ibmole F 0 8952 Feed 2 MixerOut 0 9013 0 8976 60 00 60 00 60 00 600 0 600 0 600 0 6 000 4 000 10 00 1 675e 004 1 100e 004 2 775e 004 3012 1983 4995 3 874e 004 3 706e 004 3 807e 004 35 71 ce a 35 66 4 180e 007 Heat Flow Btu hr 2 553e 007 re a 1 628e 007 7a Design Rating Worksheet ES croc 15 Now that the Mixer is completely known close the view to return to the Workbook The new operation appears in the table on the Unit Ops tab of the Workbook Figure 1 46 Workbook Case Main p Name Obiect Tye Inet Ouwiet Ignored Calc Level
18. 3 On the Variables tab click the Insert button The Variable Navigator appears 4 Inthe Object Filter group select the UnitOps radio button The Object list is filtered to show unit operations only 5 Inthe Object list select Reactor The variables available for the Reactor object appear in the Variable list Chemicals Tutorial 3 69 The Variable Navigatorisused 9 In the Variable list select Vessel Temperature Vessel Temperature extensively in HYSYS for appears in the Variable Description field You can edit the default locating and selecting variable description variables The Navigator operates in a left to right manner the selected Figure 3 90 Flowsheet determines the Object list the chosen Object ae owner dictates the Variable list and Flowsheet j Variable Case Main gt Vapour Level ie selected eS Tower COL1 Vapour Mass Flow etermines whether an Vapour Molar Flow ae i ae y Vapour Mole Fracti Object Filter available Vapour Volume C Streams Yapour Volume Flo Vessel Diameter Navigator Scope Vessel Geometry C C Logicals Flowsheet Vessel Length or H C ColumnOps Vessel Mole Frac C C Case Vessel Pressure Custom Basis Vessel Pressure Dn Custom C Utility Vessel Temperature Volume Fixed Orde Volume Sorted by Fo Variable Description R eactor Temp Cancel 7 Inthe Variable Description field rename the variable Reactor Temp then click the OK button The variable no
19. Adding the Duty Specification 9 Click the Add button again to add the second new specification 10 Select Column Duty as the Column Specification Type then click the Add Spec s button The Duty Spec view appears 11 In the Name cell change the name to Kero Reb Duty 12 In the Energy Stream cell select KeroSS_Energy COLI from the drop down list 13 In the Spec Value cell enter 7 5e6 Btu hr Figure 2 106 Duty Spec Kero Reb Duty Oe x Name Kero Reb Duty seroSS Energy COL1 7 5e 006 Btu hr Parameters Summary Delete Refining Tutorial 14 Close the view to return to the Specs page of the Column property view The completed list of Column Specifications is shown in the figure below Figure 2 107 Column Specifications Reflux Ratio Distillate Rate Yap Prod Rate WasteH20 Rate KeroSS Prod Flow KeroSS BoilUp Ratio DieselSS Prod Flow Update Specs from Dynamics Default Basis Yolume X Degrees of Freedom f Running the Column 1 Select the Monitor page to view the Specifications matrix The Degrees of Freedom is again zero so the column is ready to be calculated however a value for the distillate Naphtha rate specification must be supplied initially In addition there are some specifications which are currently Active that you want to use as Estimates only and vice versa Make the following final changes to the specifications 2 Inthe Specified Value
20. Figure 1 119 Current Cell Imported From SalesGas B5 Variable Comp Mole Frac Propane Mole Fraction Total Heat Value 0 7664 4 6 9693e 02 0 1565 2 5333e 02 0 0414 9 5887e 01 0 0070 2 0345e 01 0 0043 1 2932e 01 Mion coho oOo i co oo Click in cell C9 and enter the label Sales Gas NHV Click in cell D9 Enter d3 d4 d5 d6 d7 in cell D9 to sum the individual heating values The result is the NHV of SalesGas in Btu scf Figure 1 120 Current Cell z Variable Type Vapour Fraction Exportable V DS Variable Angles in Rad d3 d4 d5 d6 d7 Mole Fraction Comp Heat Value Total Heat Value 0 7664 909 4 6 9693e 02 0 1565 2 5333e 02 0 0414 9 5887e 01 0 0070 2 0945e 01 0 0043 1 2932e 01 00 00 so on oo po Sales Gas NHY i 1 0800e 03 lt Connections Parameters Formulas Spreadsheet Calculation Order ks IT Delete Function Help Spreadsheet Only Ignored 1 92 Gas Processing Tutorial 1 83 Processing Tutorial 1 93 To add the value of Sales Gas NHV to the Databook Click the Parameters tab of the Heating Value property view In the Exportable Cells table enter a Variable Name for cell D9 for example NHV Close the Heating Value property view Open the Databook by pressing CTRL D On the Variables tab insert
21. Name Reflux Ratio Name Draw Rate Condenser Draw Propene Molar Molar 16 40 774 1 bmole hr IV Include Yapour Parameters Summar Parameters Summary ramete ummary Delete Dete If the column has not converged at this point ensure the Run Column Solver icon is active Run Column Solver icon green Hold Column Solver icon red P1 9 PH Ret Results P1 4 Results Workbook 1 100 COLI Material Streams Tab Figure P1 4 ioixl Name o o lt U Feed Rect Out Boilup To Rect To Reboiler Vapour Fraction 1 0000 0 0000 1 0000 1 0000 0 0000 Temperature F 126 7 121 1 135 1 Tet 135 0 Pressure psia 300 0 290 0 300 0 290 0 300 0 Molar Flow Ibmole hr 1350 1 294e 004 1 284e 004 1 372e 004 1 341e 004 Mass Flow lb hr 5790e 004 5 502e 005 5 639e 005 5 826e 005 5 892e 005 Liquid Volume Flow barrel day 7698 7 276e 004 7 604e 004 705e 004 7 945e 004 Heat Flow Btu hr 1 7239e 007 1 048e 008 6 158e 008 3 209e 007 6 060e 008 Name Propane sReflux ToCondenser Propene ss New Vapour Fraction i 0 0000 0 0000 1 0000 0 0000 Temperature F 135 1 116 0 116 0 116 0 Pressure psia 300 0 280 0 280 0 280 0 Molar Flow Ibmole hr 574 9 1 271e 004 1 349e 004 775 1 Mass Flow Ib hr 2 527e 004 5 352e 005 5 678e 005 3 263e 004 Liquid Volume Flow barrel day 3408
22. Worksheet lo 2500 0 i Conditions Propane 0 00000 _ i Butane 0 00000 n Butane 0 00000 Composition i Pentane 0 00000 n Pentane 0 00000 K Value oy113 0 00000 i 0 00000 User Variables 164 000000 Notes a gt Cost Parameters Total 2500 00000 1b hr f i Edit Properties Basis Properties 3 Worksheet Attachments Dynamics Delete Define from Other Stream lt a gt gt HYSYS performs a flash calculation to determine the unknown properties of AGO Steam as shown by the status indicator displaying OK You can view the properties of each phase using the horizontal scroll bar in the matrix or by re sizing the property view In this case the stream is superheated vapour so no Liquid phase exists and the Vapour phase is identical to the overall phase To view the vapour compositions for AGO Steam scroll to the right by clicking the right scroll arrow or by click and dragging the scroll button The compositions are currently displayed by Mass Flows You can change this by clicking the Basis button and choosing another Composition Basis radio button 19 Close the AGO Steam property view 2 46 Workbook icon Refining Tutorial 2 2 6 Installing Unit Operations Now that the feed and utility streams are known the next task is to install the necessary unit operations for processing the crude oil Installing the Separator The first operation is a Separator u
23. lt empty gt 0 0000 barrel day lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt 1300 barrel day lt empty gt lt empty gt lt empty gt lt empty gt Wt Error A lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt tive Estimate Current Q WasteH20 Rate KeroSS Prod Flow KeroSS BoilUp Ratio 0 7500 DieselSS Prod Flow AGOSS Prod Flow 17000 barrel day 5000 barrel day WTId00 04 AVd0000 79 Wd 74 View Add Spec Group Active Update Inactive Degrees of Freedom fo The installation of the side strippers created four additional degrees of freedom so HYSYS created a Prod Flow product flow specification for each side stripper plus a BoilUp Ratio specification for the Kerosene side stripper The new specifications were automatically made Active to exhaust the four degrees of freedom returning the overall Degrees of Freedom to 0 Installing the Pump Arounds Click the Side Ops tab and select the Pump Arounds page Click the Add button The initial Pump Around view appears In the Return Stage drop down list select stage 1 1_Main TS oo i In the Draw Stage drop down list select stage 2 2_Main TS 2 79 Steady State Simulation 5 Click the Install button and a more detailed Pump Around view appears Figure 2 96 Nil Pump Around PA_1 Ist Activ
24. omp Mole Frac C02 0 0066 0 0063 0 0053 ji 0 0046 E 0 0000 omp Mole Frac Methane 0 7664 0 6576 0 2677 0 2412 0 0000 omp Mole Frac Ethane 0 1565 0 1846 0 2854 0 2576 0 0000 omp Mole Frac Propane 0 0414 0 0877 0 2534 0 2561 0 0200 omp Mole Frac i Butane 0 0070 0 0272 0 0998 0 1218 0 4490 omp Mole Frac n Butane 0 0043 0 0222 0 0862 0 1166 0 5309 Material Streams P T Flow Compositions Unit Ops Fancanisckinaadil _ Include Sub Flowsheets we oo C Show Name Only Number of Hidden Objects 1 76 ih Navigator icon You can start or end the search string with an asterisk which acts as a wildcard character This lets you find multiple objects with one search For example searching for VLV will open the property view for all objects with VLV at the beginning of their name Gas Processing Tutorial 1 77 Using the Object Navigator In this section you will use the Object Navigator to view properties for a particular stream or operation The Object Navigator allows you to quickly access the property view for any stream or unit operation at any time during the simulation 1 To open the Navigator do one of the following e Press F3 e From the Flowsheet menu select Find Object e Click the Navigator icon The Object Navigator view appears Figure 1 98 Object Navigator Fife xi Flowsheets Unit Operations Filter Chiller
25. 12 Close the view to return to the PFD 1 63 Steady State Simulation When HYSYS created the Balance and new stream their icons were probably placed in the far right of the PFD If you like you can click and drag the Balance and SalesDP icons to a more appropriate location such as immediately to the right of the SalesGas stream Installing the Second Mixer In this section you will install a second mixer which is used to combine the two liquid streams SepLig and LTSLiq into a single feed for the Distillation Column 1 Inthe PFD make some empty space available to the right of the LTS using the horizontal scroll bar Click the Mixer button on the Object Palette In the PFD position the cursor to the right of the LTSLiq stream icon 4 Click to drop the Mixer onto the PFD A new Mixer named MIX 101 appears Mixer icon 5 Press and hold the CTRL key to temporarily enable Attach mode while you make the Mixer connections 6 Position the cursor over the right end of the LTSLiq stream icon The connection point and pop up Out appears Multiple connection points 7 With the pop up visible click and drag the cursor toward the left appear becalse ie Mixer inlet side of the Mixer and multiple connection points appear at accepts multiple feed streams the Mixer inlet 8 Place the cursor near the inlet area of the Mixer When the solid white box appears at the cursor tip release the left mouse button to
26. 2 Inthe Name field change the operation name to Chiller Figure 1 65 Chiller Design Name Chiller Connections Parameters Inlet Energy User Variables Cool as v jo 100 Notes Outlet 7 Fluid Package Basis 1 Design Rating Worksheet Performance Dynamics Delete lt UrknownDetaP T Cre 3 Select the Parameters page 4 Inthe Delta P field specify a pressure drop of 10 psi Figure 1 66 Chiller Design Connections Parameters Delta P Duty User Variables 10 00 psi Design Rating Worksheet Performance Dynamics Delete o krom T dr 5 When you are finished close this view Gas Processing Tutorial 1 55 At this point the Chiller has two degrees of freedom one of these will be exhausted when HYSYS flashes the CoolGas stream after the exchanger temperature approach is specified To use the remaining degree of freedom either the Chiller outlet temperature or the amount of duty in the Chiller energy stream must be specified The amount of chilling duty which is available is unknown so you will provide an initial guess of 0 F for the Chiller outlet temperature Later this temperature can be adjusted to provide the desired sales gas dew point temperature 6 Double click on the outlet stream icon 1 to open its property view 7 Inthe Name field change the name to ColdGas 8 Inthe Temperature field specify a temperature of 0 F The remaining degree of
27. 3 Install the hypothetical components into the fluid package 2 19 Steady State Simulation HYSYS has given the new Assay the default name of Assay 1 You can change this by typing a new name in the Name field 2 20 Defining the Assay 1 On the Assay tab click the Add button to create and view a new Assay The Assay view appears Figure 2 18 Ni Assay Assay 1 Assay Definition Input Data Bulk Properties Not Used Assay Data Type None v Light Ends Handling amp Bulk Fitting Options m Input Data Calculation Defaults Working Curves Correlations User Curves Delete Name Assay _ Assap Was Not Calculated Calculate When the property view for a new Assay is opened for the first time the view contains minimal information Depending on the Assay Data Type you choose the view is modified appropriately For this example the Assay is defined based on TBP data Refining Tutorial 2 21 2 From the Assay Data Type drop down list select TBP The view is customized for TBP data Figure 2 19 Ni Assay Assay 1 of x Assay Definition Input Data Bulk Properties Not Used x Assay Basis Mole t Assay Data Type H Assay Percent Light Ends Ignore v Molecular Wt Curve Not Used Density Curve Not Used x Viscosity Curves Not Used v TBP Distillation Conditions Atmospheric C Yacuum Light Ends Handling amp Bulk Fit
28. 415 8 300 0 485 9 482 1 467 3 300 0 31 70 31 70 50 00 30 99 30 99 30 99 50 00 2785 143 7 2500 781 4 292 8 655 1 166 5 1 393e 005 5 759e 004 4 504e 004 2 196e 005 3 239e 004 1 902e 005 3000 1 142e 004 5001 3090 1 969e 004 2897 1 700e 004 205 8 2 997e 008 P _1_Draw 4 034e 007 P _1_Return 2 547e 008 PA_2_Draw 1 436e 008 P _2 Return 3 348e 007 PA_3_Draw 0 0000 0 0000 0 0000 1 271e 008 PA _3_ Return 1 697e 007 x New x 0 0000 0 0000 311 2 126 6 485 9 600 9 465 3 28 84 28 84 30 99 31 70 31 70 3048 3048 1191 965 2 965 2 282e 005 282e 005 3 345e 005 3 345e 005 3 41 7e 005 3 417e 005 000e 004 000e 004 3 000e 004 3 000e 004 3 001e 004 3 001e 004 4 100e 008 4 650e 008 2 188e 008 2 538e 008 1 920e 008 2 270e 008 Energy Streams Unit Ops Condenser Main TS L Show Name Only Number of Hidden Objects 0 tT Enter Parent Simulation Environment icon The PFD shown in the Figure 2 119 has been manually rearranged by moving some of the stream icons and by enlarging the furnace icon Workbook Case Main Name emperature F iquid Volume F
29. 905 4 Mass Flow lb hr Liquid Yolume Flow barrel day 7 241e 005 5 000e 004 7 241e 005 5 000e 004 4 761e 009 7 035e 005 4 827e 004 4 661e 009 7 035e 005 4 827e 004 4 737e 009 2 061e 004 1732 4 955e 007 Material Streams Compositions Energy Streams Unit Ops FeederBlock_SourH20 Feed LJ Include Sub Flowsheets Feed Bottoms L Show Name Only Number of Hidden Objects Compositions Tab Figure R2 6 Workbook Case Main og Ioj x Name o f SouH20 Feed Stripper Feed Stripper Bottom Comp Mass Frac H25 0 0132 0 0000 Comp Mass Frac Ammonia 0 0047 0 0000 Comp Mass Frac H20 0 9821 1 0000 Name Effluent Off Gas New Comp Mass Frac H25 0 0000 0 4625 Comp Mass Frac Ammonia A 0 0000 0 1648 Comp Mass Frac H20 1 0000 0 3727 Material Streams Compositions Energy Streams Unit Ops FeederBlock_SourH20 Feed LJ Include Sub Flowsheets Feed Bottoms L Show Name Only Number of Hidden Objects 0 R2 8 Sour Water Stripper R2 9 Energy Streams Tab Figure R2 7 Workbook Case Main a Name Q Reb Q Cond Heat Flow Btu hi 2 073e 008 1 571e 008 Material Streams Compositions Energy Streams Unit Ops Sw Stripper C Include Sub Flowsheets pe L Show Name Only Number of Hidden Objects 0 R2 9 R2 10 R2 10 Case Study Ae 6 Case Study The simulatio
30. Any other library components 1 Setup The component list must include C1 to C4 light ends ae for the oTa re components as well as the hypocomponents that will be used to Savon Nene represent the C5 portion of the crude oil The Oil Characterization be selected as well i procedure in HYSYS will be used to convert the laboratory data into petroleum hypocomponents 2 Steady State Simulation This case will be modeled using a Pre Fractionation Train consisting of a Separator and Heater The Outlet stream will then fed to an Atmospheric Crude Fractionator The results will be displayed Dynamic Simulation The steady state solution will be used to size all the unit operations and tray section An appropriate control strategy will be implemented and the key variables will be displayed on a strip chart RB Setup 6 Setup This example will be developed using Field units Oil Environment icon R1 6 Ale Setup From the Tools menu select Preferences and set the unit set to Field units Variables tab Units page Next you will establish the property package and Component Basis that will be used in the simulation Al 2 1 Components amp Fluid Package 1 Define a fluid package with Peng Robinson as the Property Package 2 Create a components list that contains the following methane ethane propane i butane n butane and water as components Al 2 2 Oil Characterization Click the Oil Environment icon to enter t
31. Delete Name Component List 1 10 When Propylene Glycol is selected in the list press the ENTER key to add it to the Selected Components list Finally you will add the component H20 11 In the Filter view clear the Alcohols checkbox by clicking on it 12 Ensure the Match field is empty by pressing ALT M and then the DELETE key 13 H20 does not fit into any of the standard families so click on the Miscellaneous checkbox 14 Scroll down the filtered list until H20 is visible then double click on H20 to add it to the Selected Components list 3 13 A component can be removed from the Selected Components list by selecting it and clicking the Remove bution or the DELETE key 3 14 Steady State Simulation 15 The final component list appears below Figure 3 15 Selected Components lt Add Pure lt Substitute gt Remove gt Sort List View Component Viewing Component Properties To view the properties of one or more components select the component s and click the View Component button HYSYS opens the property view s for the component s you select 1 Click on 12C3diol in the Selected Components List 2 Click the View Component button The property view for the component appears Figure 3 16 iojxi Component Identification i Alcohol C3H802 500 CAS Number UNIFAC Structure CH3 CH2 CH OH 2 User ID Tags TagNumber Tag Text lt
32. Figure 1 155 4 DataBook Available Data Entries Object Variable Sales Gas Production Liquid Production LTS Temp Insert Delete ia Variables Process Data Tables Strip Charts Data Recorder Case Studies For more information refer to In the next set of steps you will add all of the variables that you would Using the Databook on like to manipulate or model page 78 e Include feed and energy streams that you want to modify in the dynamic simulation e Include unit operation temperature levels and pressures that you want to monitor and record 2 On the Variables tab click the Insert button The Variable Navigator appears Figure 1 156 Variable Navigator Iof xX Flowsheet Object Variable Case Main Heavy Liquid Fractior a DePropanizer COL1 Higher Heating Value Add Kinematic Viscosity gt Object Filter Light Liquid Fraction Liq Mass Density es Al C Streams Lig Yol Flow Std C Liquid Fraction Lower Heating Yalue UnitOps Navigator Scope gt Mass Density C Logicals oa Mass Enthalpy C ColumnOps C Case C Custom C Basis Mass Heat Capacity Ti Utility Mass Heat Of Vapour Etom Mass Higher Heating Se Mass Lower Heating hd alar Monciti Variable Description Mass Flow Cancel 1 127 Select Case Main in the Flowsheet group to ensure you can find all streams and operations The purpose of selecting mani
33. Inlets Outlet Feed 1 Flid Package Basis 1 v Design Rating Worksheet Dynamics Delete MMe M ooe 8 Select Feed 1 from the list The stream is transferred to the list of Inlets and lt lt Stream gt gt is automatically moved down to a new empty cell 9 Repeat steps 1 3 to connect the other stream Feed 2 HYSYS recognizes that there is no existing stream named MixerOut so it will create the new stream with this name HYSYS has calculated the outlet stream by combining the two inlets and flashing the mixture at the lowest pressure of the inlet streams In this case both inlets have the same pressure 600 psia so the outlet stream is set to 600 psia Gas Processing Tutorial The status indicator now displays Requires a product stream Next you will assign a product stream 10 Move to the Outlet field by clicking on it or by pressing TAB 11 Type MixerOut in the cell then press ENTER The status indicator now displays a green OK indicating that the operation and attached streams are completely calculated gt MIX 100 Design Name MIx 00 Connections Parameters User Variables Notes Inlets Outlet Feed 1 M ixerOut Feed 2 Fluid Package B asis 1 Design Rating Worksheet Dynamics Delete ET onc 12 Click the Parameters page 13 In the Automatic Pressure Assignment group leave the default setting at Set Outlet to Lowest Inlet Figure 1 44
34. Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment 3 23 Steady State Simulation Making the Reaction Set Available to the Fluid Package The final task is to make the set available to the Fluid Package which also makes it available in the flowsheet 1 Click on Set 1 in the Reaction Sets group on the Reactions tab 2 Click the Add to FP button The Add Set 1 view appears This view prompts you to select the Fluid Package to which you would like to add the reaction set In this example there is only one Fluid Package Basis 1 Figure 3 29 Add Set to Fluid Package 3 Select Basis 1 then click the Add Set to Fluid Package button Figure 3 30 Reaction Sets Global Rxn Set View Set Set Add Set Delete Set Copy Set Assoc Fluid Pkgs Import Set Basis 1 Export Set 3 24 Chemicals Tutorial 3 25 4 Click the Fluid Pkgs tab to view a summary of the completed Fluid Package Figure 3 31 Simulation Basis Manager Current Fluid Packages rFlowsheet Fluid Pkg Associations FlowSheet Fluid Pkg To Use Import 1 l Export Default Fluid Pkg Basis 1 x E Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment The list of Current Fluid Packages displays the new Fluid Package Basis 1 showing the nu
35. Temperature F Pressure psia Mass Flow lb hr Main Steam 375 00 150 00 7500 00 Diesel Steam 300 00 50 00 3000 00 AGO Steam 300 00 50 00 2500 00 Atmospheric Crude Tower RIS Crude Tower R1 13 Column Note that Input Experts The main column Atms Tower is represented by the following Preferences have been BEN Off ae ihe Colui e Number of stages is 29 ideal stages not including the is being configured directly condenser through the Property View e The overhead condenser operates at 19 7 psia and the bottom stage at 32 7 psia e The condenser experiences a 9 psi pressure drop e The temperature estimates for the condenser top stage and bottom stage are 100 F 250 F and 600 F respectively e Condensed water is removed via a water draw from the three phase condenser HYSYS comes with a 3 Stripper Crude Column template A Refluxed Absorber template could also be used but this would add the procedure of installing Side Strippers and Pump Arounds For this example install the 3 Stripper Crude Column custom template 1 Select the Custom Column icon in the Object Palette then click the Read an Existing Column Template button The Available Column Templates finder view appears In the Files of type drop down list select Column Templates col Custom Column icon From the list select the 3sscrude col template file then click the Open button The 3sscrude col template installed
36. macro uses the GetObject method to open the target link case which will initially be hidden lt then attempts to locate the material stream named by the LinkStream variable in the target case If a stream is attached to the Feeds1 nozzle of the User Unit Op the stream conditions and compositions are then copied between the streams All the stream names are in lower case Building Flowsheet 1 The use of the DuplicateFluid method to copy the stream parameters requires identical property packages in both simulation cases The example code instead uses a technique of explicitly copying T and P and then searches for components by name in order to copy their molar flow Components that are not available in the target case are ignored Also the definition of User Unit Op usually involves the definition of three macros e Initialize e Execute e StatusQuery For this example the StatusQuery macro is commented out to avoid the overhead of having that macro called Removing the StatusQuery code entirely would accomplish the same thing but it is highly recommended that StatusQuery be implemented to provide valuable user feedback This implementation is left as an exercise for the user X12 Building Flowsheet X1 2 1 Setup 1 Define a Peng Robinson Stryjek Vera PRSV property package 2 Select the following components C1 C2 C3 i C4 3 Set the unit preferences to SI X1 2 2 Installing Streams Specify streams
37. the column pressure drop is user specified In dynamics it is calculated using dynamic hydraulic calculations Complications will arise in the transition from steady state to dynamics if the steady state pressure profile across the column is very different from that calculated by the Dynamic Pressure Flow solver Column Tray Sizing 1 From the Tools menu select Utilities Add a Tray Sizing utility to size the DEA Contactor tray section Click the Select TS button The Select Tray Section view appears From the Flowsheet list select DEA Contactor From the Object list select TS 1 4 Click the Auto section button to calculate the tray section dimension Accept all the defaults 5 Select the Trayed radio button in the Section Results group Performance tab Results page 6 Confirm the following tray section parameters for Section_1 VEUF Lol Value Section Diameter 3 5 ft Weir Length 34 81 in 7 Select the Trayed radio button in the Section Results group The number of flow paths for the vapour is 1 8 Calculate the Actual Weir Length using the Weir Length divided by the number of flow paths for the vapour Variable Value Actual Weir Length Weir Length 1 34 81 in 9 Open the DEA Contactor column property view 10 Click the Rating tab then select the Tray Sections page G1 22 Acid Gas Sweetening with DEA 11 Enter the tray section parameters for TS 1 obtained from the tray sizing ut
38. 1 000e 005 lt empty gt Heat Flow Btu hr 7 619e 008 lt empty gt Material Streams Compositions Energy Streams Unit Ops ProductBlock_Bottom Steam LJ Include Sub Flowsheets FeederBlock_Bottom Steam L Show Name Only Number of Hidden Objects 0 2 41 Steady State Simulation In the Mass Flow cell enter 7500 lb hr Create a new utility stream called Diesel Steam Define the conditions of this stream as follows e Temperature 300 F e Pressure 50 psia e Mass Flow 3000 lb hr The Workbook view appears as shown below Figure 2 44 Name Preheat Crude Bottom Steam Diesel Steam Vapour Fraction 0 1292 lt empty gt lt empty gt Temperature F 450 0 375 0 300 0 Pressure psia 75 00 150 0 50 00 7 619e 008 lt empty gt lt empty gt xx New xx Molar Flow Ibmole hr 3814 lt empty gt lt empty gt 1 144e 006 7500 1 000e 005 lt empty gt lt empty gt Heat Flow Btu hr Vapour Fraction Material Streams Compositions Energy Streams Unit Ops ProductBlock_Diesel Steam LJ Include Sub Flowsheets FeederBlock_Diesel Steam _ Show Name Only Number of Hidden Objects Providing Compositional Input Now that the utility stream conditions have been specified the next task is to input the compositions 1 Click the Compositions tab in the Workbook The components are listed by Mole Fraction by default 2 Inthe Bottom Steam column click in th
39. 7 036e 004 7 465e 004 4290 Heat Flow Btu hr 2 626e 007 3 350e 007 1 064e 008 2 043e 006 Material Streams Energy Streams Feed Main Stripper L Show Name Only Number of Hidden Objects 0 Compositions Tab Figure P1 5 Workbook T 100 COL1 A Yee To Reboiler Name Comp Mole Frac Workbook Pr 0 4000 0 9157 Comp Mole Frac Workbook Pr 0 6000 0 0843 Name Propane To Condenser Propene Comp Mole Frac Workbook Prd 0 9251 0 0105 Comp Mole Frac Workbook Pr 0 0749 0 9895 0 9895 L Material Streams Compositions Energy Streams Feed Main Stripper L Show Name Only Number of Hidden Objects 0 P1 10 Propylene Propane Splitter P1 11 Energy Streams Tab Figure P1 6 Workbook T 100 COL1 Reboiler Duty Condenser Duty Heat Flow Btu hr 6 396e 007 7 090e 007 Material Streams Compositions Energy Streams Unit Ops Reboiler L Show Name Only Number of Hidden Objects 0 P1 11 P1 12 Ethanol Plant C1 1 Cl Ethanol Plant Civ Process DESCrIDUON sioari ccceadiccceceernieiedncdeecicndee lenin ainda 3 C12 SOU neri aaia eee tan duane Caen duillia 6 C1 3 Steady State Simulation cccceeceeeeeeeeseeeeceeseeeseeeneeseeeenseeseoees 6 C1 3 1 AddagStreams 0 OA cece ccesseeseesssceseneeessscoees 6 C1 3 2 ldstalling Equipment 00 NA aannaai
40. Case Main hoon 10 x Name Wash 20 Yapour Fraction 0 0000 FromFerm 0 0277 Steam A 1 0000 To CO2 Wash 1 0000 Beer 0 0000 CO2 Stream 1 0000 Temperature C 25 00 30 00 140 0 30 00 30 00 26 06 E E Pressure kPa 101 3 107 3 101 3 101 3 101 3 101 3 Molar Flow kgmole h 130 0 2400 610 6 66 47 2334 64 72 Mass Flow kg h Liquid Volume Flow m3 h Heat Flow kJ h Name 2342 2 347 3 704e 007 To Fermenter 4 672e 004 48 16 6 892e 008 To Light 1 100e 004 11 02 1 448e 009 Stillage 2857 3 454 2557e 007 Rect Feed 4 386e 004 44 70 6 636e 008 Light Vent 2792 3 375 2 515e 007 2ndEtOH Vapour Fraction 0 0000 1 0000 0 0000 1 0000 1 0000 0 0000 Temperature C Pressure kPa Molar Flow kgmole h 33 34 101 3 85 89 101 3 100 3 102 3 94 82 101 6 46 40 101 3 46 40 131 8 10 03 2617 316 6 1 600 Mass Flow kg h 2407 301 9 4 716e 004 7402 68 89 Liquid Yolume Flow m3 h 2 426 0 3511 47 25 8 126 8 37 9e 002 Heat Flow kJ h Name Vapour Fraction 3 745e 007 To Rect 0 0000 Temperature C 80 85 2 556e 006 Rect Yap 1 0000 78 01 7 308e 008 Rect Dist 0 0000 7 506e 007 Stillage B 0 0000 78 01
41. Design Parameters 1 972e5 1 972e5 Btwhr Comments Add this pump m the stream REGEN BTTMS and the recycle RCY 2 G1 18 Add Valves Acid Gas Sweetening with DEA 149 Gas Sweetening with DEA G1 19 Add the following valves to define the pressure flow relation Valve Name Tab Page Design Connection Worksheet Conditions Rating Sizing Tab Page Design Connection Worksheet Conditions Rating Sizing Tab Page Design Connection Design Parameters Rating Sizing Comments Tab Page Design Connection Design Parameters Rating Sizing Comments VLV FWKO Inlet Outlet Pressure FWKO 1 Valve Opening VLV Flash Vap Inlet Outlet Pressure Flash Vap 1 Valve Opening VLV 101 Inlet Outlet Delta P Valve Opening FWKO FWKO 1 986 5 psia 50 FLASH VAP FLASH VAP 1 89 99 psia 50 RICH TO VALVE RICH TO L R 5 8 psi 50 Add this valve between the pump P 101 and the stream RICH TO L R VLV 102 Inlet Outlet Delta P Valve Opening Emere OOOO Add this valve between the stream REGEN BTTMS TO VALVE and the recycle RCY 2 G1 19 Dynamic Simulation Valve Name VLV 103 Tab Page Design Connection Feed Product Delta P 1 psi Valve Opening 50 Add this valve between MIX 100 and the stream DEA TO COOL VLV 100 COL1 Tab Page In this cells Design Connection 1 COL1 SWEET GAS COL1 Design Parameters 1 psi Rating Sizi
42. Dynamic mode Recycle RCY 2 Connections REGEN BTTMS G1 17 GB Dynamic Simulation 8 Dynamic Simulation Delete the Std Ideal Liq Vol Flow value in stream DEA TO COOL Specify the Std Ideal Liq Vol Flow in stream MAKEUP H20 at 2 195 USGPM 6 Delete MIX 100 and replace it with a tank V 101 Name the vapour outlet from the tank Nitrogen Blanket 7 Change the Heat Exchanger model of the E 100 exchanger from Exchanger Design End Point to Dynamic Rating Delete the temperature of the REGEN FEED stream since it will be calculated by the exchanger Use the following table to set the new specifications for the exchanger Heat Exchanger E 100 Tab Page In this cells Enters O Design Connections Shell Side Inlet REGEN BTTMS TO L R Design Parameters Heat Exchanger Model Dynamic Rating Add Pumps Add the following pumps to define the pressure flow relation Two pumps are added Pump Name P 101 because Dynamics mode performs rating calculations Tab Page In this cell Enter Mia Consider pro surg Design Connection RICH TO PUMP differences and flow resistance To accommodate Outlet RICH TO VALVE this you add equipment that Q 100 significantly impacts the pressure and drives flow Design Parameters 3739 72 Btu hr Comments Add this pump between the separator FLASH TK and the stream RICH to L R P 102 Tab Pagel _ Design Connection REGEN BTTMS REGEN BTTMS TO VALVE 001
43. F 2 Click the Size icon on the PFD button bar and a frame with eight sizing handles appears around the tray section icon Size icon 3 Place the cursor over the handle at the middle right of the icon and the cursor changes to a double ended sizing arrow 4 With the sizing cursor visible click and drag to the right An outline appears showing what the new icon size is when you complete the next step Rj lt A A 5 When the outline indicates a new icon size of about 1 5 to 2 times the width of the original size release the button The tray section icon is now re sized 6 Click the Size icon again to return to Move mode The final task is to customize the PFD by moving some of the streams Hf 8 and operation labels names so they do not overlap To move a label 7 Click on the label you want to move 2 8 Right click and select Move Size Label i 8 z 9 Move the label to its new position by clicking and dragging it or by pressing the arrow keys HA You can also move the icon on its own simply by clicking and dragging it to the new location 10 When you are finished working with the maximized Column PFD click the Restore icon for the PFD not for the HYSYS Application view in the upper right corner of the view of the PFD The PFD returns to its previous size 11 You can manually resize the view and expand the PFD to fill the new size by again clicking the Zoom All icon in the lowe
44. Hoverl extUnitS et Delete HoverT estUnitSet2 Unit Set Name fField U SGPM Display Units Add Delete A X t Tray Sizing Save Preference Set Load Preference Set 7 Your new unit set is now defined Close the Session Preferences view 3 3 8 Steady State Simulation L New Case Icon All commands accessed via the tool bar are also available as menu items HYSYS displays the current Environment and Mode in the upper right corner of the view Whenever you begin a new case you are automatically placed in the Basis Environment where you can define your property package and components The Simulation Basis Manager allows you to create modify and otherwise manipulate Fluid Packages in your simulation case Most of the time as with this example you will require only one Fluid Package for your entire simulation HYSYS has created a Fluid Package with the default name Basis 1 You can change the name of this fluid package by typing a new name in the Name cell at the bottom of the view 3 8 3 c 3 Defining the Fluid Package 1 Click the New Case icon The Simulation Basis Manager appears Simulation Basis Manager m loj xj Component Lists View Add Delete Copy Import Export Refresh Fluid Pkgs Master Component List Components UserProperty Hypotheticals j OilManager Reactions Component Maps T
45. Include Sub Flowsheets FeederBlock_Feed 1 L Show Name Only Number of Hidden Objects 0 Alternative Methods for Defining Streams In addition to the method you just learned there are several alternative ways to define streams via the Workbook 1 The Object Palette should be visible if not press F4 2 To add another feed stream do any one of the following dd Object Icon gt Press F11 e From the Flowsheet menu select Add Stream e Double click the Material Stream icon on the Object Palette fens x e Click the Material Stream icon on the Object Palette then click on the Add Object icon a n Each of these four methods displays the property view for the new stream which will be named according to the Automatic Naming of N Flowsheet Objects setting defined in the Session Preferences Material Simulation tab Naming page HYSYS will name new material streams tream i i D i with numbers starting at 1 and new energy streams starting at Q 100 When you initially access the stream property view the Conditions page on the Worksheet tab is the active page and 1 appears in the Stream Name cell 1 28 Steady State Simulation Next you will define this second feed stream 3 Inthe Stream Name cell replace the name by typing Feed 2 then press ENTER All these variables are in the 4 default units Enter the following values e Temperature 60 e Pressure 600 e Molar Flow 4 Figure 1 29 Feed 2 Wo
46. Liquid volume Percent Input Data Calculation Defaults Refining Tutorial 2 29 The independent x axis variable is the Assay percent while the dependent variable is the TBP in E You can view any of the other input curves by selecting the appropriate variable in the Property drop down list The remaining tabs in the Assay property view provide access to information which is not required for this tutorial 9 Close the Assay view to return to the Oil Characterization view Cutting the Assay Creating the Blend Now that the assay has been calculated the next task is to cut the assay into individual petroleum hypocomponents 1 Click the Cut Blend tab of the Oil Characterization view 2 Click the Add button HYSYS creates a new Blend and displays its property view Figure 2 29 Ni Blend Blend 1 il Ed Assay Selection and Oil Information gt Cut Ranges Available Assays Dil Flow Information Cut Option Selection Auto Cut v Assay 1 Dil Flow Units Flow Rate Data Correlations Property Plot Distribution Plot Composite Plot Plot Summary Delete Name Blend Blend Was NotCaleusted 3 In the list of Available Assays select Assay 1 2 29 2 30 Steady State Simulation 4 Click the Add button There are two results e The Assay is transferred to the Oil Flow Information table When you have only one Assay there is no need to enter a Flow Rate in this table e A Ble
47. Molar Mass C Liquid Volume Yap Phase Fraction 0 60531 Temperature 623 56 Pressure 65 000 Molar Flow 6231 1 Mass Flow 1 2850e 006 Std Ideal Lig Yol Flow 1 000e 005 Molar Enthalpy 1 201e 005 Molar Entropy 161 81 z 0 000284 0 000624 0 008618 0 005439 0 019285 0 000000 0 036381 0 041615 0 043817 Cancel OK 13 Click on the OK button to copy the Atm Feed stream information to the Store stream Figure 2 150 Conditions Temperature F Vapour Phase Fraction 0 60531 623 56 Properties Pressure psia 65 000 Composition Molar Flow Ibmole hr 6231 1 Mass Flow lb hr 1 2850e 006 K Value Std Ideal Lig Vol Flow barrel day 1 0000e 005 User Variables Molar Enthalpy Btu Ibmole Molar Entropy Btu lbmole F 1 201e 005 161 81 Notes Heat Flow Btuhr 748466408 Cost Parameters Lig Vol Flow Std Cond barrel day 1 0042e 005 Fluid Package lt Worksheet Attachments Dynamics Delete 14 Close the Store stream view Basis 1 b Dynamic Simulation 15 Delete all material streams and unit operations upstream of the Atm Feed stream The following eight items should be deleted When you delete a stream unit or logical operation from the flowsheet HYSYS asks you to confirm the deletion If
48. S E M Water Draw using this Overhead _ Optional Side Draws liquid product field lt Stream gt gt Although the overhead vapour product has zero flow do not change the condenser to Total At this time only the Partial radio button allows you to specify a three phase condenser 1 Clickin the top Ovhd Outlets field 2 Enter Off Gas as the name of the overhead vapour product stream HYSYS creates and attaches a new stream with this name 3 Press TAB again to move to the bottom Ovhd Outlets field and enter the new stream name Naphtha The next task is to attach the water draw stream to the condenser 4 Inthe Optional Side Draws table click in the lt lt Stream gt gt cell 5 Enter the name of the draw stream WasteH2O HYSYS automatically places a hydrocarbon liquid indicated by the Lin the Type column draw on stage 15 You will change this to a condenser water draw 2 69 2 0 Steady State Simulation Click on the Type cell the L for the WasteH20 stream Specify a water draw by typing W then pressing ENTER or by selecting W from the drop down list Click on the Draw Stage cell 15_Main TS for the WasteH20 stream Select Condenser from the drop down list The condenser is now three phase Figure 2 81 Condenser orGa Fj C Total Off Gas f Partial Ovhd Outlets C Full Rflg Naphtha IV Water Draw WasteH20 Optional Side Draws WasteH20 wW lt lt Stream gt g
49. SEIE 5 678e 005 1st Prod 0 0000 78 09 7 444e 005 Fusel 0 0000 83 39 Pressure kPa 101 3 101 3 101 3 101 3 101 3 101 3 Molar Flow kgmole h 5 742 Mass Flow kg h _ l Liquid Volume Flow m3h Heat Flow kJ h Name 128 2 0 1388 0 1000 4 306 5 360e 003 4 653e 002 2 000 2 489e 003 253 1 4566 4 578 69 04 2955 3 675 8 660e 002 3 541 2 003 3 000 1 602e 006 xx New xx 2 324e 004 1 261e 004 7 068e 007 1 67 1e 007 2 435e 004 Thaman Dentin E Tz Material Streams FeederBlock_Wash H20 CO2 Wash Energy Streams Unit Ops J Include Sub Flowsheets J Show Name Only Number of Hidden Objects C1 13 Bs gt Compositions Tab Figure C1 7 Workbook Case Main o p o x Name O O OO Wash 20 FromFerm SteamA ToCO2 Wash Beer CO2Stream Comp Mole Frac Ethanol 0 0000 0 0269 0 0000 0 0170 0 0272 0 0000 Bj Comp Mole Frac H20 1 0000 0 3464 1 0000 0 0403 0 9722 0 0333 Comp Mole Frac C02 0 0000 0 0266 0 0000 0 9421 0 0005 0 9667 Comp Mole Frac Methanol 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac AceticAcid 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 1 Propanol 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 2 Propanol 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 1 Butanol 0
50. Stream making this stream accessible to the Template Environment 6 Enter the Column Environment by clicking the Column Environment button at the bottom of the Column property view P1 5 P1 6 Steady State Simulation Column Object Palette 2 Tray Section icon Define the Number of Trays on the Parameters page first P1 6 For this example you will need a Total Condenser Reboiler and two Tray Sections A Tray Section and a Condenser will be used for the Refluxed Absorber Rectifier a Reboiler and another Tray Section will be used for the Reboiled Absorber Stripper The overhead product from the Stripper will serve as the feed to the Rectifier and the bottoms product from the Rectifier provides a second feed to the Stripper entering at Stage 1 P1 3 2 Adding the Stripper Reboiled Absorber Install the Reboiled Absorber before the Reboiler This column has 94 ideal stages and a Reboiler Ensure that you are within the Column Environment the PFD view and the Column Object Palette should be visible as shown on the left Installing the Tray Section For this Column a new Tray Section has to be installed 1 Double click the Tray Section icon on the Object Palette The tray section appears in the PFD and the Tray Section property view appears 2 Supply the following information Tray Section Stripper Tab Page inthis cells Enters 3 Close the Tray Section view Reboiler icon
51. T 100 COL1 Condenser Overall U Degree of Subcool Distillate Mass Flow Object Filter Distillate Molar Flow All Distillate Volume Flow P4_1_Cooler Duty Streams PA_2 Cooler Heavy Liquid Mass Fl UnitOps Navigator Scope PA_3 Cooler Heavy Liquid Molar FI Lagicals Flowsheet peni asp aes ColumnOps C Case Level Tap Liquid Custom Basis i Custom Utility igui i Liquid volume Resear liana titah irna CP WISCONMes Variable Description Liquid Percent Level Cancel 2 131 2 132 Dynamic Simulation 7 Inthe Output Target Object group click the Select OP button then select the information as shown in the figure below Click the OK button when you are finished Figure 2 168 Select OP Object For Cond LC EA Flowsheet Case Main AGO_SS_Draw OK T 100 COL1 Atmos Cond Diesel_55_Draw Object Filter Kero_SS_ Draw C All Kero_SS_Energy Streams UnitOps C Logicals ColumnOps Custom Custom Waste Water Cancel 8 Click the Parameters tab then select the Configuration page 9 Supply the following for the Configuration page In this cell Enter 10 Click the Control Valve button The FCV for Reflux view appears 11 In the Max Flow cell of the Valve Sizing group enter 2000 kgmole h Figure 2 169 Valve Sizing MolarFlow 1 0000 kamole h Max Flow 2000 kamole h 12 Close the FCV for Reflux view For more information regard
52. calculated with the above formula Specify the Level Calculator as a Horizontal cylinder Open the Reboiler property view Click the Worksheet tab then select the Conditions page Confirm the following Std Ideal Liquid Volume Flow Stream Std Ideal Liquid Volume Flow To Reboiler 239 7 bbl day 11 12 13 Calculate the vessel volume using Equation G1 1 and assuming a 50 liquid level residence time Click the Dynamics tab then select the Specs page In the Model Details group specify the vessel volume as 641 ft and the Level Calculator as a Horizontal cylinder Separator Sizing l Use a residence time of 5 min and a 50 liquid level to size the separator FLASH TK Confirm the Std Ideal Liquid Volume flow in the table below and enter the vessel volume Acid Gas Sweetening with DEA 3 Click the Rating tab then select the Sizing page Select the Vertical orientation radio button for the separator Separator Name FLASH TK Tab Page In this cell Enters Worksheet Conditions Std Liq Vol Flow RICH TO L R 498 27 USGPM V 100 EE inthis cels Leh The vapour flow rate through V 100 is large as compared to the liquid flow rate therefore Separator V 100 is sized according to the terminal vapour velocity Vertical Cylinder Tank Sizing The tank V 101 will be sized with a 10 minute liquid residence time and a 75 liquid level Confirm the volumetric flow rate of the exit stream and s
53. gt You can specify the exit 17 Close the Ovhd property view t t f the Heat R E Dynamic aes 18 In the PFD double click the Heater icon to access the property view The duty of the heater is back 19 Click the Dynamics tab then select the Specs page In the Model calculated to make the temperature specification Details group select the Product Temp Spec radio button Figure 1 148 Dynamics Model Details Sunes C Supplied Duty Number of Zones Holdup Duty Fluid Duty Btu h f ear Stripchart Dynamic Specifications Overall Delta P psi 9 000 F Overall k Ib hr sqrt psia Ib ft3 1613 M Calculate k Spec Zones Design Rating Worksheet Performance Dynamics Delete A S ooe 20 Close the view 21 Save the case as DynTUT1 3 hsc 1 118 Gas Processing Tutorial 1 119 1 3 4 Adding Controller Operations In this section you will identify and implement key control loops using PID Controller logical operations Although these controllers are not required to run in Dynamic mode they will increase the realism of the model and provide more stability PFD of the main flowsheet environment after all controllers are added Figure 1 149 gt Ovhd DePropanizer ES CondDuty LTSYap LiquidProd i ColdGas Chiller TowerFeed Feed 4 SalesGas gt MixerOut Feed2 x10 lt _______________ am LTSExit gt lt H Toverlnlet Towe
54. make the connection 9 Repeat the above steps to connect SepLiq to the Mixer 10 Move the cursor over the right end of the Mixer icon The connection point and pop up Product appears 11 With the pop up visible click and drag the cursor to the right of the Mixer A white arrow stream icon appears LTSLiq 12 With the stream icon visible release the mouse button HYSYS will create a new stream with the default name 1 13 Release the CTRL key to leave Attach mode epee MD lt 101 Gas Processing Tutorial 65 Processing Tutorial 1 65 ES Distillation Column icon The Input Expert is a logical sequence of input views that guide you through the initial installation of a Column Completion of the steps will ensure that you have provided the minimum amount of information required to define the column 14 Double click on the outlet stream icon 1 to access its property view When you created the Mixer outlet stream HYSYS automatically combined the two inlet streams and flashed the mixture to determine the outlet conditions 15 In the Stream Name cell rename the stream to TowerFeed then click the Close icon Installing the Column HYSYS has a number of pre built column templates that you can install and customize by changing attached stream names number of stages and default specifications In this section you will install a Distillation Column 1 From the Tools menu select Preferences 2 On the Si
55. n Butane i Pentane n Pentane n Hexane n Heptane n Octane n Nonane n Decane n C11 n C12 Cluster lt none gt ha Family Type Filter WM Use Filter J Hydrocarbons Solids Miscellaneous Amines Alcohols Ketones Aldehydes Esters M Caboxylic Acids Halogens P Nitriles Phenols Ethers User Defined All Invert The Match feature remains active when you are using a family filter so you could have also typed C3 in the Match field and then added it to the component list 10 Double click Propane to add it to the component list 2 12 To select consecutive components use the SHIFT key To select non consecutive components use the CTRL key Refining Tutorial Next you will add the remaining Light Ends components iC4 through nC5 The following procedure shows you quick way to add components that appear consecutively in the library list 11 Click on the first component to be added in this case iC4 12 Do one of the following e Hold down the SHIFT key and click on the last component in this case nC5 All components iC4 through nC5 are now selected Release the SHIFT key e Click and drag from iC4 to nC5 Components iC4 through to nC5 are selected 13 Click the Add Pure button The selected components are transferred to the Selected Component group Figure 2 12 Selected Components To remove a component from the n Pentane Tee
56. position the cursor over the top of the Separator icon The connection point and pop up Vapour Product appears With the pop up visible left click and hold Drag the cursor to the LTSVap stream icon A solid white box appears when you move over the connection point 4 Release the mouse button and the connection is made Figure 1 69 CoolGas ColdGas Chiller salesGas 5 Position the cursor over the bottom of the Separator icon The connection point and pop up Liquid Product appears With the pop up visible left click and hold Move the cursor to the right of the Separator A white arrow stream icon appears with a trailing line attached to the Separator liquid outlet 8 With the stream icon visible release the mouse button HYSYS creates a new stream with the default name 1 9 Click the Attach Mode icon to leave Attach mode 10 Double click on the stream icon 1 to open its property view 11 In the Stream Name cell type LTSLiq then press ENTER 12 Click the Close icon to close the stream property view 1 58 Steady State Simulation 13 Select Auto Position All from the PFD menu Your PFD should appear similar to the one shown below Figure 1 70 PFD Case Main OF x Hi 4 oY t R D A P D Default Colour Scheme LTS ap CoolGas Chiller Gas Gas b ColdGas SalesGas InletSep MixerOut MIx 100 Lm SepLig Streams LTSVap and LTSLiq 14 Double click the ic
57. you must have the Amines property package which is an optional property package A spreadsheet is used to calculate various loadings and verify that they are within an acceptable range B 1 a a B 2 Hefining Al Atmospheric Crude Tower Steady State Modeling Oil Characterization A preheated 450 F light crude 29 API is processed in an atmospheric fractionation tower to produce naphtha kerosene diesel atmospheric gas oil AGO and atmospheric residue products A complete oil characterization procedure is part of this example application Re Sour Water Stripper Steady State Modeling Sour Thermo Options Case Study Sour water is fed to a distillation tower for NH3 and HS removal The use of the Sour Peng Robinson Sour_PR is highlighted HYSYS s built in Case Study tool is used to examine the effects of varying column feed temperatures Petrochemicals PI Propane Propylene Splitter Steady State Modeling Column Sub flowsheet The individual Stripper tower and Rectifier tower components of a propane propylene splitter system are modeled Two separate towers in the same Column sub flowsheet are used in this example to illustrate the simultaneous solution power of HYSYS s Column sub flowsheet HYSYS Applications B 3 Chemicals CI Ethanol Plant Steady State Modeling An ethanol production process is modeled right from the fermentor outlet through to the production of low grade and high grade azeo
58. 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 3 M 1 C4ol 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 2 Pentanol 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac Glycerol 0 0000 0 0000 0 0000 0 0000 0 0000 Name To Fermentor To Light Stillage 4 Rect Feed Light Vent Comp Mole Frac Ethanol 0 0086 0 3164 0 0000 0 1903 0 1890 Comp Mole Frac H20 j 0 9910 0 5610 1 0000 0 8091 0 0517 Comp Mole Frac C02 0 0005 0 1213 0 0000 0 0000 0 7589 Comp Mole Frac Methanol 0 0000 0 0002 0 0000 0 0002 0 0001 Comp Mole Frac AceticAcid 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 1 Propanol 0 0000 0 0003 0 0000 0 0001 0 0001 Comp Mole Frac 2 Propanol 0 0000 0 0003 0 0000 0 0001 0 0002 Comp Mole Frac 1 Butanol 0 0000 0 0001 0 0000 0 0000 0 0000 Comp Mole Frac 3 M 1 C4ol _ 0 0000 0 0001 0 0000 0 0002 0 0000 Comp Mole Frac 2 Pentanol 0 0000 0 0003 0 0000 0 0000 0 0000 Comp Mole Frac Glycerol 0 0000 0 0000 0 0000 0 0000 0 0000 Name To Rect Rect Yap Rect Dist Stillage B 1st Prod Comp Mole Frac Ethanol 0 1513 0 8883 0 8886 0 0002 0 8826 Comp Mole Frac H20 0 8473 0 1057 0 1090 0 9995 0 1163 Comp Mole Frac CO2 0 0000 0 0024 0 0000 0 0000 0 0000 Comp Mole Frac Methanol 0 0001 0 0034 0 0022 0 0000 0 0003 Comp Mole Frac AceticAcid 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 1 Propanol 0 0003 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac 2
59. 1 72 The table in the Optional Checks group displays the lteration number Step size and Equilibrium error and Heat Spec error The column temperature profile appears in the Profile group You can view the pressure or flow profiles by selecting the appropriate radio button The status indictor has changed from Unconverged to Converged Gas Processing Tutorial Running the Column 1 73 1 Click the Run button to begin calculations The information displayed on the Monitor page is updated with each iteration The column converges quickly in three iterations Figure 1 92 L Column DePropanizer Z COL1 Fluid Pkg Basis 1 Peng Robinson Design Connections Monitor Specs Specs Summary Subcooling Notes Input Summary View Initial Estimates r ptional Checks Liter Step Equilibrium _ Heat Spec 0 004626 0 033156 0 000197 0 001220 0 000001 0 0001 oat Profile tf Temp C Press C Flows TT 000 MMSCFD 1 00 2 35 0 0000 EES 0 1750 Reflux Rate lt empty gt 2 35 lt empty gt Btms Prod Rate lt empty gt 0 632 lt empty gt Propane Fraction 2 000e 002 2 00e 002 0 0003 View Add Spec Group Active Update Inactive Degrees of Freedom fo ian Design Side Ops Worksheet Performance Flowsheet Reactions Dynamics
60. 11 All DePropanizer C Streams DewPoint eee UnitOps C Logicals C Custom Setup Custom The UnitOps radio button in the Filter group is currently selected so only the Unit Operations appear in the list of available objects 2 To open a property view select the operation in the list then click the View button or double click on the operation 3 To change which objects appear select a different radio button in the Filter group To list all streams and unit operations select the All button 4 You can also search for an object by clicking the Find button When the Find Object view appears enter the Object Name then click the OK button HYSYS opens the property view for the object When you are done close the Object Navigator view and any property views you opened Steady State Simulation Using the Databook The HYSYS Databook provides you with a convenient way to examine your flowsheet in more detail You can use the Databook to monitor key variables under a variety of process scenarios and view the results in a tabular or graphical format For this example the effects of LTS temperature on the Sales Gas dew point and flow rate and the Liquid Product flow rate will be examined Defining the Hey Variables Before opening the Databook close the Object Navigator or any property view you might have opened using the Navigator 1 To open the Databook do one of the following e Press CTRL D e Op
61. 2 5 G1 30 Acid Gas Sweetening with DEA Pressure Controllers Pressure Controller Name PIC 100 COL1 Tab Page Connections Process Object TS 1 COL1 Process Variable Top Stage Pressure Output Variable VLV 100 COL1 Ti 2 PIC 100 COL2 Tab Page inthis cell Enters Connections Process Object Condenser COL2 Process Variable Output Variable VLV 100 COL2 Parameters Configuration G1 31 Dynamic Simulation Flow Controller Flow Controller Name RECY FC Tab Page inthis cells Eterm 01 6 3 Preparing Dynamic Simulation Now that the case is ready to run in Dynamic mode the next step is installing a strip chart to monitor the general trends of key variables Monitoring in Dynamics You may use several variables in the same chart If you have a large number of variables that you would like to track use several Strip Charts rather than use all of the variables on one chart You may use the same variable in more than one Strip Chart G1 32 Acid Gas Sweetening with DEA For this simulation case use the Databook CTRL D to set up two strip charts as defined below StripChartl Contactor Flowsheet Object Ela tle StripCharte Regenerator Flowsheet Object Variable Start the Integrator and allow the variables to line out If you get an initial numerical error after you start the integrator start the integrator again In the Session Preferences view Simulati
62. 36 Steady State Simulation See Section 12 2 3 Naming Page in the User Guide for detailed information on setting your Session Preferences Alternatively you can make the connections by typing the exact stream name in the cell then pressing ENTER As with a stream a unit operation s property view contains all the information defining the operation organized in tabs and pages The four tabs shown for the Mixer namely Design Rating Worksheet and Dynamics appear in the property view for most operations More complex operations have more tabs HYSYS provides the default name MIX 100 for the Mixer As with streams the default naming scheme for unit operations can be changed on the Session Preferences view Many operations such as the Mixer accept multiple feed streams Whenever you see a table like the one in the Inlets group the operation will accept multiple stream connections at that location When the Inlets table has focus you can access a drop down list of available streams Now you will complete the Connections page 6 Click the lt lt Stream gt gt cell to ensure the Inlets table is active The status bar at the bottom of the view shows that the operation requires a feed stream 7 Open the lt lt Stream gt gt drop down list of feeds by clicking on or by pressing the F2 key and then the Down arrow key Figure 1 42 _ MIX 100 Design Name Mix 00 Connections Parameters User Variables Notes
63. 9 Click the Next button to advance to the Pressure Profile page 10 In the Condenser Pressure field enter 200 psia 11 In the Reboiler Pressure field enter 205 psia The Condenser Pressure Drop can be left at its default value of zero Figure 1 82 Ni Distillation Column Input Expert x Condenser Pressure 200 0 psia Condenser Pressure Drop 0 0000 psi Reboiler Pressure Pressure Profile page 2 of 4 Cancel 12 Click the Next button to advance to the Optional Estimates page Although HYSYS does not require estimates to produce a converged column good estimates will usually result in a faster solution 13 Specify a Condenser temperature of 40 F and a Reboiler Temperature Estimates of 200 F Figure 1 83 I Distillation Column Input Expert x Optional Condenser Temperature Estimate 40 00 F Optional Top Stage Temperature Estimate ene Optional Reboiler Temperature Estimate 200 0 F Optional Estimates page 3 of 4 Cancel 1 67 Steady State Simulation In general a Distillation Column has three default specifications however by specifying zero overhead liquid flow Full Reflux Condenser one degree of freedom was eliminated For the two remaining default specifications overhead Vapour Rate is an estimate only and Reflux Ratio is an active specification 1 68 14 Click the Next button to advance to the fourth and final page of the Input Expert This page a
64. Absorber column operation with the specifications shown below The Amines property package requires that real trays be modeled in the contactor and regenerator operations but in order to simulate this component specific efficiencies are required for H2S and CO2 on a tray by tray basis These proprietary efficiency calculations are provided in the column as part of the Amines package Tray dimensions must be supplied to enable this feature Absorber Column DEA CONTACTOR See ve O O OO Ovhd Vapour Outlet SWEET GAS Bottoms Liquid Outlet RICH DEA e a E a tare Steady State Simulation Using this information the component specific tray efficiencies can be calculated 3 Runthe Column 4 Once it has converged click the Parameters tab and select the Efficiencies page 5 Click the Component radio button and note the efficiency values for CO2 and H2S on each tray HYSYS provides an estimate of the component tray efficiencies but allows you to specify the individual efficiencies if required Figure G1 4 L Column DEA Contactor COL1 Fluid Pkg Basis 1 Amine Pkg LM Component Efficiencies Parameters Profle Efficiency Type H2S Methane C Overal 0 1872 0 5254 1 000 1 000 1 000 1 0C Estimates Seno 01878 0 5258 1 000 1 000 1 000 1 0C Efficiencies f Component 0 1883 0 5259 1000 1 000 1 000 1 0C 01890 0 5260 1000 1 000 1 000 1 0C Solver 01898 052
65. Atm Feed 0 60531 623 56 65 000 6231 1 1 2850e 006 1 0000e 005 1 201e 005 Molar Entropy Btu Ibmole F 161 81 Heat Flow Btu hr Lig Vol Flow Std Cond barrel day Fluid Package Dynamics preflash train 7 4846e 08 1 0042e 005 Basis 1 Refining Tutorial 2 5 2 Adding Equipment amp Sizing Columns In preparation for dynamic operation the column and side stripper tray sections and surrounding equipment must be sized In the steady state scenario column pressure drop is user specified In dynamics it is calculated using dynamic hydraulic calculations Complications arise in the transition from steady state to dynamics if the steady state pressure profile across the column is very different from that calculated by the Dynamic Pressure Flow solver The Cooler operations in the pump arounds are not specified with the Pressure Flow or Delta P option however each cooler must be specified with a volume in order to run properly in dynamic mode Column Tray Sizing 1 Open the Utilities property view by pressing CTRL U The Available Utilities view appears 2 Scroll down the list of available utilities until the Tray Sizing utility is visible Figure 2 152 Available Utilities a loj x Critical Properties Data Recon Utility Depressuring Dynamics Depressuring Original Derivative Utility Envelope Utility Hydrate Formation Utility Parametric Utility Pipe Sizing
66. Basis tab appears below Kinetic Reaction Rxn 1 Basis Molar Conen _ 12030 ide Combined iquid 453 7 F Max Temperature Basis Units Ibmoleft3 Ibmole ft3 hr v Rate Units Delete Name Rant No Ready eee z Stoichiometry Basis The Min Temperature Max Temperature Basis Units and Rate Units are acceptable at their default values 15 Click the Parameters tab On this tab you provide the Arrhenius parameters for the kinetic reaction In this case there is no Reverse Reaction occurring so you only need to supply the Forward Reaction parameters 16 In the Forward Reaction A cell enter 1 7e13 17 In the Forward Reaction E cell activation energy enter 3 24e4 Btu Ibmole The status indicator at the bottom of the Kinetic Reaction property view changes from Not Ready to Ready indicating that the reaction is completely defined The final Parameters tab appears below 5 x Ni Kinetic Reaction Rxn 1 Forward Reaction Equation Help _1 7000e 013 r k f Basis kf Basis 32400 k A exp E RT TB lt empty gt k A exp E RT TR Reverse Reaction lt empty gt Ei lt empty gt B lt empty gt T in Kelvin Stoichiometry Basis Parameters Delete Name Rxn t Ready o 3 21 3 22 Steady State Simulation A Basis Icon The same reaction s can be in multiple React
67. Column Vapour Flow specification from the list of available specifications Complete the Vap Prod Flow specification as shown below Figure R1 13 Nome Vap Prod Fow Condenser Molar 0 000000 Ibmole hr ca Parameters Delete The final specification table will appear as shown below Figure R1 14 Specifications Specified Value Current Value wt Enor Active Estimate Current ero_SS Prod Flow 9 30e 003 iesel_SS Prod Flow 1 925e 004 barrel day 1 92e 004 GO_SS Prod Flow 4500 barrel day 4 50e 003 4 1_Rate Pa 5 000e 004 barrel day 5 00e 004 1_Duty Pa _ 5 500e 007 Btu hr 5 50e 007 2 Rate Pa 3 000e 004 barrel day 3 00e 004 2 Duty Pa 3 500e 007 Btu hr 3 50e 007 _ 3 Rate Pa 3 000e 004 barrel day 3 00e 004 43 Duty Pa 3 500e 007 Btuhr 3 50e 007 eflux Ratio es FE 0 686 aptha Prod Rate 2 300e 004 barrel day 2 30e 004 iquid Flow 3500 barrel day 3 50e 003 ero Reb Duty 7 500e 006 Btu hr 7 50e 006 apour Flow 0 0000 Ibmole hr 3 87e 005 5 View Add Spec Group ctive Update Inactive Degrees of Freedom 0 P r 10 50 5077 00 0 lt 1 WIT IIIa WIVIIIIII Id 9 Once you have provided all of the specifications click the Run button R1 17 HI 4 Results Workbook Case Main The material stream results for the Workbook Case Main appear below Figure R1 15 Workbook Case Main x R1 18 Name Vapou
68. DELETE key 23 Click in the Reboiler pressure cell and press the DELETE key 24 Click in the Pressure cell for the top stage 1_Main TS and input a value of 202 6 psia 25 Specify the bottom stage pressure 10_Main TS as 203 3 psia 26 Click the Run button at the bottom of the column property view to start the Column Solver 27 Return to the Parent Main Simulation environment 28 Save the case as DynTUT1 2 hsc 1 112 Gas Processing Tutorial 1113 Processing Tutorial 1 113 1 3 3 Using the Dynamics Assistant Before you can run the simulation case in Dynamic mode the degrees of freedom for the flowsheet must be reduced to zero by setting the pressure flow specifications It is also necessary to size the existing valves vessels coolers and heat exchangers in the Main Flowsheet and the Column Sub flowsheet The following sizing parameters must be specified for these unit operations Unit Operation Sizing Parameter Valves Cv value Coolers Heat Exchangers The Dynamics Assistant makes recommendations as to how the flowsheet topology should change and what pressure flow specifications are required in order to run a case in Dynamic mode In addition it automatically sets the sizing parameters of the equipment in the simulation flowsheet Not all the suggestions that the Dynamics Assistant offers need to be followed The Dynamics Assistant will be used to do the following e Add Pressure Flow specification
69. Environment The text on the right side of the view indicates that before entering the Oil Environment two criteria must be met e atleast one fluid package must be present In this case only one fluid package Basis 1 is selected e the property package must be able to handle Hypothetical Components In our case the property package is Peng Robinson which is capable of handling Hypothetical components Oil Environment icon The Oil Characterization view allows you to create modify and otherwise manipulate the Assays and Blends in your simulation case For this example the oil is characterized using a single Assay Refining Tutorial Since both criteria are satisfied the oil is characterized in the Oil Environment 2 To enter the Oil Characterization environment do one of the following e click the Enter Oil Environment button on the Oil Manager tab e click the Oil Environment icon on the toolbar The Oil Characterization view appears Figure 2 17 i Oil Characterization Available Assays Assay Information hy atti Oil Input Preferences Assay Cut Blend User Property Correlation Install Oil Clear All Calculate All Oil Output Settings Return to Basis Environment In general three steps must be completed when you are characterizing a petroleum fluid 1 Supply data to define the Assay 2 Cut the Assay into hypothetical components by creating a Blend
70. Feed and Product streams e Size the Valve Vessel and Heat Exchange operations 3 78 Chemicals Tutorial Tutorial 3 79 For this tutorial the Session Preferences will be set so that the Dynamics Assistant will not manipulate the dynamic specifications 1 Open the Tools menu and select Preferences The Session Preferences view appears 2 Click the Simulation tab then select the Dynamics page Ensure that the Set dynamic stream specifications in the background checkbox is cleared Figure 3 106 Assistant J Perform checks when switching to dynamics or starting the integrator 4 Close the Session Preference view then close all open views on the HYSYS desktop except for the PFD view l Next you will initiate the Dynamics Assistant to evaluate the wo specifications required to run in dynamic simulation Dynamic Assistant icon 5 Click the Dynamics Assistant icon Browse through each tab in the Dynamic Assistant view to inspect the recommendations Uk All recommendations in the Dynamic Assistant will be implemented by I default unless you deactivate them You can choose which An Active recommendation recommendations will be executed by the Dynamic Assistant by ull De miplementeg by ie activating or deactivating the OK checkboxes beside each Dynamic Assistant OK Ci An Inactive recommendation will not be implemented by the Dynamic Assistant recommendation 3 79
71. Flow 4 sig fig Liquid Volume Flow 4 sigfig _Eormat Heat Flow 4 sig fig Order The four existing tabs are listed in the Workbook Tabs area When you add a new tab it will be inserted before the highlighted tab currently Material Streams You will insert the new tab between the Materials Streams tab and the Compositions tab 2 Inthe Workbook Tabs list select Compositions then click the Add button The New Object Type view appears 3 43 344 Steady State Simulation Steady State Simulation 3 Click the beside Stream to expand the tree Figure 3 54 Stream Material Stream Z Energy Stream Cancel Unit Operations Vessels Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling Operations Reactors Prebuilt Columns l Short Cut Columns l Sub Flowsheets Logical Operations Electrolyte Equipment R afinar n Mor ahane H A A Ae A of 4 Select Material Stream then click the OK button You return to the Setup view and the new tab Material Streams 1 appears after the existing Material Streams tab 5 Inthe Object group click in the Name field and change the name for the new tab to PT Flow to better describe the tab contents Tab Contents Object Name P T Flow Order Type Material Stream New Type Variables Format 1 4 fixed Use Set Temperature 4 sig fig Ad
72. Hidden Objects 0 Add Object Icon Lage Main x lt x Material Stream Icon weg These parameters are in default units so there is no need to change the units Chemicals Tutorial 3 33 Adding Another Stream Next you will use an alternative method for adding a stream 18 To add the second feed stream do any one of the following e Press F11 e From the Flowsheet menu select Add Stream e Double click the Material Stream icon on the Object Palette e Click the Material Stream icon on the Object Palette then click the Palette s Add Object button A new stream appears in the Workbook and is named according to the Auto Naming setting in your Session Preferences settings The default setting names new material streams with numbers starting at 1 and energy streams starting at Q 100 When you create the new stream the stream s property view also appears displaying the Conditions page of the Worksheet tab 19 In the Stream Name cell change the name to Water Feed 20 In the Temperature cell enter 75 E 21 In the Pressure cell enter 16 17 psia Figure 3 39 Water Feed Worksheet Stream Name Water Feed i Vapour Phase Fraction lt empty gt Conditions Temperature F 75 000 Properties Pressure psia T 16 170 empty gt Mass Flow lb hr lt empty gt K Value Std Ideal Lig Vol Flow USGPM lt empty gt User Variables Molar Enthalpy Btu Ibmole _ lt empty gt Mol
73. I Process Description Figure R1 1 PreFlash PreFlash vap Residue Crude Heater PreFlash Hot Crude Kerosene Iq Crude Duty Diesel Naphtha After passing through a preheat train 100 000 barrel day of 29 32 API crude is fed into a pre flash separator operating at 450 F and 75 psia The vapour from this separator bypasses the crude furnace and is re mixed with the hot 650 F pre flash liquids leaving the furnace The combined stream is then fed to the atmospheric crude column RA Process Description Process Description The column operates with a total condenser three coupled side strippers and three pump around circuits Figure R1 2 PA_1_Coner PA_1 0 PA_1 RE Im Kero_SS_Boaliup Kero_SS_ToReb Main TS Diesel_SS_Reim A naphtha product is produced overhead a kerosene product is produced from the first side stripper a diesel product is produced from the second side stripper and an atmospheric gas oil AGO is produced from the third side stripper Both the AGO side stripper and the diesel side stripper are steam stripped while the kerosene side stripper has a reboiler Atmospheric Crude Tower The following Assay data is used to characterize the oil for this example Assay Liq Volume Boiling Temperature F Light Ends Liq Volume Bulk Properties Standard Density 29 32 API There are two basic steps in this process simulation
74. Identification Family Class Hydrocarbon Chem Formula C4H10 ID Number 5 Group Name i CAS Number UNIFAC Structure ICH 3 2 CH2 2 User ID Tags Tag Number_ 1 lt empty gt Not Spec d 7 ID Point TDep UserProp Delete Edit Properties Edit Vise Curve See Chapter 3 Hypotheticals in the Simulation Basis manual for more information about cloning library components If the Simulation Basis Manager is not visible select the Home View icon from the toolbar a ew Enter Simulation Environment icon Gas Processing Tutorial 1 17 The Component property view only allows you to view the pure component information You cannot modify any parameters for a library component however HYSYS allows you to clone a library component as a Hypothetical component which you can then modify as required Close both of the component views and the Component List View to return to the Fluid Package If your project required it you could continue to add information such as interaction parameters and reactions to the Fluid Package For the purposes of this tutorial however the Fluid Package is now completely defined Close the Fluid Package view to return to the Simulation Basis Manager Figure 1 18 Simulation Basis Manager Curent Fluid Packages gt Flowsheet Fluid Pkg Associations Basis 1 NC PP Peng Robinson Vie FlowSheet Fluid Pka To Use
75. Impor _ DEA TO CONT Comp Molar Flow DEAmir Y gt Delete Import Connections Parameters Formulas Spreadsheet Calculation Order f Delete Function Help Spreadsheet Only Ignored G1 15 Calculating Lean amp Rich Loadings The following formulas will produce the desired calculations Figure G1 6 i SPRDSHT 1 Formula Summary 0 1817 0 4395 5 279e 004 8 926e 003 gt 7 5 Connections Parameters Formulas Spreadsheet Calculation Order Delete Function Help Spreadsheet Only I Ignored Figure G1 7 i SPRDSHT 1 Current Cell Imported From DEA TO CONT B4 Comp Molar Flow DEAmine ae aac Rich DEA 258 7085 Ibmole hi Rich H25 Loading 0 1817 Rich H25 46 9977 Ibmole hr Rich CO2 Loading 0 4395 Rich CO2 113 6896 Ibmole h Lean DEA Lean H25 Loading 5 279e 004 Lean H25 0 1366 Ibmole hr Lean CO2 Loading 8 926e 003 Lean C02 2 3033 Ibmole hr C02 Vol Frac 0 0006 H25 ppm 0 0790 0 0000 ii Connections Parameters Formulas Spreadsheet Calculation Order Delete Function Help Spreadsheet Only Ignored The acid gas loadings can be compared to values recommended by D B Robinson as shown below Maximum Acid Gas Loadings moles acid gas mole of amine se MEA DGA fos fos oa fos foo G1 16 Acid Gas Sweetening with DEA G17 Gas Sweetening with DEA G1 17 1 6 Dunamic Simulati
76. Lig Vol Flow 4sigfig _ Format HeaFlow 4 sig fig Molar Enthalpy 4 sig fig Order The next task is to customize the tab by removing the variables that are not required 7 Inthe Variables group click on the first variable Vapour Fraction 8 Press and hold the crrt key 2 54 Refining Tutorial 2 55 9 Click on the other variables Molar Flow Mass Flow Heat Flow and Molar Enthalpy These four variables are now highlighted 10 Release the crrt key If you want to remove 11 Click the Delete button to remove them from this Workbook tab variables from another tab only The finished Setup view appears below you must edit each tab individually Figure 2 61 The new tab Workbook Tabs now appears in Tab Contents Material Streams Add Object the list of P T Flow wae Compositions ame P 1 Flow Order Workbook Tabs Eran Streams Delete in the same Unit Ops Type Material Stream New Type order as it Variables appears in the Use Set _ Workbook Temperature 4 sig fig Presswe 4 sig fig Add Std Ideal Lig Yol Flow 4sigfig The new tab displays only these three Variables 12 Click the Close icon to return to the Workbook view and see the new tab Figure 2 62 Temperature F Pressure psia Std Ideal Lig Yol Flow barrel da Name AGO Steam PreFlashVap __PreFlashLig Temperature F 300 0 450 0 450 0 Pre
77. MixerOut Delete Unit0p C Include Sub Flowsheets View Unit0p Add Unit0p Material Streams Compositions Energy Streams Unit Ops MixerOut The table shows the operation Name its Object Type the attached streams Feeds and Products whether it is Ignored and its Calculation Level When you click the View UnitOps button the property view for the currently selected operation appears Alternatively double clicking on any cell except Inlet Outlet and Ignored associated with the operation also opens the Mixer property view 1 38 Gas Processing Tutorial 1 39 You can also open the property view for a stream directly from the Unit Ops tab When any of the Name Object Type Ignored or Calc Level cells are active the box at the bottom of the Workbook displays all streams attached to the current operation Currently the Name cell for MIX 100 has focus and the box displays the three streams attached to this operation To open the property view for one of the streams attached to the Mixer do one of the following e Double click on Feed 1 in the box at the bottom of the Workbook e Double click on the Inlet cell for MIX 100 The property view for the first listed feed stream in this case Feed 1 appears Installing the Inlet Separator Next you will install and define the inlet separator which splits the two phase MixerOut stream into its vapour and liquid phases In the Workboo
78. Number of Hidden Objects 0 The operations to which SepVap is attached are displayed in this box You can access the property view by double clicking on the corresponding operation name 1 45 Steady State Simulation Adding a Tab to the Workbook When the Workbook has focus the Workbook item appears in the HYSYS menu bar This allows you to customize the Workbook to display specific information In this section you will create a new Workbook tab that displays only stream pressure temperature and flow 1 Doone of the following e From the Workbook menu select Setup e Object inspect right click the Material Streams tab in the Workbook then select Setup from the menu that appears The Workbook Setup view appears Figure 1 56 Workbook Tabs rTab Contents Material Streams Add Object Compositions TORNET aie Name M aterial Streams Order Unit Ops Delete Type Material Stream New Type Variables Format Use Set 1 4 fixed Temperature 4 sig fig Add Pressure 4 sig fig Molar Flow 4 sig fig Delete Mass Flow 4 sig fig Liquid Volume Flow 4 sig fig __ Format Heat Flow 4 sig fig _ Order Currently all variables are displayed with four significant figures You can change the display format or precision of any Workbook variables by clicking the Format button The four existing tabs are listed in the Workbook Pages group When you add
79. Object Case Main Coolant Mixer Out Prop Oxid Prop Oxide 1 a Object Filter Reactor Prods iqui All Reactor Prods 1 Pichaane Reactor Vent C Uni Water Feed Unit ps Navigator Scope _ Water Feed 1 Phase Temperature Logicals Flowsheet Heyah C ColumnOps A zani i Second Liquid Hole C Custom asis VLV Reactor Prods 55 Liquid Volume Custom Utility VLV Water Feed Tank Volume Custom FeederBlock_Prop Oxide Total Moles FeederBlock_ Water Fee User Variables PradiictBlael Raseter Varner Flaw CB Variable Description Liquid Percent Level Cancel 8 Inthe Output Target Object group click the Select OP button The Select OP Object view appears 9 Inthe Object list select VLV Reactor Prods then click the OK button Figure 3 116 Select OP Object For Reactor LC Ea Flowsheet Object Case Main i OK Reactor Prods Object Filter Reactor Yent G Al C Streams C UnitOps LV Water Feed C Logicals C ColumnOps C Custom Custom Nrecnmmert WISCONNHEGI Cancel 10 Click the Parameters tab then select the Configuration page 3 87 3 88 Reactor LC x Exec Int l Bt L PID Controller icon 3 88 Dynamic Simulation 11 On this page enter the following information In this cell Enter Aeron brect 12 Click the Face Plate button at the bottom of the property view The Reactor LC face plate view appears 13 From the d
80. Press F3 e From the Flowsheet menu select Find Object e Double click on any blank space on the HYSYS Desktop e Click the Object Navigator icon The Object Navigator view appears Figure 2 121 Object Navigator OF E4 Flowsheets Unit Operations Filter Atmos Tower C All C Streams UnitOps C Logicals C Custom Setup Custom Cancel The UnitOps radio button in the Filter group is currently selected so only the Unit Operations appear in the list of objects To open a property view select the operation in the list and click the View button or double click on the operation You can change which objects appear by selecting a different Filter radio button For example to list all streams and unit operations select the All radio button You can also search for an object by clicking the Find button When the Find Object view appears enter the Object Name and click the OK button HYSYS opens the property view for the object whose name you entered Refining Tutorial 2 2 10 Installing a Boiling Point Curves Utility Previously the boiling point profiles for the product streams was viewed using the Plots page in the column property view You can also view boiling point curves for a product stream using HYSYS BP Curves Utility To create a Boiling Point curves utility for the Kerosene product 1 Open the Navigator using one of the methods described above 2 Select the Streams radio button 3 Scr
81. Pressure 4 sig fig Mass Flow 4 sig fig button Liquid Volume Flow 4 sig fig _ Format Heat Flow 4 sig fig Dn Order The four existing tabs are listed in the Workbook Tabs area When you add a new tab it is inserted before the selected tab currently Material Streams You will insert the new tab before the Compositions tab 2 Inthe Workbook Tabs group list select Compositions 2 53 2 54 Steady State Simulation 3 Click the Add button The New Object Type view appears Figure 2 59 Stream Unit Operations H Vessels Cancel Heat Transfer Equipment H Rotating Equipment Piping Equipment Solids Handling Operations H Reactors Prebuilt Columns H Short Cut Columns H Sub Flowsheets Logical Operations Electrolyte Equipment Refinery Operations Extension Unit Operation 1 LD bilitt Nhisrnte wi 4 Click the beside Stream select Material Stream from the branch then click the OK button You return to the Setup view and the new tab appears after the existing Material Streams tab In the Tab Contents Object group click in the Name field Change the name of the new tab to PT Flow to better describe the tab contents Figure 2 60 Tab Contents Object Name P T Flow Order Type Material Stream New Type Variables Format Use Set Temperature ig fi Add Pressure Molar Flow ig fi Delete Mass Flow ig fi Std Ideal
82. Propanol 0 0001 0 0002 0 0002 0 0000 0 0003 Comp Mole Frac 1 Butanol 0 0003 0 0000 0 0000 0 0001 0 0000 Comp Mole Frac 3 M 1 C4ol 0 0002 M A A m a Material Steams Compositions Energy Streams Unit Ops FaadDloci wash Hot J Include Sub Flowsheets CO2Wash J Show Name Only Number of Hidden Objects C1 14 Ethanol Plant MB Plant C1 15 Energy Streams Tab Figure C1 8 Workbook Case Main 4 Name S SCout RectRebO Rect CondQ Heat Flow kJh 3 584e 005 2 764e 007 4 043e 007 Name Heat Flow kJ h 4 Material Streams Compositions Energy Streams Unit Ops Lights C Include Sub Flowsheets as L Show Name Only Number of Hidden Objects 0 C1 15 C1 16 Synthesis Gas Production Ce Sunthesis Gas Production C2 1 C2 2 C2 3 C2 4 Process Descrip ina sais iecdaa aa a aa 3 SEUD iaa aeaa a eaa e aa aa E ous 4 C2 2 1 Components amp Fluid Package ccccccseeeeeeeeeeeeeeeeeeeees 4 C2 2 2 Defining the Reactions cccccccccecsseeseeeceeeeeeeeeeeeeeeeaaeeeees 5 Steady State Simulation 2 22050 WUD eeeeeseeeceneeeceeeseseeneeecenes 9 C2 3 1 Building the FlowsSheet ccccceccsesseeeseseeeeeeeseeeesaeeees 10 C2 3 2 Installing Adjust Operations ccccccccsseeeeeeeeeeeeeeeeenees 14 R
83. Propylene Propane Splitter P1 7 Installing the Reboiler The Reboiler for the Absorber must be installed with the Stripper Column 1 Double click the Reboiler icon on the Object Palette The Reboiler appears in the PFD and the Reboiler property view appears 2 Enter the following information Reboiler Reboiler Tab Page inthis cell Een einai P1 3 3 Adding the Rectifier Refluxed Absorber Next you will install the Rectifier This column has 89 ideal stages and a Total Condenser Installing the Tray Section Install a new Tray Section for the Absorber 1 Double click the Tray Section icon on the Object Palette The tray section appears in the PFD and the Tray Section property view appears 2 Supply the parameters as shown below Tray Section Rectifier Tab Page inthis cels Enter Design Parameters Number oftrays e Steady State Simulation Tray Section Rectifier Design Pressures 280 psia Tray 89 290 psia 3 Close the Tray Section view Installing the Total Condenser A Total Condenser is required for the column 1 Double click the Total Condenser icon in the Object Palette The a condenser icon appears in the PFD and the condenser property view appears Total e icon 2 Supply the following information Total Condenser Condenser Tab Page inthis cell Emere cae Reflux Reflux P1 3 4 Adding the specifications Two specifications are
84. Save Simulation Case As view appears By default the File Path is the cases sub directory in your HYSYS directory 3 Inthe File Name field type a name for the case for example REFINING You do not have to enter the hsc extension HYSYS adds it automatically 4 Once you have entered a file name press the ENTER key or click the OK button When you click the Save button HYSYS saves the case under the name you gave it The Save As view does not appear again unless you choose to give it anew name using the Save As command g c o USing the Workbook Click the Workbook icon on the toolbar to ensure the Workbook view is active Specifying the Feed Conditions In general the first task in the Simulation environment is to install one or more feed streams however the stream Preheat Crude was already installed during the oil characterization procedure At this point your current location should be the Compositions tab of the Workbook view 2 39 240 Steady State Simulation Steady State Simulation When you press ENTER after entering a stream property you are advanced down one cell in the Workbook only if the cell below is lt empty gt Otherwise the active cell remains in its current location Alternately you can specify the unit simply by selecting the unit in the drop down list 2 40 1 Click the Material Streams tab The preheated crude enters the pre fractionation train at 450 F and 75 psia 2 Inthe
85. Specification Specs Active Stripchart Flow Specification Molar C Mass C IdealLig ol Std LigVol Molar Flow a 2183 kgmole h Worksheet Attachments Dynamics era S Delete Define from Other Stream 13 Close the PA_1_Draw property view 14 Activate the following flow specifications for the following streams in the Column sub flowsheet Material Stream Pressure Flow Specification VEUT PA_2_Draw Molar Flow PA_3_Draw Molar Flow Molar Flow Kero_SS_Draw Molar Flow Diesel_SS_Draw Molar Flow AGO_SS_Draw Molar Flow 124 8 kgmole h 15 Save the case as DynTUT2 5 hsc 16 Close all the views except the face plates 830 2 kgmole h 648 0 kgmole h 879 7 kgmole h 426 6 kgmole h 616 8 kgmole h 17 To arrange the face plates select the Arrange Desktop command from the Windows menu 18 The integrator can be run at this point Click the Start Integrator icon When you are given the option to run dynamic assistant select No Refining Tutorial When the integrator initially runs HYSYS detects that no vapour phase exists in the Condenser at the specified process conditions It displays the following message Figure 2 174 Ni Condenser Liquid Level Initialisation This vessel has no vapour phase at the specified process conditions HYSYS can initialise this vessel with a vapour phase either by increasing the total vessel or by creating a non equilibri
86. Specs Steady State Specs Vapour Fraction Cancel Temperature _ Como Yolume Frac hd Description Temperature Gas Processing Tutorial 1 95 Processing Tutorial 1 95 14 From the Variable list select Temperature 15 Click the OK button oF gt 16 Click the Attach Mode icon to leave Attach mode aay ai 17 Double click the ADJ 1 icon to open its property view The connections made in the PFD have been transferred to the appropriate cells in the property view Adjusting the Target Variable The next task is to provide a value for the target variable in this case the dew point temperature A 5 F safety margin will be used on the pipeline specification of 15 F so the desired dew point is 10 E 1 In the Specified Target Value field enter 10 F Figure 1 123 Connections Adjust Name ADJ 1 Connections Adjusted Variable Notes Object ColdGas Select Var Variable Temperature Target Yariable Object SalesDP Select Var Variable Temperature Target Value J Source User Supplied Specified Target Value C Another Object OOF C SpreadSheetCell Object Connections Parameters Monitor User Variables Unknown Main Delete M Ignored 2 Click the Parameters tab 3 In the Tolerance cell enter 0 1 E 1 96 Steady State Simulation 4 Inthe Step Size cell enter 5 E No values will be entered in the Minimum and Maximum field as these are option
87. Steam the stream will not be Notes Critical Values affected i Critical Pressure 1477 psia Likewise if you delete the stream the Utility will Maxima remain but will not display any information until you Leita iA attach another stream using the Select Stream button Design Performance Dynamics Delete Ignored 7 Close this Utility view since it is no longer required For more information about defining utilities refer to Section 7 27 Utilities in the User Guide 8 Close the Feed 2 view 1 33 Steady State Simulation 1 2 6 Installing Unit Operations In the last section you defined the feed streams Now you will install the necessary unit operations for processing the gas Installing the Mixer The first operation that you will install is a Mixer used to combine the two feed streams As with most commands in HYSYS installing an operation can be accomplished in a number of ways One method is through the Unit Ops tab of the Workbook 1 Click the Workbook icon to ensure the Workbook window is active 2 Click the Unit Ops tab of the Workbook Workbook icon Figure 1 39 Workbook Case Main p Name Obiect Type Inlet view Unitiip Add UnitOp Delete Write i Material Streams Compositions Energy Streams Unit Ops PO C Include Sub Flowsheets Gas Processing Tutorial 85 Processing Tutorial 1 35 3 Click the Add UnitOp b
88. Steam Stripped Draw Stage Boil Up Ratio Flow Basis f 75 Molar C Mass C Volume Std Volume Delete Insta Product Stream Information Product Stream lt empty gt Draw Spec _ lt empty gt In the Name field change the name to KeroSS In the Return Stage drop down list select stage 8 8_Main TS In the Draw Stage drop down list select stage 9 9_Main TS In the Flow Basis group select the Volume radio button a Se oR In the Product Stream field enter Kerosene The straight run product distribution data calculated during the Oil Characterization appears in the figure below Figure 2 90 Cut Distributions e TETE 4 Ma Kerosene Liquid Volume Fraction Naphtha Kerosene Light Diesel Heavy Diesel Atm Gas Dil Residue The Kerosene liquid volume fraction is 0 129 For 100 000 bbl day of crude fed to the tower Kerosene production can be expected at 100 000 0 129 12 900 or approximately 13 000 bbl day Close icon Refining Tutorial 9 Inthe Draw Spec field enter 13000 The completed Side Stripper view appears below Figure 2 91 Ni Side Stripper KeroSS E Name KeroSs Return Stage 8 Main TS Configuration Draw Stage Reboiled 9 Main TS Steam Stripped Flow Basis Boil Up Ratio C Molar 0 75 C Mass Volume C Std Volume Product Stream Information j Product Stream Kerosene Delete Install Draw Spec
89. The heavier liquid component of the gas stream is processed in a depropanizer column yielding a liquid product with a specified propane content Figure 1 127 gt Ovhd DePropanizer gt CondDuty LTS ap nowy RebDuty a gt LiquidProd CoolGas ColdGas Chiller TowerFeed gt SalesGas Uptiq Tower FC LTS Valve lt o q LTSExit l on Towerlnlet Tower M ii SepLig Sep id MIx 101 Valve ii valve The Dynamics Assistant will be used to make pressure flow specifications and size pieces of equipment in the simulation flowsheet It is also possible to set your own pressure flow specifications and size the equipment without the aid of the Dynamics Assistant This tutorial will comprehensively guide you through the steps required to add dynamic functionality to a steady state gas plant simulation To help you navigate these detailed procedures the following milestones have been established for this tutorial 1 Modify the steady state model so that a pressure flow relation exists between each unit operation 2 Implement a tray sizing utility for sizing the Depropanizer column Gas Processing Tutorial 1 890 Processing Tutorial 1 99 3 Use the Dynamics Assistant to set pressure flow specifications and size the equipment in the simulation case In this Tutorial you will follow 4 Install and define the appropriate controllers this basic procedure in building the dynamic model gi Set up
90. Tower COL iect dictates the Variable aoe Product Stream Coi Object Filter list and the selected Product Steam Cor ra Variable determines whether Product Stream Coi C Streams any Variable Specifics are UnitOps Navigator Scope i C Logicals vailable available Op eee Spec Calc Value C ColumnOps Spec Error C Case Spec Is Active C Custom C Basis Custom C Utility Stage Liq Comp Lic Sec RARE Fia Variable Description Reflux Ratio Cancel HYSYS duplicates this variable name in the Variable Description field If you want you can edit the default description To edit the default description 5 Click inside the Variable Description field and delete the default name 6 Type a new description such as Reflux Ratio and click the OK button The variable now appears in the Databook Figure 2 133 DataBook Available Data Entries Object Variable Atmos Tower Reflux Ratio E Variables Process Data Tables Strip Charts Data Recorder Case Studies 7 To add the next variable click the Insert button and the Variable Navigator again appears 8 Select the Streams radio button in the Object Filter group The Object list is filtered to show streams only 2 105 Steady State Simulation 9 Scroll down and click on Trim Duty in the Object list and the Variable list available for energy streams appears to the right of the Object list 10 Select Heat Flow in the Variab
91. View Process Data T able Procb atal Reflux Ratio i TimDuy Trim Duty F Residue BP Curv ASTM 1160 Vac 5 Residu L Setup Add All Variables Invert All Variables Remove All Variables Variables Process Data Tables Strip Charts Data Recorder Case Studies 3 Change the default name from ProcDatal to Key Variables by editing the Process Data Table field Notice that the three variables added to the Databook appear in the matrix on this tab 4 Activate each variable by clicking on the corresponding Show checkbox Figure 2 138 Individual Process Data Selection Process Data Table Key Variables Atmos Tower Reflux Ratio Trim Duty Trim Duty Iv _ Residue BP Curv ASTM 1160 Vac 5 Residu Vv Add All Variables Invert All Variables Remove All Variables 2 108 Refining Tutorial HO Tutorial 2 109 5 Click the View button to view the new data table which is shown below Figure 2 139 Key Variables Data Object Variable Value Units Reflux Ratio 0 7720 Trim Duty Trim Duty 3 179e 007 Btu hr Residue BP Cur ASTM 1160 Vac 5 Resi 389 6 F ne of View DataBook This table is accessed later to demonstrate how its results are updated whenever a flowsheet change is made 6 For now click the Minimize icon in the upper right corner of the Key Variables Data view HYSYS reduces the v
92. View button The Component List View appears Figure 3 11 Component List View fel x Add Component Selected Components Components Available in the Component Library Components Match View Filters Traditional Electrolyte C Sim Name C Formula Hypothetical Other lt Add Pure Methane Ethane Propane i Butane n Butane i Pentane n Pentane n Hexane n Heptane Sort List nOctane n Nonane n Decane l n C11 n C12 lt Substitute gt J Show Synonyms Cluster B Selected Component by Type Delete Component List 1 Each component can appear in three forms corresponding to the three radio buttons that appear above the component list Feature Description SimName The name appearing within the simulation FullName Synonym IUPAC name or similar and synonyms for many components The chemical formula of the component This is useful when you are unsure of the library name of a component but know its formula 3 10 Chemicals Tutorial 3 11 Based on the selected radio button HYSYS locates the component s that best matches the information you type in the Match field In this tutorial you will use propylene oxide propylene glycol and H20 First you will add propylene oxide to the component list 2 Ensure the SimName radio button is selected and the Show Synonyms checkbox is checked 3 Inthe Match field start typing propyleneoxide as one word HYSYS filters the list as
93. a new tab it will be inserted before the highlighted tab currently Material Streams 2 Inthe Workbook Tabs group list select the Compositions tab Gas Processing Tutorial 1 47 3 Click the Add button The New Object Type view appears Figure 1 57 Ni New Object Type Stream Unit Operations _ Vessels Cancel Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling Operations Reactors Prebuilt Columns Short Cut Columns Sub Flowsheets Logical Operations Electrolyte Equipment Refinery Operations Extension Unit Operation Utility Objects Dynamic Equipment Op Control Type Fe 0 0 E E 4 Click the beside Stream to expand it into Material Stream and Energy Streams 5 Select the Material Stream and click the OK button You will return to the Setup view and the new tab appears in the list after the existing Material Streams tab Figure 1 58 workbook Tabs Tab Contents Material Streams Object n _ Material Streams 1 i Name M aterial Streams 1 Order Compositions Delete Energy Streams Unit Ops Type Material Stream New Type re Variables Format Use Set ___ Vapour Fraction _1 4 fixed Temperature 4 sig fig Add Pressure 4 sig fig Molar Flow 4 sig fig Delete a EE Flow 4 sig fig Std Ideal Lig Vol Flow 4 sig fig Format Heat Flow 4 s
94. any zero components then click the OK button 2 43 Steady State Simulation This stream is pure water therefore there is no need to enter fractions for any other components 4 Click the Normalize button and all other component fractions are forced to zero 5 Click the OK button HYSYS accepts the composition and you are returned to the Workbook view The stream is now completely defined so HYSYS flashes it at the conditions given to determine the remaining properties 6 Repeat steps 2 to 5 for the other utility stream Diesel Steam If you want to delete a 7 Click the Material Streams tab The calculated properties of the two stream move to the Name utility streams appear here cell for the stream then press DELETE HYSYS ask for confirmation of your action Figure 2 46 Name Preheat Crude Bottom Steam Diesel Steam Yapour Fraction i Oe 1 0000 1 0000 Temperature F 450 0 375 0 300 0 Pressure psia 75 00 150 0 50 00 Molar Flow Ibmole hr 3814 416 3 166 5 Mass Flow lb hr 1 144e 006 7500 3000 Liquid Yolume Flow barrel day 1 000e 005 514 6 205 8 7 619e 008 4 222e 007 1 697e 007 Vapour Fraction S a 5 Material Streams Compositions Energy Steams Unit Ops ProductBlock_Preheat Crude LJ Include Sub Flowsheets FeederBlock_Preheat Crude L Show Name Only Number of Hidden Objects 0 Next you will learn alternative methods for creating a new stream
95. boundary stream however there are exceptions to the rule One extra pressure flow specification is required for the condenser attached to the column Regenerator This rule applies only if there are no pieces of equipment attached to the reflux stream downstream of the condenser Without other pieces of the equipment i e pumps coolers valves to define the pressure flow relation of these streams they must be specified with a flow specification 1 Inthe Main flowsheet add the following pressure flow specifications to the boundary streams Material Stream Pressure Specification Flow Specification Value PSOURGAS Inacive Molar Fow 25MMSCFD FWKO MAKEUP H20 2 Ensure the PF Relation checkbox for all the valves is checked Dynamics tab Specs page 3 Activate the Efficiency and Power checkboxes for pumps you may have to deactivate the Pressure Rise checkbox 4 Onthe E 100 property view click the Calculate K s button Dynamics tab Specs page 5 Also on the cooler E 101 property view set the pressure flow option instead of the pressure drop by selecting the Overall k Value checkbox and deactivating the pressure drop checkbox 6 Deactivate the Delta P checkbox and select the k checkbox for both the Shell and Tube side G1 21 Dynamic Simulation Equipment Sizing In preparation for dynamic operation both column tray sections and the surrounding equipment must be sized In steady state simulation
96. build the first part of the flowsheet from specifying the feed conditions through to installing the pre flash separator The PFD is then used to install the remaining operations from the crude furnace through to the column 2 2 2 Setting Your Session Preferences l nA Start HYSYS and create a new case The Simulation Basis Manager view appears md NoName hsc HYSYS File Edit Basis Tools Window Help Dee aT Simulation Basis Manager View Add Delete Copy Import Export Refresh Fluid Pkgs Environment Basis Mode Steady State Component Lists Master Component List Components Hypotheticals Oil Manager Reactions ComponentMaps UserProperty Your first task is to set your Session Preferences From the Tools menu select Preferences The Session Preferences view appears The most important preference you will set is the unit set HYSYS does not allow you to change any of the default unit sets listed however you can create a new unit set by cloning an existing one In this tutorial you will create a new unit set based on the HYSYS Field set and customized it 2 7 Steady State Simulation 3 Click the Variables tab then select the Units page 4 Inthe Available Unit Sets group select Field Figure 2 6 Session Preferences tut2 PRF Iof Xx Available Unit Sets EuroS Units Field Variables Formats
97. can continue with this example by proceeding to the Optional Study sections or you can begin building your own simulation case In the Optional Study you will use some of the other tools available in HYSYS to examine the process in more detail 1 2 10 Optional Study In the following sections the effects of the LTS temperature on the SalesGas dew point and heating value are determined Before proceeding re specify the temperature of ColdGas back to its original value of 0 F 1 Click the Workbook icon on the toolbar 2 Onthe Material Streams tab of the Workbook click in the Workbook icon Temperature cell for the ColdGas stream 3 Type 0 then press the ENTER key Steady State Simulation Using the Spreadsheet HYSYS has a Spreadsheet operation that allows you to import stream or operation variables perform calculations and export calculated results Accessing the spreadsheet 1 To install a Spreadsheet and display its property view double click Spreadsheet icon the Spreadsheet icon in the Object Palette Figure 1 115 Imported ariables i Add Import Exported Variables Variable Description Add Export a Connections Parameters Formulas Spreadsheet Calculation Order Delete Function Help Spreadsheet Only M ignored 2 On the Connections tab change the spreadsheet name to Heating Value The heating value of the sales gas is calculated by imp
98. checkbox is checked then close the view Refluxed Absorber icon The Input Expert is a Modal view indicated by the absence of the Maximize Minimize icons You cannot exit or move outside the Expert view until you supply the necessary information or click the Cancel button To install this column using the pre built crude column template 1 Double click on the Custom Column icon on the Object Palette 2 On the view that appears click the Read an Existing Column Template button The Available Column Templates view appears listing the template files col that are provided in your HYSYS template directory Both 3 and 4 side stripper crude column templates are provided 3 Select 3sscrude col and click the OK button The property view for the new column appears You can now customize the new column Refining Tutorial 2 67 3 Double click the Refluxed Absorber icon on the Object Palette The first page of the Input Expert appears Figure 2 77 Refluxed Absorber Column Input Expert Condenser Energy Stream x Condenser C Total xi Column Name T 00 Partial Ovhd Outlets Full Rflx Optional Inlet Streams gt Water Draw Inlet Stage lt lt Stream gt gt Optional Side Draws lt Stream gt gt Bottom Stage Inlet 1 ee Bottoms Liquid Outlet Stage Numbering Top Down C Bottom Up Pie Next Connections page 1 of 4 Cancel When you ins
99. click the Add button The Add Column Component Ratio i Specs view appears Column Component Recover Column Cut Point Orn Ea a h 4 Select Column Component Fraction as the Specification Type Column DT Heater Cooler Spec err ai 5 Click the Add Spec s button The Comp Frac Spec view appears Column Duty Column Duty Ratio Column Feed Ratio Column Gap Cut Point Column Liquid Flow Fig ure 3 78 Column Physical Properties Spec Column Pump Around n Column Reboil Ratio Spec N Comp Frac Spec Comp Fraction PEG Column Recovery Column Reflux Feed Ratio Spec Column Reflux Fraction Spec tage lt lt Stage gt gt Column Reflux Ratio low Basis Mole Fraction Column Tee Split Spec hase Liquid Column Temperature lt empty gt Column Transport Properties Spec ts Column User Property Spec Si iiaii te Companen 2 t Column Yapour Flow Column Yapour Fraction Spec Column Vapour Pressure Spec Column Cold Properties Spec Target Type Stream Stage Add Spec s i Parameters Spec Type Delete 6 Inthe Name cell change the name to H20 Fraction 7 Inthe Stage cell select Reboiler from the drop down list Figure 3 79 4s Comp Frac Spec H20 Fraction FES H20 Fraction Stage Components Target Type C Stream Stage T Parameters Spec Type Delete 3 60 Chemicals Tutorial 3 61 8 In the Spec Value cell enter 0 005 as the liquid mole fraction specification value 9 Inthe Com
100. defining streams unit operations and columns and using various aspects of the HYSYS interface to examine the results while you are creating the simulation If you are new to HYSYS it is recommended that you begin with one of these tutorials in order to familiarize yourself with the initial steps required to build a HYSYS simulation Often in HYSYS more than one method exists for performing a task or executing a command Many times you can use the keyboard the HYSYS Icon HYSYS Tutorials A 3 mouse or a combination of both to achieve the same result The steady state tutorials attempt to illustrate HYSYS flexibility by showing you as many of these alternative methods as possible You can then choose which approach is most appropriate for you The dynamics tutorials use the steady state solution as a basis for building the dynamic case If you like you can build the steady state case and then proceed with the dynamic solution or you can simply call up the steady state case from disk and begin the dynamic modeling atarting HYSY9 With Windows NT 4 0 or Windows 95 98 the installation process creates a shortcut to HYSYS 1 Click on the Start menu 2 Move from Programs to Hyprotech to HYSYS 3 Select HYSYS The HYSYS Desktop appears Figure A 1 Tool Bar Menu Bar Maximize icon File Tools Help D ow bed Status Bar Object Status Trace Window Performance Window Slider To learn more about the basics of the
101. example a new unit set will be made based on the HYSYS Field set which you will then customize To create a new unit set do the following 1 Inthe Session Preferences view click the Variables tab 2 Select the Units page if it is not already selected 1 7 Steady State Simulation THadelauitPreierenesfileis 3 Inthe Available Unit Sets group select Field to make it the active set named HYSYS prf When you modify any of the Figure 1 5 preferences you can save the changes ina new Session Preferences HYSYS PRF Preference file by clicking the Save Preference Set button HYSYS prompts you to provide a name for the new Fonna Preference file which you l ee pee can load into any simulation i case by clicking the Load Preference Set button Variables Units Available Unit Sets Display Units Unitless Temperature F Pressure psia Flow Ibmole hr Mass Flow lb hr Simulation Variables Reports Files Resources Extensions Oillnput Tray Sizing Save Preference Set Load Preference Set 4 Click the Clone button A new unit set named NewUser appears This unit set becomes the currently Available Unit Set 5 Inthe Unit Set Name field enter a name for the new unit set You can now change the units for any variable associated with this new unit set In the Display Units group the current default unit for Flow is lbmole hr A more appropriate unit f
102. feed and cold_liq2 as shown Stream Name cold_liq2 e tf E Pressure KPa e Molar Flow kgmole h 100 O 7 5 X1 2 3 Installing Unit Operations Enter the Simulation Environment and add the following unit operations to the flowsheet Add Separators Separator Name V 100 Tab Page Design Connections feed ee V 101 Tab Page Design Connections precooled Vapour Out Liquid Outlet cooled_liq Design Parameters V 102 Tab Pagel nimis cal Emere Design Connections Building Flowsheet 1 Add a Heat Exchanger Heat Exchanger Name E 100 Tab Page In this cell Enters Design Parameters Heat Exchanger Model Exchanger Design End Point Rating Sizing Counter Add an Expander Expander Name K 100 Tab Page Inthis oel Mn Add a Compressor Compressor Name K 101 Tab Page inthis cell Enters Design Parameters Efficiency Adia X1 6 Case Linking X1 7 Add a Recycle Operation Recycle RCY 1 Tab Pagel pints cl Design Connections cold_liq The case should converge immediately Save the case as LinkCasel hsc Building Flowsheet 2 X1 3 Building Flowsheet d X1 3 1 Setup Now you will create the target case for the linked case 1 Define the same property package as PRSV as Flowsheet 1 2 Select SI units in the Session Preferences 3 Select the following components C1 C2 C3 i C4 H20 X1 3 2 Installing Unit Opera
103. flash tank FLASH TK which is modeled using a Separator operation Separator FLASH TK Tab Page Design Connections DEA TO FLASH TK Vapour Outlet FLASH VAP Liquid Outlet RICH TO L R 01 3 2 Regenerating the DEA Add a Heat Exchanger The stream RICH TO L R is heated to 200 F REGEN FEED in the lean rich exchanger E 100 prior to entering the regenerator which is represented by a distillation column Heat is supplied to release the acid gas components from the amine solution thereby permitting the DEA to be recycled back to the contactor for reuse Steady State Simulation The heat exchanger is defined below Heat Exchanger E 100 Tab Page In this cell Etern Design Connections RICH TO L R Semenn eee Add a Distillation Column 1 Add a distillation column configured as shown in the following table The amine regenerator is modeled as a distillation column with 20 real stages 18 stages in the Tray Section plus a Reboiler and Condenser Distillation Column Regenerator Page Oeo E REGEN FEED Reboiler Energy Stream RBLR Q Condenser Energy Stream COND Q Pressure Profile 27 5 psia Cond Pressure Drop Reboiler Pres 31 5 psia G1 10 Acid Gas Sweetening with DEA GIT Gas Sweetening with DEA G1 11 For this tower the component efficiencies will be fixed at 0 80 for H2S and 0 15 for CO2 The efficiencies of the condenser and reboiler must remain at 1 0 so enter the effici
104. ft3 displayed on the Parameters page of the Design tab Figure 3 67 Reactor Set 1 Model Details EN Initialize From Products Vessel Volume t3 290 0 p C Dry Startup Vessel Diameter ft B Holdup C Initialize From User Height ft StripChart Lig Volume Percent Init A oldwp Duty Level Calculator I LagRxn Temperature Fraction Calculator Use levels and nozzles Dynamics J Enable Explicit Reaction Calculations Dynamic Specifications Feed Delta P psi Vessel Pressure psia ane Design Reactions Rating Worksheet Dynamics Delete o romby o ooed 11 Click on the Worksheet tab Figure 3 68 Reactor Set 1 Worksheet Reactor Prods Reactor Vent Coolant ae 0 0000 1 0000 lt empty gt ene l lt empty gt lt emply gt lt empty gt Properties Pressure psial 17 er er cem Composition lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt PF Specs 42 84 lt empty gt lt empty gt lt empty gt 1 086e 005 lt empty gt lt empty gt lt empty gt 0 8824 cempe ___ lt emply gt lt empty gt 8 262e 007 lt empty gt lt empty gt lt empty gt Design Reactions Rating Worksheet n a re 3 53 3 54 Steady State Simulation At this point the Reactor product streams and the energy stream Coolant are unknown because the
105. it will be blue indicating that you have specified it 3 20 Steady State Simulation In the Fwd Order cell for H2O change the value to 0 to reflect the excess of water The Stoichiometry tab is now completely defined and appears as shown below Ni Kinetic Reaction Rxn 1 Stoichiometry and Rate Info H 18 015 1 000 0 00 0 00 12030 xide 58 080 1 000 0 00 12 Cadial 76 096 1 000 0 00 1 00 Add Comp Balance 0 00000 3 9e 04 Btu lbmole Balance Error Reaction Heat 25 C Stoichiometry Basis Parameters Delete Name Far Not Ready The next task is to define the reaction basis 10 11 12 13 In the Kinetic Reaction view click the Basis tab In the Basis cell accept the default value of Molar Concn Click in the Base Component cell By default HYSYS has chosen the first component listed on the Stoichiometry tab in this case H20 as the base component Change the base component to Propylene Oxide by doing one of the following e Open the drop down list of components and select 12C3Oxide e Begin typing 12C3QOxide and HYSYS filters as you type When 12C3QOxide is selected press the ENTER key You can have the same reaction occurring in different phases with different kinetics and have both calculated in the same REACTOR Chemicals Tutorial 3 21 14 In the Rxn Phase cell select CombinedLiquid from the drop down list The completed
106. made to the connection point at the Cooler inlet Adding Outlet and Energy Streams 1 Position the cursor over the right end of the Cooler icon The connection point and pop up Product appears 4 With the pop up visible left click and hold The transparent box again becomes solid black 5 Move the cursor to the right of the Cooler A white stream icon appears with a trailing line attached to the Cooler outlet The stream icon indicates that a new stream will be created after the next step is completed 6 With the white stream icon visible release the left mouse button HYSYS creates a new stream with the default name 1 7 Repeat steps 11 14 to create the Cooler energy stream originating the connection from the arrowhead on the Cooler icon The new stream is automatically named Q 100 The Cooler has yellow warning status indicating that all necessary connections have been made but the attached streams are not entirely known Figure 1 64 gt 100 CoolGas 1 E 101 8 Click the Attach Mode icon again to return to Move mode Steady State Simulation Defining the Material and Energy Streams The Cooler material streams and the energy stream are unknown at this point so they are light blue and purple respectively 1 Double click the Cooler icon to open its property view On the Connections page the names of the Inlet Outlet and Energy streams that you recently attached appear in the appropriate cells
107. move the legend double click anywhere in the plot resize the view i area then click and drag the legend to its new location 14 When you are finished viewing the Boiling Point Curves click the Close icon 2 101 Steady State Simulation Installing a Second Boiling Point Curves Utility Alternative to using the Utilities page of a stream property view you can also install a utility using the Available Utilities view Another BP Curves utility is installed for stream Residue This utility is used for the case study in the next section To install the utility 1 Doone of the following e press CTRL U e from the Tools menu select Utilities The Available Utilities view appears Figure 2 127 Notice the name of the utility created previously Kerosene BP Curves appears in the Available Utilities view Available Utilities Kerosene BP Curves Boiling Point Curves a CO2 Freeze Out Cold Properties Critical Properties Data Recon Utility Depressuring Hydrate Formation Utility Parametric LP Utility Pinch Utility Pipe Sizing Property Balance Utility x View Utility Add Utility Delete Utility 2 Select Boiling Point Curves and click the Add Utility button The Boiling Point Curves view appears opened to the Design tab Figure 2 128 Boiling Point Curves Boiling Point Curves 1 Boiling Point Curves 1 Object Type Stream x Notes Stream Select Object Basis Liquid Yolu
108. o LTSLiq DePropanizer Sepliq MIx 101 The following pages will guide you through building a HYSYS case to illustrate the complete construction of the simulation from selecting a property package and components to examining the final results The tools available in HYSYS interface will be utilized to illustrate the flexibility available to you Before proceeding you should have read the introductory chapter which precedes the Tutorials in this manual 1 3 Steady State Simulation l e Steady State Simulation 1 2 1 Process Description This tutorial will model a natural gas processing facility that uses propane refrigeration to condense liquids from the feed and a distillation tower to process the liquids The flowsheet for this process appears below Figure 1 2 LTSVap C3Buty Gas Gas ay ColdGas Sepv ap J Chiller yN Ovhd Sy CondDuty p SalesGas Feed InletSep bee 1 b MixerOut lt B gt Feed wed TowerFeed 2 LTSLiq hs sa G Mix 100 DewPoint neenu LiquidProd DePropanizer Sepliq Mix 101 The combined feed stream enters an inlet separator which removes the free liquids Overhead gas from the Separator is fed to the gas gas exchanger where it is pre cooled by already refrigerated gas The cooled gas is then fed to the chiller where further cooling is accomplished through exchange with evaporating propane represented by the C3Duty stream In the chiller which will be modeled simpl
109. other information such as a petroleum fluid characterization The fluid package for this example will contain the property package Peng Robinson the pure components H20 C3 iC4 nC4 iC5 nC5 and the hypothetical components which are generated in the Oil characterization 1 Click the Fluid Pkgs tab then click the Add button The Fluid Package Basis 1 view appears Figure 2 13 Fluid Package Basis 1 Property Package Selection Property Package Filter All Types t EOSs C Activity Models C Chao Seader Models Vapour Press Models C Miscellaneous Types Extended NATL GCEOS General NATL v Advanced Thermodynamics Component List Selection Component List 1 z View COMThermo faa Set Up Parameters Binary Coeffs StabTest Phase Order Axns Tabular Notes Name Basis PropetyPkg No This view is divided into a number of tabs that allow you to supply all the information necessary to completely define the fluid package For this tutorial however only the Set Up tab is used On the Set Up tab the currently selected Property Package is lt none gt Before you begin characterizing your petroleum fluid you must choose a property package that can handle hypothetical components If you have multiple fluid packages and components lists in a case you can use the drop down list in the Component List Selection group to attache a component list to a particular property package
110. produces heat so cooling is required Figure 3 65 Reactor Design Connections Parameters Single Phase User Variables Delta P 0 0000 psi Volume Notes k empty gt Liquid Yolume k empty gt C Heating a Liquid Level Duty 50 00 a Design Reactions Rating Worksheet Dynamics Delete NERS Ionored 6 Click the Reactions tab Next you will attach the Reaction Set that you created in the Basis Environment 7 From the Reaction Set drop down list select Set 1 The completed Reactions tab appears below Figure 3 66 Reactor Set 1 Reactions Reaction Informatiorr Details Reaction Set Set 1 Reaction Rgn Results Specifics Stoichiometry C Basis View Reaction Stoichiometry Stoich Coeff H20 18 015 12C30xide 58 080 i 12 C3diol 76 096 Add Comp 0 00000 Reaction Heat 25 C 3 9e 04 Btu lbmole Design Reactions Rating Worksheet Dynamics Dete O nomd o T oo The next task is to specify the Vessel Parameters In this Tutorial the reactor has a volume of 280 ft3 and is 85 full 3 52 Chemicals Tutorial 3 53 Click the Dynamics tab then select the Specs page In the Model Details group click in the Vessel Volume cell Type 280 ft3 then press ENTER 10 In the Lig Volume Percent cell type 85 then press ENTER HYSYS automatically calculates the Liquid Volume in the vessel 280 ft3 x 85 full 238
111. properties The properties ee AOP NOt as ne of Preheat Crude are shown below The values you specified are a stream ensure that the Solver Active icon in the tool different colour blue than the calculated values black bar is selected Figure 2 42 Workbook Case Main 4 m Ioj x Solver Active icon Name Preheat Crude New Yapour Fraction Temperature F Pressure psia Molar Flow Ibmole hr Mass Flow lb hr 1 1446 006 Liquid Volume Flow barrel day 1 000e 005 Material Streams Compositions Energy Streams Unit Ops ProductBlock_Preheat Crude LJ Include Sub Flowsheets FeederBlock_Preheat Crude L Show Name Only Number of Hidden Objects 0 The next task is to install and define the utility steam streams that will be attached to the fractionation tower later Installing the Utility Steam Streams 1 On the Material Streams tab click in the header cell labeled xx New HYSYS accepts blank 2 Type the new stream name Bottom Steam then press ENTER HYSYS spaces within a stream or creates the new stream operation name 3 Inthe Temperature cell enter 375 E In the Pressure cell enter 150 psia Figure 2 43 Workbook Case Main F Ioj x Name Preheat Crude Bottom Steam New Vapour Fraction lt empty gt Temperature F 375 0 Pressure psia g 00 150 0 Molar Flow Ibmole hr lt empty gt Tae 006 Liquid Yolume Flow barrel day
112. required components to the Fluid Package 1 Click the Enter Basis Environment icon The Simulation Basis Manager view appears 2 Click the Fluid Pkgs tab In the Current Fluid Packages group the Fluid Package associated with the Chemical Tutorial appears Figure 3 109 Simulation Basis Manager Current Fluid Packages gt gt Flowsheet Fluid Pkg Associations Import Export Default Fluid Pkg Basis 1 v m 7 Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Return to Simulation Environment Chemicals Tutorial 3 83 3 Inthe Current Fluid Packages group select the fluid package then click the View button The Fluid Package Basis 1 property view appears Figure 3 110 Fluid Package Basis 1 Property Package Selection NBS Steam NATL OLI_ Electrolyte Peng Robinson PRSY Sour PR 5 Property Package Filter All Types C EOSs C Activity Models Chao Seader Models C Vapour Press Models C Miscellaneous Types Component List Selection Activity Model Specifications Vapour Model Ideal UNIFAC Estimation Temp Use Poynting Correction Advanced Thermodynamics COMThermo Hegres SIGT 77 0000 F Vv Basis 1 Component List v ig Set Up Binary Coeffs Delete Name Basis 1 Property Pkg UNIQUAC Ideal Edit Properties StabTest Phase Order Tabular 4 Clic
113. required for this column 1 Flow of the Rectifier Distillate Propene is 775 lbmole hr 2 Rectifier Top Stage Reflux Ratio is 16 Adding the Distillate Rate specification First you will add the Propene Distillate Rate specification 1 Return to the Parent environment and ensure the Column property view is visible Click the Design tab and select Monitor page Click the Add Spec button The Add Specs view appears P1 8 Propylene Propane Splitter PQ Splitter P1 9 4 Inthe Add Specs view select Column Draw Rate then click the Add Spec s button In the Draw cell select Propene as the associated stream In the Spec Value cell enter775 Ibmole hr Adding the Reflux Rate Specification Next you will add the Rectifier Top Stage Reflux specification using a slightly different procedure than what you used to add the Distillate Rate Specification This is only to show you another way to add specifications 1 Click the Design tab then select the Specs page 2 Inthe Column Specifications group click the Add button The Add Specs view appears 3 Inthe Add Specs view select Column Reflux Ratio then click the Add Spec s button The Reflux Ratio Spec view appears 4 In the Stage cell select Condenser In the Flow Basis cell select Molar In the Spec Value cell enter 16 4 The specification views should appear as shown below Figure P1 3 b Reflux Ratio Spec Reflux Ratio C x Draw Spec Draw Rate Ol x
114. residence volume The vessel volume calculated for the Kero_SS_Reb is 20 5 m 11 Click the Dynamics tab then select the Specs page 12 In the Volume cell enter 20 5 m In the Level Calculator cell select Horizontal Cylinder from the drop down list Figure 2 165 Model Details Initialize From Products Dry Startup 2 591 Length m 3 887 Lig Volume Percent 50 00 Level Calculator Horizontal cylinder Fraction Calculator e levels and nozzles C Initialize From User 13 Close the Kero_SS_Reb property view 2 129 Dynamic Simulation Cooler Volume Sizing HYSYS assigns a default volume to each Cooler unit operation in the Column sub flowsheet In this section you will modify each pump around cooler to initialize with a default vessel volume 1 Double click the PA_1_Cooler operation in the PFD to open the property view Click the Dynamics tab then select the Specs page In the Model Details group click in the Volume cell then press DELETE The default volume of 0 10 m appears 4 Inthe Dynamic Specifications group ensure that all the specification checkboxes are inactive No dynamic specifications should be set for the pump around coolers Figure 2 166 Dynamic Specifications Overall Delta P kPa Overall k ka s sqrt kPa kg m3 lt empty gt Calculate k Spec Zones Close the PA_1_ Cooler view 6 Repeat this process for the PA_2_Cooler and the PA_3_C
115. residence time Total Liquid Exit Flow x Residence Time 2 2 0 5 Vessel Volume The vessel volume calculated for the Condenser is 88 3 m 5 Click the Dynamics tab then select the Specs page 6 Inthe Model Details group specify the vessel Volume as 88 3 m and the Level Calculator as a Vertical Cylinder Model Details Initialize From Products Dry Startup 4 216 Height m 6 324 Lig Volume Percent 50 00 J Level Calculator Vertical cylinder Fraction Calculator e levels and nozzles C Initialize From User Close the Condenser property view In the PFD double click the Kero_SS_Reb icon to open its property view 2 128 Refining Tutorial Tutorial 2 129 9 Click the Worksheet tab then select the Conditions page Figure 2 164 Kero_SS_ Reb Worksheet Kero_SS_ToRe Kerosene Kero_SS_Boill K apour 0 0000 0 0000 1 0000 emperature C 229 7 235 5 235 5 Properties ressure kPa Conditions c ti omposition Mass Flow kazh PF Specs td Ideal Lig Yol Flow m3 h 91 94 e 30 33 E Molar Enthalpy kJ kgmole 2 671e 005 2 697e 005 2 151e 005 Molar Entropy kJ kgmole C 334 9 347 3 403 3 eat Flow kJ h 1 32 e 008 8 934e 007 3 642e 007 10 In the Conditions page confirm that the Liquid Volumetric Flow Std Ideal Liq Vol Flow for Kerosene is 61 61 m h Assume a 10 minute of residence time and a 50 liquid level
116. stream feed and product connections and created two text user variables The Execute macro uses the GetObject method to open the target link case and then it attempts to locate the material stream in the target case named by the Initialize macro Acid Gas Sweetening with DEA bl Acid Gas Sweetening with DER G1 1 Process Description vi s aaa aaaea aa Vaaraa 3 G12 S6 UD aas a a a N aaa 5 G1 3 Steady State Simulation cccceeeeseeeseceeeeseeeeeeenseeseeenneeseoeneees 5 G1 3 1 Installing the DEA CONTACTOR cccccssseceeeeeeeeeeeeeees 6 G1 3 2 Regenerating the DEA ccccccessseeceecceeeeeeeeenseeesseaeeees 9 G1 4 Simulation Analysis 0012 cgfsecccsnescscecMMl ccnnsssssccnnssscccnasseneenes 15 G1 5 Calculating Lean amp Rich LOACINGS seesseeeeeeeeeeeeeeeeeeeeees 15 G1 6 Dynamic Similaires ccnnesccccnes MiiPenssscccnnsssscccnsssscennsssssennees 17 G1 6 1 Converting from Steady State cceeeeeeeeteeeeeeeees 17 G1 6 2 Adding a Control Scheme cccceeccccceseseeeeeeeeseaeeeeeeeees 27 G1 6 3 Preparing Dynamic Simulation cccceeeeeeeeeeeeeeeeenees 32 GLZ FREIEKENCES oaae Es aa 34 G1 1 Acid Gas Sweetening with DEA bl 1 Process Description In this example a typical acid gas treating facility is simulated A water saturated natural gas stream is fed to an amine contactor For this example Diethanolamine DEA at a strength of 28 w
117. stripper configuration shown in the above PFD is a common unit in refineries It processes sour water that comes from a variety of sources including hydrotreaters reformers hydrocrackers and crude units The sour water is often stored in crude tanks thereby eliminating the need for special vapour recovery systems A sour water stripper either uses the direct application of stripping steam usually low quality low pressure or a steam fired reboiler as a heat source Figure R2 2 Condenser ar Gas U Cond Q Stripper Fee Boilup 4m Reb Q Stripper Bottoms R2 3 R2 4 Introduction The intent is to drive as much H2S and NH3 overhead in the stripper as possible The sizing of a sour water stripper is very important since its capacity must equal or exceed the normal production rates of sour water from multiple sources in the refinery Often refiners find their strippers undersized due to a lack of allowance for handling large amounts of sour water which can result from upset conditions like start up and shutdown Consequently there is often a backlog of sour water waiting to be processed in the stripper With the increasing importance of environmental restrictions the sour water stripper plays a greater role in the overall pollution reduction program of refiners Ae c Introduction The Sour Water feed stream goes through a feed effluent exchanger where it recovers heat from the tower bottoms stream Stripp
118. the Attach Mode icon on the PFD toolbar to enter Attach Sepvap cotie GasiGas E 100 mode Ga SalesGas Gas Processing Tutorial 53 Processing Tutorial 1 53 CoolGas Q E 100 CooalGas is E 100 H If you make an incorrect connection l Click the Break Connection icon on the PFD toolbar Move the cursor over the stream line connecting the two icons A checkmark attached to the cursor appears indicating an available connection to break Click once to break the connection 2 Position the cursor over the right end of the CoolGas stream icon A small transparent box appears at the cursor tip Through the transparent box you can see a square connection point and a pop up description attached to the cursor tail The pop up Out indicates which part of the stream is available for connection in this case the stream outlet 3 With the pop up Out visible left click and hold The transparent box becomes solid black indicating that you are beginning a connection 4 Move the cursor toward the left inlet side of the Cooler A trailing line appears between the CoolGas stream icon and the cursor anda connection point appears at the Cooler inlet 5 Place the cursor near the connection point and the trailing line snaps to that point Also a solid white box appears at the cursor tip indicating an acceptable end point for the connection 6 Release the left mouse button and the connection is
119. the Databook Make changes to key variables in the process and observe the dynamic behaviour of the model 1 3 1 Modifying the Steady State Flowsheet It is necessary to add unit operations such as valves heat exchangers or pumps to define pressure flow relations between unit operations that have no pressure flow relation In this tutorial valve operations will be added between Separator Mixer and Column operations A Heater operation will also be added between the Mixer and Column operation for dynamic simulation purposes Installing a heater allows you to vary the temperature of the feed entering the column Valves will be added to the following material streams e SepLiq e LTSLiq e TowerFeed e LiquidProd The first task is to set the session preferences The steady state Gas 1 Open the pre built case file TUTOR1 hsc Processing simulation file TUTOR1 hsc is located in your 2 From the Tools menu select Preferences The Session Preferences HYSYS Samples directory view appears Click the Variables tab then select the Units page In the Dynamic simulation part In the Available Unit Sets group list select Field of this tutorial you will work with the default Field units 1 100 Dynamic Simulation 5 Click the Simulation tab then select the Dynamics page Figure 1 128 Session Preferences H SYS PRF Ioj xj General Options c J Use Input Experts Simulation Opti i i paons V View
120. the Microsoft Corporation Documentation Credits Authors of the current release listed in order of historical start on project 2002 1995 Pamela Smith Clement Ng BASc Sandy Brar BSc Jessie Channey BAC Tsitsi Ettienne BSc Angeline Teh BSc Sarah Jane Brenner BASc Conrad Gierer BASc Chris Strashok BSc Adeel Jamil BSc Yannick Sternon BIng Nana Nguyen BSc Allan Chau BSc Muhammad Sachedina BASc Lisa Hugo BSc BA Chris Lowe PEng Kevin Hanson PEng Since software is always a work in progress any version while representing a milestone is nevertheless but a point in a continuum Those individuals whose contributions created the foundation upon which this work is built have not been forgotten The current authors would like to thank the previous contributors A special thanks is also extended by the authors to everyone who contributed through countless hours of proof reading and testing Contacting Hyprotech Hyprotech can be conveniently accessed via the following Web site www hyprotech com Information and Sales info hyprotech com Documentation HypCalgaryDocumentation hyprotech com Training training hyprotech com Technical Support support hyprotech com Detailed information on accessing Hyprotech Technical Support can be found in the Technical Support section of the Get Started manual TAH3 1 B4814 NOV02 O Table of Contents A HYSYS Tutorials ccccccsececssesenseeseneeeeenseeeseneseenesene
121. the Name field at the bottom of the view Steady State Simulation lc Building the simulation Creating a Fluid Package The next step is to create a Fluid Package As a minimum a Fluid Package contains the components and property method for example an Equation of State HYSYS will use in its calculations for a particular flowsheet Depending on what is required in a specific flowsheet a Fluid Package may also contain other information such as reactions and interaction parameters 1 On the Simulation Basis Manager view click the Fluid Pkgs tab 2 Click the Add button and the property view for your new Fluid Package appears Figure 1 8 Property Package Selection Property Package Filter All Types EOSs C Activity Models C Chao Seader Models C Vapour Press Models C Miscellaneous Types a Advanced Thermodynamics Component List Selection moor COMThermo Heare mai Component List 1 7 View JEsi a Set Up The property view is divided into a number of tabs to allow you to supply all the information necessary to completely define the Fluid Package For this example the Set Up tab and Component List Selection group will be used You choose the Property Package on the Set Up tab The currently selected Property Package is lt none gt There are a number of ways to select a property package For this tutorial you will select the Peng Robinson property package 3 Do one
122. the figure below Figure 2 51 100 Design Name v 00 Connections Inlets Vapour Outlet Parameters User Variables Notes Energy Optional Fluid Package Liquid Outlet Basis 1 Design Reactions Rating Worksheet Dynamics Delete I EEE EET Icnored A unit operation property view contains all the information defining the operation organized into tabs and pages The Design Rating and Worksheet tabs appear for most operations Property views for more complex operations contain more tabs Many operations like the separator accept multiple feed streams Whenever you see a matrix like the one in the Inlets group the operation accepts multiple stream connections at that location When the matrix is active you can access a drop down list of available streams 6 Click in the Name field type PreFlash then press ENTER The status indicator at the bottom of the view shows that the operation requires a feed stream In the Inlets matrix click in the lt lt Stream gt gt cell Click the down arrow to open the drop down list of available streams Refining Tutorial Alternatively you could have 9 Select Preheat Crude from the list Preheat Crude appears in the made the connection by Inlets matrix and the lt lt Stream gt gt label is automatically moved DPU a betel down to a new empty cell The status indicator now displays name in the cell and pressing ENTER Requires a produ
123. the first time you have saved your case the Save Simulation Case As view appears Figure 1 20 Save Simulation Case As El FS Save in Z Cases e Save as type HYSYS Process Simulation Case hsc Cancel Steady State Simulation When you choose to open an existing case by clicking the Open Case icon or by selecting Open Case from the File menu a view similar to the one shown in Figure 1 20 appears The File Filter drop down list will then allow you to retrieve backup bk and HYSIM sim files in addition to standard HYSYS hsc files Workbook icon HYSYS accepts blank spaces within a stream or operation name By default the File Path is the Cases sub directory in your HYSYS directory To save your case do the following 1 Inthe File Name cell type a name for the case for example GASPLANT You do not have to enter the hsc extension HYSYS will automatically add it for you 2 Once you have entered a file name press the Enter key or click the Save button HYSYS will now save the case under the name you have given it when you save in the future The Save As view will not appear again unless you choose to give ita new name using the Save As command If you enter a name that already exists in the current directory HYSYS will ask you for confirmation before over writing the existing file lc Using the Workbook The Workbook displays information about streams and unit operat
124. the list of 4sigfig Workbook Tabs in issue tsigfig __ oe the same order as it Std Ideal Lig Vol Flow appears in the Workbook The new tab displays only these four Variables 1 48 Gas Processing Tutorial 649 Processing Tutorial 1 49 12 Close the Setup view to return to the Workbook and see the new tab Figure 1 61 Workbook Case Main MixerOut emperature F 60 00 ressure psia 600 0 Molar Flow MMSCFD 10 00 td Ideal Lig Yol Flow barrel da 4995 CoolGas SalesGas LTSVap emperature F lt empty gt lt empty gt lt empty gt ressure psia iz 590 0 __ lt empty gt lt empty gt 8 976 lt empty gt lt empty gt td Ideal Lig Yol Flow barrel da 4342 lt empty gt lt empty gt ee ee A Material Steams P_T Flow Energy Streams Unit Ops Paaisek Gea C Include Sub Flowsheets we oo C Show Name Only Number of Hidden Objects 13 At this point save your case by doing one of the following e Click the Save icon on the toolbar e Select Save from the File menu e Press CTRL S 1 2 8 Using the PFO The PFD is the other home view used in the Simulation environment Save Icon ev To open the PFD do one of the following PFD Icon e Click the PFD icon on the toolbar e Press CTRL P or from the Tools menu select PFDs The Select PFD view appears Select the required PFD from the list
125. the target case finds the target stream and copies the stream conditions from the main case 3 Inthe User Unit Op view Design tab select the Code page 4 Click the Edit button The Edit Existing Code view appears X1 10 Case Linking XT Linking X1 11 X1 4 1 Initializing the User Unit Op The following table contains a listing of the code required to implement this operation along with a brief description of what the code means Partitions placed in the code are made only to clearly associate the relevant code with the explanation Also indentations made in the code are common with standard programming practices Ozeye Explanation Sub Initialize Signifies the Start of the initialization subroutine You do not have to add it as it should already be there On Error GoTo Catch Preparing the interface ActiveObject FeedslName Feed ActiveObject ProductsilName Unused Prodi ActiveObject Feeds2Name Unused Feed2 ActiveObject Products2Name Unused Prod ActiveObject Feeds2Active False ActiveObject Products2Active False ActiveObject EnergyFeedsActive False ActiveObject EnergyProductsActive False Adding user variables Dim LinkCase As Object This UV will hold the Linked case name Set LinkCase ActiveObject CreateUserVariable LinkCas e LinkCase uvtText utcNull 0 Dim LinkStream As Object This UV will hold the Linked stream name Set LinkStream ActiveObject CreateU
126. then click the Add button The variable now appears in the Databook and the Variable Navigator view remains open Figure 1 103 ariable Navigator Flowsheet Variable Case Main C3Duty Specific Gravity rel Ail a De Propanizer COL1 ColdGas Std Gas Flow ConDuty Std Ideal Liq Mass De 2 CoolGias Std Ideal Liq Vol Flow Object Filter Std Lig Vol Flow Spec C All Steady State Specs Po cheam Surface Tension Temperature UnitOps Navigator Scope Thermal Conductivity Logicals Flowsheet Ui Component Liq C ColumnOps otal Component Ma eton C Case Total Component Mol C Basis Total Liquid Volume F Custom Utility Total Mass Fractions i Total Mole Fractions User Property I lear Ww ari ahlas Variable Description D ewPoint Cancel Gas Processing Tutorial BT Processing Tutorial 1 81 13 Repeat the previous steps to add the following variables to the Databook e Sales Gas stream Molar Flow variable change the Variable Description to Sales Gas Production e LiquidProd stream Liq Vol Flow Std Cond variable change the Variable Description to Liquid Production The completed Variables tab of the Databook appears as shown below Figure 1 104 ioj xi Available Data Entries Object Variable 0S Vessel Temperature SalesDP DewPoint SalesGas Sales Gas Production iat LiquidProd Liquid Production sae Delete Case Studies Data Recorder Process Da
127. this cell Enter Min Available 0 Btu h Max Available 6x10 Btu h 29 Close the FCV for RebDuty view 30 Click the Face Plate button Change the controller mode to Auto on the face plate Close the face plate view 31 Close the Reb LC property view Temperature Control Temperature control is important in this dynamic simulation case A temperature controller will be placed on the ColdGas stream to ensure that the SalesGas stream makes the 10 F dewpoint specification Temperature control will be placed on the top and bottom stages of the depropanizer to ensure product quality and stable column operation 1 Enter the Main Flowsheet environment by clicking the Enter Parent Simulation Environment button Next you will add a PID Controller operation that will serve as the ColdGas temperature controller 2 On the Object Palette click the Control Ops icon A sub palette appears Right click the PID Controller icon and drag the cursor to the PFD 4 Double click the controller icon to open its property view Specify the following details Tab Page In this cell Enter Process Variable Source ColdGas Temperature Output Target Object C3Duty Gas Processing Tutorial 16125 Processing Tutorial 1 125 Tab Page In this cell Enter shown here do not use the default units Enter the values a E HP He eects HYSYS automatically converts the values to the default units 5 Click th
128. this cell Enter os 11 Click the Control Valve button The FCV for Diesel_SS_ Draw view appears 12 In the Valve Sizing group enter the following details In this cell Enter Flow Type MolarFlow 13 Close the FCV for Diesel_SS_ Draw view 14 Click the Face Plate button The Diesel FC face plate view appears Change the controller mode to Auto and input a set point of 127 5 m3 h 2 135 Dynamic Simulation 15 Close the property view but leave the face plate view open 16 Click the PID Controller icon in the Object Palette then click near the AGO stream on the PFD The controller icon appears 17 Double click the controller icon then specify the following details Tab Page In this cell Enter aore O OOOO a e 18 Click the Control Valve button The FCV for AGO SS Draw view appears 19 In the Valve Sizing group enter the following details In this cell Enter Flow Type MolarFlow 20 Close the FCV for AGO SS_Draw view 21 Click the Face Plate button The AGO FC face plate view appears Change the controller mode to Auto and input a set point of 29 8 m3 h 22 Close the property view but leave the face plate view open 23 Save the case as DynTUT2 4 hsc 2 5 4 Adding Pressure Flow Specifications Before integration can begin in HYSYS the degrees of freedom for the flowsheet must be reduced to zero by setting the pressure flow specifications Norm
129. this process appears below Figure 3 2 Ovhd Vap CondDuty Reactor e RecyProds Vent Prop Oxide Mixer Out Water nii 1 00 Coolant Feed Reactor RebDuty Glycol The propylene oxide and water feed streams are combined in a Mixer The combined stream is fed to a Reactor operating at atmospheric pressure in which propylene glycol is produced The Reactor product stream is fed to a distillation tower where essentially all the glycol is recovered in the bottoms product The two primary building tools Workbook and PFD are used to install the streams and operations and to examine the results while progressing through the simulation Both of these tools provide you with a large amount of flexibility in building your simulation and in quickly accessing the information you need The Workbook is used to build the first part of the flowsheet including the feed streams and the mixer The PFD is then used to install the reactor and a special sequence of views called the Input Expert will be used to install the distillation column Figure 3 3 Chemicals Tutorial 3 5 3 2 2 Setting Your Session Preferences Start HYSYS and create a new case Your first task is to set your Session Preferences From the Tools menu select Preferences The Session Preferences view appears Session Preferences hysys PRF oj x Simulation Options Desktop Naming Tool Tips Dynamics Performanc
130. views 18 Double click on the Column T 100 icon in the PFD then click the Column Environment button to enter the Column subflowsheet 19 On the column PFD double click the Main TS Column icon to enter the Main TS property view 20 Click the Rating tab then select the Sizing page 21 Enter the previous calculated values into the following tray section parameters Be aware that the default units for each tray section Diameter 5 639m parameter may not be e Tray Spacing 0 6096m consistent with the units Weir Height 0 0508m provided in the tray sizing utility You can select the units e Weir Length Actual Weir Length 4 44m you want from the drop down 22 In the Internal Type group select the Valve radio button list that appears beside each input cell Figure 2 158 Sizing Tray Space m Tray Yol m3 Heat Loss Diameter m Tray Dimensions Efficiencies Pressure Drop Weir Height m 5 080e 002 Weir Lenath m 4 440 H8 936e 002 lt empty gt Flow Paths 1 Internal Type C Sieve Valve C Bubble Cap Packed Quick Size Design Rating Worksheet Performance Dynamics Delete ES core 2 123 Dynamic Simulation 23 Close the Main TS property view 24 Access the Column property view by clicking the Column Runner L icon in the tool bar Column Runner icon 25 Click the Parameters tab then select the Profiles page Observe the steady state press
131. will leave the top of the absorber whereas the rich amine stream from the bottom will be sent to a regenerator column An analysis on both the SWEET GAS and the ACID GAS will be performed to satisfy the specified criterion 3 Dynamics Simulation The steady state solution will be used to size all the unit operations and tray sections An appropriate control strategy will be implemented and the key variables will be displayed Acid Gas Sweetening with DEA ble Setup l Select the following components N2 CO2 H2S C1 C2 C3 i C4 n C4 i C5 n C5 C6 C7 H20 and DEAmine Select the following property package Amines The Amines property package is required to run this example problem This is a D B Robinson proprietary property package that predicts the behaviour of amine hydrocarbon water systems Use the Li Mather Non Ideal Thermodynamic model In the Session Preferences clone the Field unit set then change the default units for the Liquid Volume Flow to USGPM and the molar Flow to MMSCFD 01 3 Steady State Simulation There are two main steps for setting up this case in steady state l Installing the DEA Contractor A 20 stage absorber column will be used to scrub the SOUR GAS stream with DEA solution DEA TO CONT The SWEET GAS will leave the tower from the top whereas the pollutant rich liquid will be flashed before entering the REGENERATOR Regenerating the DEA The liquid stream from the absorber will b
132. you type displaying only those components that match your input Figure 3 12 Components Available in the Component Library Match Propylened View Filters Sim Name C Full Name Synonym C Formula BisPhenol p p lsopropylidenebisphenol C15H1602 12 CIC3 Propylene_Chloride C3HECI2 12 CIC3 Propylene_Dichloride C3HECI2 12 C3diol Propylene_Glycol C3H802 C3 Carbonate Propylenecarbonate C4H603 12C30 xide PropyleneO side C3H60 J Show Synonyms Cluster 4 When propylene oxide is selected in the list add it to the Selected Components List by doing one of the following e Press the ENTER key e Click the Add Pure button e Double click on PropyleneOxide Steady State Simulation The component now appears in the Selected Components List Figure 3 13 Component List View Add Component p Selected Components Components Available in the Component Library E Components 12C30xide Match Propyleneo View Filters Traditional Electrolyte Sim Name C Full Name Synonym C Formula Hypothetical Other BisPhenol p p l sopropylidenebisphenol C15H1602 12 CIC3 Propylene_Chloride C3HECI2 12 CIC3 Propylene_Dichloride C3HECI2 12 C3diol Propylene_Glycol C3H802 C3 Carbonate Propylenecarbonate C4H603 V Show Synonyms T Cluster Selected Component by Type Delete Component List 1 Another method for finding components is to use the View Filters to display only those component
133. your Session Preferences before building a case Gas Processing Tutorial 1 7 2 From the Tools menu select Preferences The Session Preferences view appears You should be on the Options page of the Simulation tab Figure 1 4 Session Preferences HYSYS PRF lol x General Options laces J Use Input Experts Options V View New Streams upon Creation Iv Confirm Deletes Desktop Use Modal Property Views Iv Confirm Mode Switches Naming V Record Time When Notes Are Modified J Enable Single Click Actions Tool Tips J Enable Cross Hairs On PFD J Enable Cell Edit Button Dynamics Errors Performance Display Errors in Trace Window Licensing Display Numerical Errors in Trace Window Ignore Them in Dynamics Mode ATI Server Show Property Package Warning Column V Show Property Package Warning Status Window Property Correlations Trace Window MV Activate Standard Property Correlations MV Confirm Before Adding if Active Correlations are Present E Simulation Reports Resources Extensions j Oillnput Tray Sizing Save Preference Set Load Preference Set 3 Inthe General Options group ensure the Use Modal Property Views checkbox is unchecked Creating a New Unit Set The first step in building the simulation case is choosing a unit set Since HYSYS does not allow you to change any of the three default unit sets listed you will create a new unit set by cloning an existing one For this
134. 0 Percent of Light Ends in Assay 1 1300 Input Data Calculation Defaults Working Curves Correlations User Curves Delete Name ssa Assay Was Not Calculated Calculate Before entering any of the assay data you must activate the molecular weight density and viscosity curves by choosing appropriate curve types in the Assay Definition Group Currently these three curves are not used sA 10 11 From the Bulk Properties drop down list select Used A new radio button labeled Bulk Props appears in the Input Data group From Molecular Wt Curve drop down list select Dependent A new radio button labeled Molecular Wt appears in the Input Data group From the Density Curve and Viscosity Curves drop down lists select Independent as the curve type For Viscosity two radio buttons appear as HYSYS allows you to input viscosity assay data at two temperatures Your view now contains a total of seven radio buttons in the Input Data group The laboratory data are input in the same order as the radio buttons appear Refining Tutorial 2 23 In the next few sections you will enter the following laboratory assay data e bulk molecular weight and density e TBP Distillation assay data e dependent molecular weight assay data e independent density assay data e independent viscosity assay data at two temperatures Entering Bulk Property Data 1 Select the Bulk Props radio b
135. 0 Molar Flow Ibmole hr 3814 416 3 166 5 Mass Flow lb hr 1 144e 006 500 3000 Liquid Volume Flow barrel day 1 000e 005 514 6 205 8 Heat Flow Btu hr 7 619e 008 4 222e 007 1 697e 007 Name AGO Steam i Material Streams Compositions Energy Streams Unit Ops FeederBlock_Preheat Crude J Include Sub Flowsheets PreFlash L Show Name Only Number of Hidden Objects 0 The operation to which Preheat Crude is attached appears in this display field Double click the operation name to access its property view Refining Tutorial 2 53 Adding a Tab to the Workbook When the Workbook is active the Workbook item appears in the HYSYS menu bar This item allows you to customize the Workbook In this section you will create a new Workbook tab that displays only stream pressure temperature and flow 1 Doone of the following e From the Workbook menu select Setup e Object inspect right click the Material Streams tab in the Workbook then select Setup from the menu that appears The Workbook Setup view appears Figure 2 58 Workbook Tabs Tab Contents Add Object Currently all Name Material Streams Order variables appear Delete D E ZETTE with four significant Type Material Stream New Type figures a can Variables change the display format or precision Format Use Set ml 1 4 fixed Hesa of any Workbook Temperature 4 sig fig Add variables by
136. 0 16332 8 0375e 00 NBP_236 fae ai 144 8 72 82 0 17922 8 9059e 00 NBP_259 Arala 152 7 68 88 0 20002 0 10003 NBP_257 287 2 160 9 66 19 0 22056 0 11042 __NBP_311 311 0 170 4 64 01 0 25354 0 12631 NBP_336 335 8 178 4 62 56 0 30509 0 14955 NBP_361 360 8 189 5 61 27 0 37361 0 17794 NBP_386 386 0 201 4 59 89 0 46242 0 21164 NRP 411 4in4g 7145 A 73 NAPRFA nan Z ns Data Correlations Tables Property Plot Distribution Plot Composite Plot Plot Summary __ Delete Name Blend Blend Was Calculated Refining Tutorial These components could be used in the simulation Suppose however that you do not want to use the IBP as the starting point for the first temperature range You could specify another starting point by changing the Cut Option to User Ranges For illustration purposes 100 F is used as the initial cut point 6 Return to the Data tab Since the NBP of the 7 From the Cut Option Selection drop down list select User Ranges heaviest Light Ends i component is the starting The Ranges Selection group appears point for the cut ranges 8 Inthe Starting Cut Point field enter 100 E This is the starting point Bese NYPOCOMPONENIS WEE for the first range The same values as the HYSYS defaults are used generated on a light ends free basis That is the Light for the other temperature ranges SNOS Are CAU ala 9 In the Cut End point T column in the table click on the top
137. 0 6 760 6 8712 1 100e 004 1 971e 004 td Ideal Lig Yol Flow USGPM 20 83 22 01 42 84 Molar Enthalpy Btu Ibmole 6 203e 004 1 225e 005 1 086e 005 Molar Entropy Btu Ibmole F 5 768 1 499 0 8824 eat Flow Btu hr 7 804e 006 7 481e 007 8 262e 007 I oz SS a g a any m gt x Dynamics Chemicals Tutorial AT Tutorial 3 41 16 In the Workbook click the Unit Ops tab The new operation appears in the table Figure 3 51 Workbook Case Main OF Xx p Name Obiect Type inlet Outlet Ignored Calc Level Prop Oxide i Mlx lt 100 Mixer Out Water Feed View Unit0p Add Unit0p Delete Unit0p i Material Streams Compositions Energy Streams Unit Ops Prop Oxide C Include Sub Flowsheets Water Feed Mixer Out The table shows the operation Name Object Type the attached streams Inlet and Outlet whether it is Ignored and its Calc Level When you click the View UnitOp button the property view for the currently selected operation appears Alternatively by double clicking on any cell except Inlet or Outlet associated with the operation you will also open its property view You can also open a stream property view directly from the Workbook Unit Ops tab When any of the cells Name Object Type Ignored or Calc Level are selected the gray box at the bottom of the v
138. 000 0 000213 4 0000 0 000039 1 0000 0 000007 0 000716 0 000309 0 000133 7 Temp C Press Flows Specifications eflux Ratio istillate Rate ap Prod Rate WasteH20 Rate lt empty gt 2 000e 004 barrel day 0 773 Specified Value Curent Value Wt Eror Active Estimate Current a 0 2268 0 0000 barrel day 2 00e 004 4 72e 003 lt empty gt 0 0000 0 0000 lt empty gt eroSS Prod Flow 1 300e 004 barrel day 1 30e 004 0 0000 ero55 Boillp Ratio 0 7500 0 533 DieselSS Prod Flow 1 700e 004 barrel day View Add Spec Group Active Update Inactive Degrees of Freedom f 1 70e 004 Flowsheet 0 2172 0 0001 Reactions Ka iian fica fin fica lica V AKIKI zj Dynamics J Update Outlets Ignored The converged temperature profile is currently displayed in the upper right corner of the view To view the pressure or flow profiles select the appropriate radio button In the Performance tab the Column Profiles and Feed Products pages display more detailed stage summary In the Basis group near the top of the view select the Liq Vol radio button to examine the tray vapour and liquid flows on a volumetric basis Refining Tutorial 2 89 The Column Profiles page appears below Figure 2 109 L Column Atmos Tower COL1 Fluid Pkg Basis 1 7 Peng Robinson Reflux
139. 000e 005 7 650e 008 3000 205 8 1 697e 007 WasteH20 4 504e 004 3090 2 547e 008 Residue 4 958e 004 4941 3 034e 007 1 095e 006 9 506e 004 7 346e 008 1 095e 006 9 506e 004 5 484e 008 Diesel 0 0000 1 144e 006 1 000e 005 5 787e 008 467 3 30 99 7 021e 005 5 508e 004 5 535e 005 1 412e 005 5 759e 004 655 1 1 902e 005 7122 004 7 852 1 754e 008 2 000e 004 3779 3 702e 008 4 503e 004 2 839e 008 1 300e 004 9 624e 007 5001 4 034e 007 1 700e 004 1 271e 008 Compositions Energy Streams Unit Ops C Include Sub Flowsheets L Show Name Only Number of Hidden Objects 0 2 97 2 98 Steady State Simulation ih Object Navigator icon You can start or end the search string with an asterisk which acts as a wildcard character This lets you find multiple objects with one search For example searching for VLV will open the property view for all objects with VLV at the beginning of their name 2 98 Using the Object Navigator Now that results have been obtained you can view the calculated properties of a particular stream or operation The Object Navigator allows you to quickly access the property view for any stream or unit operation at any time during the simulation 1 Open the Navigator by doing one of the following e
140. 009 Distillate Rate lt empty gt 476 lt empty gt Reflux Rate lt empty gt 476 lt empty gt Btms Prod Rate lt empty gt 143 lt empty gt View Add Spec Group Active Update Inactive Degrees of Freedom 0 Design Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset o Converged J Update Outlets Ignored kalkalkalkalkalka The converged temperature profile appears in the upper right corner of the view 2 Select the Press or Flow radio button to view the pressure or flow profiles 3 62 Chemicals Tutorial 3 63 3 To access a more detailed stage summary click the Performance tab then select the Column Profiles page Figure 3 83 L Column Tower COL1 Fluid Pkg Basis 1 UNIQUAC Ideal Basis Performance Reflux Rato eth Bate La Flows Energy i E Mass Lig Vol Summary eboil Ratio Column Profiles Pressure Net Liquid Net Vapour Net Feed Net Draws Feeds Products F psi lbmole hr Plots OO 475 785 i 498 675 951 5711 498 964 974 460 498 737 974 750 494 326 974 522 1188 80 970 111 1189 94 1046 04 1183 75 1047 17 1082 20 1040 99 913848 939 438 960 612 771 084 817 847 T Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics
141. 04 3 487e 011 2 018e 002 15_ Main TS 1 922e 010 1 033e 004 1 549e 010 3 297e 002 16_ Main TS 1 906e 010 1 020e 004 6 853e 010 5 17 1e 002 17_Main TS 1 894e 010 9 97 7e 005 3 007e 003 7 647e 002 18_Main TS 1 884e 010 9 568e 005 1 303e 008 0 1040 19_Main TS 1 876e 010 8 910e 005 5 538e 008 1 351e 013 8 01 4e 005 1 398e 007 9 749e 017 6 985e 005 4 661e 007 0 1261 0 1338 0 1213 22_ Main TS 1 256e 018 5 763e 005 1 516e 006 7 723e 002 H ManmTcl a7ec nn2 07442 1097 0721 4 v 2 39Ne 005 15240008 E EAINNT od Clear Tray Clear All Trays Update Restore Normalize Trays Lock Estimates Unlock Estimates Phase C Yap Lig Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Conweged o J Update Outlets Ignored 3 To view the 1 Propanol composition on Tray 20 scroll through the group until you can see Tray 20 and the 1 Propanol component Stage 20 has a high concentration of 1 Propanol which has the greatest concentration among the heavy alcohols Therefore we have selected the appropriate stage for the Fusel draw C1 12 Ethanol Plant CIB Plant C1 13 C14 Results Workbook Case Main Material Streams Tab Figure C1 6 Workbook
142. 1 5 Input Data Bulk Props Light Ends Basis Liquid Yolume ne Light Ends Distillation Light Ends pt Methane 6 500e 003 258 7 Ethane 2 250e 002 127 5 Propane 0 3200 43 78 Butane 0 2400 1089 n Butane 0 8200 31 10 0 0000 212 0 Percent of Light Ends in Assay You can scroll through this 10 Upon completion of characterizing the assay select the Calculate o ii 50 points of button HYSYS will calculate the Working Curves which can be i aia viewed on the Working Curve tab Figure R1 6 Ni Assay Assay 1 Assay Working Curves Moles Cum Moles Mole Wt tes Me 0 00000 0 00000 31 10 56 89 0 01000 0 01000 48 77 59 71 0 01000 0 02000 64 86 62 74 0 01000 0 03000 81 66 65 92 0 01000 0 04000 98 48 69 54 0 01000 0 05000 gee 73 45 0 01000 0 06000 131 8 77 38 0 01000 0 07000 148 1 81 33 0 01000 0 08000 164 0 85 15 0 01000 0 09000 177 5 87 99 0 01000 0 10000 187 4 90 37 0 02500 0 12500 214 9 98 77 0 02500 0 15000 247 6 108 1 0 02500 0 17500 278 9 117 4 0 02500 0 20000 310 2 127 2 Input Data Calculation Defaults Working Curves Plots Correlations User Curves Delete Name Assay t Calculate 11 Close the Assay view R1 8 Atmospheric Crude Tower RQ Crude Tower R1 9 Create the Blend Cut the Oil Compo
143. 1300 barrel da 10 Click the Install button and a view summarizing your input appears 11 Click the Close icon to return to the Column property view Summary information for the new side operation appears in the table on the Side Ops tab Side Stripper Summary es Outlet Flow Reboiler Duty g9_MainTS 8_MainTS gt lt empty gt lt empty gt 12 Use the previous steps to install the two remaining side strippers DieselSS and AGOSS These are both Steam Stripped so choose the appropriate Configuration radio button and create the Steam Feed and Product streams as shown in the following figures The COL1 suffix is added automatically 2 7 Steady State Simulation The completed DieselSS and AGOSS side stripper views appear in the following figure Figure 2 93 Nil Side Stripper DieselSS Nil Side Stripper AGOSS Name DieselSS Name jacoss Return Stage Return Stage 16_ Main TS 21_ Main TS Configuration Configuration Draw Stage Reboiled Draw Stage C Reboiled 17 _Main TS Steam Stripped 22_Main TS Steam Stripped Steam Feed Steam Feed Diesel Steam 7 AGO Steam x Flow Basis Flow Basis C Molar C Molar C Mass Mass Volume Volume C Std Volume Product Stream Information Std Volume Product Stream Information Diesel AGO Delete Install 17000 barrel da Delete Install Draw Spec 9 5000 barrel da Although not a requirement the names of the Steam Feed streams creat
144. 253 4342 1089 3253 1742 1273 468 1 Heat Flow Btu hr Name i Material Streams P T Flow FeederBlock_Feed 1 MIx lt 100 Workbook Case Main xx New xx Compositions 2 746e 007 E E 7 Comp Mole Frac Workbook Ni 0 0700 3 756e 007 Energy Streams 9 658e 006 Unit Ops MixerOut 2 809e 007 1 541e 007 SepLig 9 765e 006 4 077e 006 C Include Sub Flowsheets L Show Name Only Number of Hidden Objects O x 0 0132 0 0017 CoolGas a d 0 0145 Comp Mole Frac workbook CO 0 0100 0 0060 0 0034 0 0063 Comp Mole Frac workbook Me 0 6000 0 6098 0 1905 0 6576 Comp Mole Frac Workbook Et 0 2000 0 1866 0 2044 0 1846 Comp Mole Frac Workbook Pr 0 1000 0 1054 0 2612 0 0877 Comp Mole Frac workbook i B 0 0400 0 0412 0 1640 0 0272 Comp Mole Frac Workbook n i Name 0 0400 SalesGas 0 0378 LTSLigq 0 1748 Tower Feed 0 0222 LiquidProd Comp Mole Frac Workbook Ni 0 0176 0 0021 0 0019 0 0000 Comp Mole Frac workbook CO 0 0066 0 0051 0 0045 0 0000 Comp Mole Frac Workbook Mld 0 7578 T 0 2593 0 2344 0 0000 Comp Mole Frac workbook Et 0 1605 0 2802 0 2528 0 0000 Comp Mo
145. 277 1410 lt empty gt All input curves except distillation are on midpoint basis Dependent curves will be shifted to middle Cancel OK 11 Click the OK button to return to the Assay property view Entering Molecular Weight Data 1 Select the Molecular Wt radio button The corresponding assay matrix appears Since the Molecular Weight assay is Dependent the Assay Percent column displays the same values as those you entered for the Boiling Temperature assay Therefore you need only enter the Molecular Weight value for each assay percent Click the Edit Assay button and the Assay Input Table view appears Click on the first empty cell in the Mole Wt column Type 68 then press the down arrow key 2 25 2 26 2 26 Steady State Simulation 4 Type the remaining Molecular Weight values as shown Figure 2 23 Assay Input Table x Assay Input Data Assay Percent All input curves except distillation are on midpoint basis Dependent curves will be shifted to middle Cancel OK 5 Click the OK button when you are finished Entering Density Data 1 Select the Density radio button The corresponding assay matrix appears Since the Density assay is Independent you must input values in both the Assay Percent and Density cells 2 Using the same method as for the previous assays enter the API gravity curve data as shown here Figure 2 24 A
146. 3 0 0000 w M M Distillate Rate lt empty gt lt empty gt lt empty gt v M M Reflux Rate lt empty gt lt empty gt lt empty gt 1 ww T Btms Prod Rate lt empty gt lt empty gt lt empty gt M Li View Add Spec Group Active Update Inactive Degrees of Freedom 0 Side Ops lt Design Parameters Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged J Update Outlets Ignored The Monitor page displays the status of your column as it is being calculated updating information with each iteration 3 59 3 59 3 60 Steady State Simulation Adding a Column Specification The current Degrees of Freedom is zero indicating the column is ready to be run however the Distillate Rate Overhead Liquid Rate for which no value was provided in the Input Expert is currently an Active specification with a Specified Value of lt empty gt For this example you will specify a water mole fraction of 0 005 in the Glycol product stream 1 Since it is not desirable to use this specification clear the Active checkbox for the Distillate Rate The Degrees of Freedom increases to 1 indicating that another active specification is required Nil Add Specs Tower CO EG Column Specification Types On the Design tab select the Specs page Column Component Flow In the Column Specifications group
147. 3 80 3 80 Dynamic Simulation 6 Click the Streams tab The Streams tab contains a list of recommendations regarding the setting or removing of pressure flow specifications in the flowsheet Figure 3 107 Nil Dynamics Assistant Stream Specs Remove pressure specifications in these streams Pressure Specs Prop Oxide Flow Specs Uninitialized Insert Valves Int Flow Spec E Set pressure specifications in these streams Tell me why T z General Streams Pressure Flow Specs Unknown Sizes Tray sections ler J Analyze Again i Cancel 7 For each page in the Streams tab activate or deactivate the following recommendations Page Recommendation Stream OK Checkbox Pressure Specs Remove Pressure Prop Oxide Active Specifications Remove Flow Prop Oxide ee Insert Valves Insert Valves The Dynamics Assistant will insert valves on all the boundary flow streams except the Reactor Vent stream This recommendation was deactivated since it is assumed that the CSTR reactor is exposed to the open air Therefore the pressure of the reactor is constant A constant pressure can be modeled in the CSTR reactor by setting the Reactor Vent stream with a pressure specification A valve should not be inserted on this stream x Dynamic Mode Icon Chemicals Tutorial 3 81 8 Click the Other tab This tab contains a list of miscellaneous changes that should be made in order for the Dynamic simula
148. 4 aval asi l _ 3929e 00 m r lt meP _213 212 8 138 4 76 48 0 16473 8 1156e 00 Blen z NBP_238 9 0047e 00 NBP_261 64 0 0 10077 NBP_289 tal 5 00 2 omnt NBP_313 FJ s 0 0 12795 NBP_338 i 0 15144 NBP_362 3 is o 0 18006 NBP_388 0 21393 NRP 41 l nanara Data Correlations Tables Property Plot Distribution Plot Composite Plot Plot Summary Delete Name Blend Blend Was Calculated Use the vertical scroll bar to view the components which are not currently visible in the Component Physical Properties table Viewing the Qil Distributions 1 To view the distribution data select Oil Distributions from the Table Type drop down list The Tables tab is modified as shown below Figure 2 33 Blend Blend 1 T able Te Cut Input Information r Eut Distributions e PETE a able E Dil Blend 1 v Pon Ries Conelations _ Correlations Tables Kerosene Light Diesel Heavy Diesel isf Liquid Voume _LtSt Run 58 Naphtha O B Naphtha i Kerosene Light Diesel __ Heavy Diesel Atm Gas Oil Atm Gas Oil Residue Residue Straight Run C Cycle Dil C Yacuum Oil 2 User Custom Property Plot Distribution Plot Composite Plot Delete Name Blend Bend Was Caeulted Refining Tutorial At the bot
149. 40 trays 29 in the Main Tray section 3 trays in each of the 3 Side Strippers 1 reboiled and 2 steam stripped a reboiler and a condenser R1 13 RIG Steady State Simulation Steady State Simulation 4 Inthe Column Property view connect the Inlet and Outlet streams to the column sub flowsheet as shown Design tab Connections page Figure R1 9 Inlet Streams Split Main Steam 29 MainTS T P Flash Trim Q Trim gt 28_MainTS _ None Req d Atm Feed AtmFeed gt 28 Main TS T P Flash Kero_SS_Energy lt lt Stream gt gt Kero SS_Reb None Req d Diesel Steam Diesel Steam 3 Diesel 55 T P Flash AGO Steam AGO Steam 3_ AGO 55 T P Flash j 4 45 8 Outlet Streams Residue Residue 23_ManTS L T P Flash Atmos Cond Atmos Cond Condenser Q None Req d Off Gas Off Gas Condenser VY T P Flash Waste Water Waste Water Condenser Ww T P Flash Naphtha Naphtha Condenser L T P Flash Kerosene Kerosene Kero_SS_Reb E T P Flash E L Q Q Q Diesel Diesel 3_Diesel_SS T P Flash AGO AGO 3 AGO 55 T P Flash P _1_0 lt lt Stream gt gt lt empty gt None Req d P _2 Q lt lt Stream gt gt lt empty gt None Req d PA_ 3 0 lt lt Stream gt gt lt empty gt None Req d New lt lt Stream gt gt t 5 Modify the Draw and Return stages of the Pump Arounds and Side Strippers on the corresponding page of the SideOps tab
150. 61 1000 1000 1000 1 0C 2 3 Phase 0 1907 0 5263 1000 1 000 1 000 1 0C pene 0 1919 05264 1 000 1 000 1 000 1 0c 0 1934 O5267 1000 1000 1 000 1 0C 0 1953 0 5270 1 000 1 000 1 000 1 0C 01977 O5273 1000 1000 1000 1 0C 0 2007 0 5278 1000 1000 1000 1 0C o 2045 05284 1000 1000 1 000 1 00 0 2093 05291 1000 1000 1 000 1 0C 02151 05299 1000 1000 1000 1 0C 0 2217 0 5309 1000 1000 1 000 1 0 0 2270 05319 1000 1000 1000 1 0C 0 2248 0 5328 1000 1000 1000 1 0C 0206 05333 1000 1000 1000 1 00 0 1497 0 5334 1000 1000 1 000 1 00 9426e 05315 1000 1000 1 000 10C Reset H25 C02 Transpose Eff Multi Spec Specify gt a Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Converged J Update Outlets P Ignored Next add a valve and another separator The stream Rich DEA from the absorber is directed to valve VLV 100 where the pressure is reduced to 90 psia close to the regenerator operating pressure G1 8 Acid Gas SweeteningwithDEA amp 19 Gas Sweetening with DEA G1 9 Add a Valve Valve VLV 100 oe nthe cell Enters Design Connections RICH DEA FLASH TK Add a Separator Gases that are flashed off from the RICH DEA stream are removed using the rich amine
151. 61e 008 3 743e 008 4 222e 007 3 647e 008 7 452e 008 2 296 8 561e 007 Name Naphtha Kero Kero_SS_Draw Kero_SS_Retur Kero_SS_BoilU Kero_SS_ToRe Diesel Steam Vapour Fraction 0 0000 0 0000 0 0000 1 0000 1 0000 0 0000 1 0000 Temperature F 107 3 457 5 406 1 429 3 457 5 446 9 300 0 Pressure psia 19 70 29 84 29 84 29 84 29 84 29 84 50 00 Molar Flow Ibmole hr 2822 701 3 912 4 210 5 371 2 1073 166 5 Mass Flow lb hr 2474e 005 1 115e 005 1 397e 005 2816e 004 5 561e 004 1 67 1e 005 3000 Liquid Yolume Flow barrel day 2 300e 004 9300 1 171e 004 2410 4681 1 398e 004 205 8 Heat Flow Btu hr 2 331e 008 8 098e 007 1 063e 008 1 77 7e 007 3 406e 007 1 225e 008 1 697e 007 Name Diesel Diesel_SS_Dra Diesel_SS_Reti AGO _5 AGO_SS_Draw AGO_SS_Retui Yapour Fraction 0 0000 0 0000 1 0000 0 0000 1 0000 0 0000 1 0000 Temperature F 486 9 512 1 504 9 571 6 300 0 615 4 602 9 Pressure psia 30 95 30 39 30 99 31 70 50 00 31 70 31 70 Molar Flow Ibmole hr 1114 1331 383 8 200 4 138 8 oho 210 7 Mass Flow lb hr 2 429e 005 2 800e 005 4 015e 004 5 945e 004 2500 7 563e 004 1 868e 004 Liquid Yolume Flow barrel day 1 925e 004 2 231e 004 3269 4500 ra 5776 1448 Heat Flow Btu hr 1 722e 008 1 931e 008 3 788e 007 3 882e 007 1 414e 007 4 685e 007 2 217e 007 Name P amp _1_Draw PA_1_Return P _2 Draw P _2 Return PA_3 Draw PA_3 Return Ne
152. 7 psia 13 Click the Next button to advance to the Pressure Profile page Figure 2 83 Ni Refluxed Absorber Column Input Expert Condenser Pressure f 9 70 psia Condenser Pressure Drop 9 000 psi Bottom Stage Pressure Pressure Profile page 2 of 4 Cancel 2 Click the Next button to advance to the Optional Estimates page Although HYSYS does not usually require estimates to produce a converged column good estimates result in a faster solution 2 71 Steady State Simulation 3 Specify the following e Condenser 100 F e Top Stage 250 F e Bottom Stage 700 F Figure 2 84 Ni Refluxed Absorber Column Input Expert E4 Optional Condenser Temperature Estimate f 00 0 F Optional Top Stage Temperature Estimate 250 0 F Optional Bottom Stage Temperature Estimate 00 0 F fn Optional Estimates page 3 of 4 Cancel 4 Click the Next button to advance to the fourth and final page of the Input Expert This page allows you to supply values for the default column specifications that HYSYS has created In general a refluxed absorber with a partial condenser has two degrees of freedom for which HYSYS provides two default specifications For the two specifications given overhead Vapour Rate is used as an active specification and Reflux Ratio as an estimate only 5 From the Flow Basis drop down list select Volume All flow specifications are provided in barrels per day 2 2 Refining Tu
153. 850 0 500 0 0 0000 0 0000 Synthesis Gas 1 0000 750 0 500 0 1260 4 088e 007 Shilt2 Lig 0 0000 750 0 500 0 0 0000 Mass Flow lb hr 0 0000 1 666e 004 0 0000 1 666e 004 0 0000 1 666e 004 Liquid Volume Flow barrel day Heat Flow Btu hr Name Material Streams Compositions 0 0000 0 0000 xx New xx Energy Streams 2447 4 088e 007 Unit Ops 0 0000 0 0000 2590 4 823e 007 0 0000 0 0000 2620 4 951e 007 ooo 0 0000 0 0000 Synthesis Gas Production C2170 Gas Production C2 17 Compositions Tab Name Natural Gas Reformer Stean Air Comb Steam Combustor Feer Reformer Lig Mid Combust a Comp Mole Frac Methane 1 0000 0 0000 0 0000 0 0000 0 0600 0 0600 0 0000 Comp Mole Frac H20 0 0000 1 0000 0 0000 1 0000 0 3200 0 3200 0 2518 Comp Mole Frac CO 0 0000 0 0000 0 0000 0 0000 0 0800 0 0800 0 0770 Comp Mole Frac C02 0 0000 0 0000 0 0000 0 0000 0 0600 0 0600 0 0817 Comp Mole Frac Hydrogen 0 0000 0 0000 0 0000 0 0000 0 4800 0 4800 0 5222 Comp Mole Frac Nitrogen 0 0000 0 0000 0 7900 0 0000 0 0000 0 0000 0 0672 Comp Mole Frac Oxygen 0 0000 0 0000 0 2100 0 0000 0 0000 0 0000 0 0000 Name Mid Lig Shift Feed Mid Com Lig Shift2 Feed Shift Liq Synthesis Gas Shift2 Lig Comp Mole F
154. A Onne volun ave emere Temperature C MOIS aChOnsscntne Pressure kPa 101 3250 101 3250 101 3250 stream FromFerm the Mole Fractions will not add up to Molar Flow kgmole hr 2400 a 1 00 Click the Normalize Mass Flow kg hr o T aoo button and the total Mole Comp Mole Frac Ethanol 0 0000 0 0269 0 0000 Comp Mole Frac H20 1 0000 0 9464 1 0000 Comp Mole Frac C02 0 0000 0 0266 0 0000 Comp Mole Frac Methanol 0 0000 2 693e 05 0 0000 Comp Mole Frac Acetic Acid 0 0000 3 326e 06 0 0000 Comp Mole Frac 1 Propanol 0 0000 9 077e 06 0 0000 Comp Mole Frac 2 Propanol 0 0000 9 096e 06 0 0000 Comp Mole Frac 1 Butanol 0 0000 6 578e 06 0 0000 Comp Mole Frac 3 M 1 C4ol 0 0000 2 148e 05 0 0000 Comp Mole Frac 2 Pentanol 0 0000 5 426e 06 0 0000 Comp Mole Frac Glycerol 0 0000 6 64e 06 0 0000 Fraction will equal 1 00 C1 6 Ethanol Plant C1 7 1 3 2 Installing Equipment CO2 Vent Separator The CO2Vent Separator separates the products from the fermentor The bottom liquid of the separator is sent to the distillation section of the plant Concentrator Tower while the overhead vapour goes to the CO2Wash Tower Install a Separator and make the connections shown below SEPARATOR CO2 Vent Tab Page Vapour Outlet To CO2Wash Oe Wash Tower Water is used to strip any Ethanol entrained in the off gas mixture thus producing an overhead of essentially pure CO The bottom product from the tower is recycled t
155. CFD Access Mode No Transfer No Transfer No Transfer LiquidProd Liquid Production View DataBook barrel day No Transfer You will access this table again later to demonstrate how its results are updated whenever a flowsheet change is made 6 For now click the Minimize button in the upper right corner of the Key Variables Data view HYSYS reduces the view to an icon and places it at the bottom of the Desktop Using the Data Recorder In this section you will use the Data Recorder to automatically record the current values of the key variables before making any changes to the flowsheet Gas Processing Tutorial 83 Processing Tutorial 1 83 1 From the Tools menu select Databook 2 Click the Data Recorder tab Figure 1 108 DataBook Available Scenarios Data Recorder Data Selectiorr Current Scenario Variable Include LTS Vessel Temperature X SalesDP DewPoint SalesGas Sales Gas Production LiquidProd Liquid Production ie Table C Graph WIEY Variables Process Data Tables Strip Charts Data Recorder Case Studies When using the Data Recorder you first must create a Scenario containing one or more of the key variables then record the variables in their current state 3 In the Available Scenarios group click the Add button HYSYS creates a new scenario with the default name Scenario 1 4 Inthe table activa
156. Change the following default specifications by selecting the specification in the table and clicking the View button Change the Flow Basis from Specification Flow Basis Spec Type Spec Value Molar to Volume before Kero_SS Prod Flow Volume fo 9300 barrel day entering values Diesel_SS Prod Flow Volume ff 1 925e 04 barrel day AGO_SS Prod Flow Volume fo 4500 barrel day PA_1_Rate Pa Volume fo 5 000e 04 barrel day PA1_Duty Pa Duy 5 5006 07 Btu hr Paz paye om e5007 Bu PALS Ratele voume 80006 04barelday Paa baye om esou Naptha Prod Rate voume 23000104 barelday R1 15 RG Steady State Simulation Steady State Simulation 4 On the Specs page of the Design tab add a new specification by clicking the Add button in Column Specifications group 5 Select Column Liquid Flow from the list of available specifications Complete this specification as shown here This is an Overflash specification for the feed stage Figure R1 11 Name 2 _ Main TS Volume Spec Value 3500 00 barrel day Parameters Summary Delete 6 Add anew specification select Column Duty from the list of available specifications 7 Complete the Kero Reb Duty specification as shown below Figure R1 12 Name Kero Reb Duty a0 55 Energy COL1 Spec Value 5e 006 Btu hr Parameters Summary Delete R1 16 Atmospheric Crude Tower RIT Crude Tower R1 17 8 Add anew specification select
157. Current Components Ac Pure_ List select it and click the Remove button or lt Substitute gt press the DELETE key Remove gt Sort List View Component The complete list of non oil components appears in the figure above 14 Close the Component List View and Filters views to return to the Simulation Basis Manager view On the Components tab the Component Lists group now contains the name of the new component list that you created 2 13 Steady State Simulation The Simulation Basis Manager allows you to create modify and otherwise manipulate fluid packages in your simulation case Most of the time as with this example you require only one fluid package for your entire simulation HYSYS displays the current Environment and Mode in the upper right corner of the view Whenever you begin a new case you are automatically placed in the Basis environment where you can choose the property package and non oil components HYSYS has created a fluid package with the default name Basis 1 You can change the name of this fluid package by typing a new name in the Name field at the bottom of the view 2 14 Defining a Fluid Package In the Simulation Basis Manager view your next task is to define a fluid package A fluid package contains the components and property method HYSYS will use in its calculations for a particular flowsheet Depending on what is required a fluid package can also contain
158. Delete Column Environment Run Reset Converged V Update Outlets Ignored 2 Click the Performance tab then select the Column Profiles page to access a more detailed stage summary Figure 1 93 Column DePropanizer Z COL1 Fluid Pkg Basis 1 7 Peng Robinson Performance Reflux Ratio f Reboil Ratio Summary Column Profiles Feeds Products Condenser Plots 1_ Main TS 1 000 7 842 El i Flows Energy C Mas Lig Vol Pressure 2000 Net Liquid Net Yapour MMSCFD 200 0 4 70001 Net Feed Net Draws 2 Main TS 200 6 2 34392 4 74244 3_ Main TS 4 Main TS 5 MainTS 201 1 201 7 202 2 2 29964 2 26845 4 81111 4 69393 4 64965 4 61846 6_ManTS 202 8 5 30777 4 17910 7_ManT 203 3 5 45974 4 67575 18 MainTS 3_MainTS 10_Main TS 203 9 204 4 205 0 5 52799 5 56523 5 58798 4 82773 4 93322 4 95597 0 63202 205 0 Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Converged V Update Outlets Ignored 1 73 1 74 Steady State Simulation Accessing the Column Sub flowsheet When considering the column you might want to focus only on the column sub flowsheet You can do this by entering the column environment 1 Click t
159. Delete Column Environment Run Reset Converged J Update Outlets Ignored Accessing the Column Sub flowsheet When considering the column you might want to focus only on the rk column sub flowsheet You can do this by entering the column environment PFD Icon 1 Click the Column Environment button at the bottom of the property view While inside the column environment you can do an the following e View the column sub flowsheet PFD by clicking the PFD icon Workbook Icon e View a Workbook of the column sub flowsheet objects by clicking the Workbook icon e Access the inside column property view by clicking the Column T Runner icon This property view is essentially the same as the outside or Main Flowsheet property view of the column Column Runner Icon 3 63 tl Enter Parent Simulation Environment Icon 3 64 Steady State Simulation The column sub flowsheet PFD and Workbook appear in the following figures Figure 3 84 PFD Tower COL1 Hk OA PD A To Condenser Reflux Main TS Reactor Prods RebDuty Boilup Lm Reboiler To arctan of X a Default Colour Scheme v Ovhd ap CondDuty Condenser RecyProds Reboiler Glycol H Figure 3 85 Workbook Tower COL1 To Condenser Boilup To Reboiler Ovhd ap Name i O Refus emperature F 1 0000 212 2 1 0000 375 7 0 0000 360 0 1 0000 159 0
160. ENTER In this case 12C3Oxide is the only component in the stream 3 31 3 31 3 32 Steady State Simulation If you want to delete a stream click on the Name cell for the stream then press DELETE HYSYS asks for confirmation of your action 3 32 16 Click the Normalize button to force the other values to zero The composition is now defined for this stream Figure 3 37 Ni Input Composition for Stream Prop Oxide PCS Mole Fraction Composition Basis 2C30 ride Mole Fractions 2 C3diol C Mass Fractions C Liq Yolume Fractions C Mole Flows C Mass Flows C Lig Volume Flows Composition Controls Erase Cancel Total f 0000 OK 17 Click the OK button HYSYS accepts the composition The stream specification is now complete so HYSYS will flash it at the conditions given to determine the remaining properties The values you specified are a different colour blue than the calculated values black Figure 3 38 Workbook Case Main Prop Oxide apour Fraction 0 0000 emperature F 75 00 ressure psia 16 17 Molar Flow Ibmole hr iquid Volume Flow USGPM i 20 83 eat Flow Btu hr 7 804e 006 a a t3 zu o gt Z Material Streams Energy Streams Unit Ops ProductBlock Prop Oxid C Include Sub Flowsheets FeederBlock_Prop Oxide L Show Name Only Number of
161. ESUS cot O o S Mi aseccnnesccnsessccnnsscsnesseanes 16 C2 1 C2 2 Synthesis Gas Production Ce Process Description Figure C2 1 Synthesis 2 Gas Shift1 shit2 KE shift Feed m Feed NA Reactor Mid ON Shift O amp cy 4 as Combust Gambuetar 2 cone SET 1 SET 3 shift Natural tim Combustor Combustor y shift2 Gas Feed a shift2 Lig a Air Q Reformer shift Yt Ba Mid Liq om Reformer i Lig Steam Comb a Shift1 Steam Iq Q Reformer a Lig ADJ 2 Dummy S Stream Sens O SSRatio ADJ 1 The production of synthesis gas is an important part of the overall process of synthesizing ammonia The conversion of natural gas into the feed for the ammonia plant is modeled using three conversion reactions and an equilibrium reaction To facilitate the production of ammonia the molar ratio of hydrogen to nitrogen in the synthesis gas is controlled near 3 1 This ratio represents the stoichiometric amounts of the reactants in the ammonia process In a typical synthesis gas process four reactors are needed This model requires five reactors since the conversion and equilibrium reactions cannot be placed in the same reaction set and thus cannot be placed in the same reactor The Combustor is separated into a conversion reactor and an equilibrium reactor Desulfurized natural gas is the source of hydrogen in this example which is reformed in a conversion reactor Reformer when combined with steam Air is added to the second reacto
162. F Tray 2 lb hr Yap MF Tray Ib hr __1 783e 005_ 2 178e 005 1 813e 005 2 167e 005 1 644e 005 2 156e 005 1 875e 005 2 145e 005 1 908e 005 2 135e 005 Case Study 1 Delete C Graph Re Number Propylene Propane Splitter P1 1 PI Propulene Propane Splitter P1 1 Process DESCHIP MOM ici cicistisciccdeedicccsetiewsisedceatinctcadueereteeeideewaals 3 P12 SEUD oiin ea A aaa a Aa 4 P1 3 Steady State SIMULATION cccceeeeseceeeeseeeeeenseeeeeeeneeeseeeseeeseeees 5 P1 3 1 Staite Simulation N a eaan 5 P1 3 2 Adding the Stripper Reboiled Absorber e 6 P1 3 3 Adding the Rectifier Refluxed Absorber ccccceeees 7 P1 3 4 Adding the Specifications cccccceceseceeeeeeeeeeeeeeeeeeeeeaeees 8 P1 Results cotta T cog MiMenssscenssscenesscnnnssscensseees 10 P1 1 a Propylene 2 Propylene P1 2 Propylene Propane Splitter P1 3 P1 1 Process Description Figure P1 1 Condenser Duty Propene Reboiler Duty Propane A propylene propane splitter is generally an easy column to converge The critical factor in producing good results however is not the ease of solution but the accurate prediction of the relative volatility of the two key components Special consideration was given to these components and others in developing the binary interaction coefficients for the P
163. Flash ap Diesel Steam PreFlash Preheat Crude E AGO Steam 4 Bottom Steam PreFlashLiq T 4 Click to drop the heater onto the PFD HYSYS creates a new heater with a default name E 100 Next you will change the heater icon from its default to one more closely resembling a furnace Refining Tutorial Right click the heater icon The Object Inspect menu appears Select Change Icon from the menu The Select Icon view appears Ni Select Icon E4 7 Click the WireFrameHeater5 icon scroll to the right then click the OK button The new icon appears in the PFD Furnace icon Attaching Streams to the Furnace E 1 Click the Attach icon on the PFD tool bar to enter Attach mode Attach Mode icon 2 Position the cursor over the right end of the PreFlashLig stream icon A small box appears at the cursor tip Figure 2 66 PreFlachV ap At the square connection point a pop up description appears Brea PreFlash attached to the cursor The pop Crude up Out indicates which part of the stream is available for connection in this case the stream outlet as caiga When you are in Attach 3 With the pop up Out visible click and hold the mouse button The Ba ee white box becomes black indicating that you are beginning a return to Move mode click connection eae 30u 4 Drag the cursor toward the left inlet side of the heater A trailing between Att
164. Gas Processing Tutorial 63 Processing Tutorial 1 63 8 Inthe Balance Type group select the Mole radio button Figure 1 78 DewPoint Parameters Balance Type Parameters Mole C Heat C Mass and Heat Mass C Mole and Heat C General Ratio List Not a General Balance No Ratios Required TEn Connections Parameters Worksheet Stripchart User Variables Ignored 9 Click the Worksheet tab The vapour fraction and pressure of SalesDP can now be specified and HYSYS will perform a flash calculation to determine the unknown temperature 10 In the SalesDP column Vapour cell enter 1 0 11 In the Pressure cell enter 800 psia HYSYS flashes the stream at these conditions returning a dew point Temperature of 5 27 F which is well within the pipeline specification of 15 F Figure 1 79 DewPoint SalesDP apour 1 0000 1 0000 _ emperature F 50 00 9 9880 Worksheet Conditions j Properties Composition T Connections Parameters Worksheet Stripchart User Variables ressure psia 570 0 800 0 7 018 7 018 td Ideal Lig Yol Flow barrel day 1 562e 004 3167 3 475e 004 1 562e 004 3167 3 560e 004 Molar Entropy Btu Ibmole F Heat Flow Btu hr 36 90 2 678e 007 34 63 2 744e 007 O z lt oaj a g m njn ojo y ME ZSS m gt s mn F 2 3 2 KJ Delete Ignored
165. HYSYS interface see Chapter 1 Interface in the User Guide A 3 a n The tutorials start in Steady State mode and end in Dynamic mode Once you have completed one or more tutorials you may want to examine the Applications section for other examples that may be of interest A 4 Get Started You are now ready to begin building a HYSYS simulation so proceed to the Tutorial of your choice Samples Case Name Tutorial Chapter Steady State Dynamic Gas Processing Chapter 1 TUTOR1 HSC dyntut1 hsc Chapter 2 TUTOR2 HSC Chemicals Chapter 3 TUTOR3 HSC Gas Processing Tutorial 1 1 Gas Processing Tutorial Wet TATROGUGCIION occtincccesteicccs a a a a SE 3 1 2 Steady State Simulation nnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnn e 4 1 2 1 Process Descriptions Os o oeoa 4 1 2 2 Setting Your Session Preferences cccseeeeeeceseeeeeeeeeeeeeeens 6 1 2 3 Building We Simulation CA 10 1 2 4 Entering the Simulation Environment c cccccceseeeeeeeeee 18 1 2 5 4s8ing the Workbook ggiesccccecees M aaaea aana 20 1 2 6 Installing Unit Operations ccceccccceeeeeeeeeeeeseeeeeeeeseenaaees 34 1 2 7 Using Workbook Features cccccceeeeeceeceeseeeeeeaeeeeeeesaeeees 45 t 2 8 Using the REDRE _ 2 49 1 2 9 Viewing and Analyzing Results ceeeeeeeeeeeeeeeeneeeeeeeeeeaes 76 1 2 10 Optional SWAT Maana 87 1 3 Dynam
166. Iv v Distillate Rate lt empty gt lt empty gt lt empty gt L Iv L Reflux Rate lt empty gt lt empty gt lt empty gt D v E Btms Prod Rate lt empty gt lt empty gt lt empty gt E M L View Add Spec f Update Inactive Degrees of Freedom 0 Design Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged J Update Outlets Ignored 3 61 3 62 Steady State Simulation HYSYS automatically made The Degrees of Freedom has returned to zero so the column is ready to the new specification Active be calculated when you created it Running the Column 1 Click the Run button to begin calculations and the information displayed on the page is updated with each iteration The column converges quickly in five iterations Figure 3 82 L Column Tower COL1 Fluid Pkg Basis 1 UNIQUAC Ideal Design Optional Checks Profile F A i View Initial Estimates Connections Monitor Heat Spec r oe 1 0000 0 050935 0 224420 Press 1 0000 0 031171 0 070670 C Flows Specs Summary 0 2500 0 002362 0 013733 0 0001 0 000085 0 002672 Subcooling 1 0000 0 000003 0 000496 Notes Tempe rati re us Tray Pos thos trom Top Temp Specifications Estimate Current Ovhd Yap Rate 0 0000 Ibmole hr 1 66e 005 0 0000 Reflux Ratio 1 000 1 00 0 0000 H20 Fraction 5 000e 003 5 01e 003 0 0
167. M D86 Cut Pt 2 00 Navigator Scope ASTM D2897 ASTM D1160 Atr ASTM D1160 Vac ASTM D93 Flash P ASTM D97 Pour Pt Cetane Index Critical Pressure Cut Pt 3 50 Cut Pt 5 00 Cut Pt 7 50 Cut Pt 10 00 Cut Pt 12 50 Cut Pt 15 00 Cut Pt 17 50 Cut Pt 20 00 Object Filter All f Loe C Cold C Envelope C Hydrate fC Flowsheet Critical Temperatur C Case D86 Crack Reduce C Basis Mass Density Utility Mole Weight Cut Pt 35 00 Napthene Mole Cut Pt 40 00 Paraffin Mole x Cut Pt 45 00 Pik PLEN NNS ASTM 1160 Vac 5 Residue Cancel Cut Pt 25 00 Cut Pt 30 00 Rofractiva Indov Variable Description 18 The completed Variables tab of the Databook appears below Figure 2 136 DataBook Available Data Entries Object Variable Atmos Tower Reflux Ratio Trim Duty Trim Duty Residue BP Curves ASTM 1160 Vac 5 Residue ar Variables Process Data Tables Strip Charts Data Recorder Case Studies 2 107 Steady State Simulation Create a Data Table Now that the key variables to the Databook have been added the next task is to create a data table to display those variables 1 Click on the Process Data Tables tab 2 Click the Add button in the Available Process Data Tables group HYSYS creates a new table with the default name ProcDatal DataBook Iof x Available Process Data Tables Individual Process Data Selection ProcDatal
168. Main Environment The Raw Crude stream has been installed RAO Steady State Simulation Steady State Simulation R1 10 AL 3 Steady State Simulation The following major steps will be taken to set up this case in steady state 1 Simulate the Pre Fractionation Train This determines the feed to the atmospheric fractionator and includes the pre flash separation crude furnace and mixer which recombines the pre flash vapour and furnace outlet stream 2 Install the Atmospheric Crude Fractionator Add the column steam inlets to the flowsheet and install the crude fractionator using the rigorous distillation column operation Al 3 1 Simulate the Pre Fractionation Train Inlet Stream Specify the Inlet stream Raw Crude as shown below Stream Raw Crude Temperature F 450 0 F Pressure psia 75 0 psia Std Ideal Liq Vol Flow barrel day 100 000 barrel day Because the composition has been transferred from the Oil Characterization the stream is automatically flashed Atmospheric Crude Tower Pre Flash Operations Install the Separator Heater and Mixer and provide the information displayed below Separator PreFlash Tab Page In this cell Enter ii PreFlash Liq Heater Crude Heater Design Connections PreFlash Liq Mixer Mixer DEE in this cell Enterse O Design Connections Inlets Hot Crude PreFlash Vap The calculated specifications for the Pre Fractionation Atm Feed stream ap
169. New Streams upon Creation Iv Confirm Deletes Use Modal Property Views J Confirm Mode Switches Naming V Record Time When Notes Are Modified J Enable Single Click Actions Tool Tips Enable Cross Hairs On PFD V Enable Cell Edit Button Dynamics Errors Desktop Performance Display Errors in Trace Window Licensing Display Numerical Errors in Trace Window Ignore Them in Dynamics Mode RTI Server Show Property Package Warning Column J Show Property Package Warning Status Window Property Correlations Trace Window V Activate Standard Property Correlations M Confirm Before Adding if Active Correlations are Present Simulation Reports Resources Extensions j Oillnput Tray Sizing Save Preference Set Load Preference Set 6 In the Assistant group uncheck both the Perform checks when switching to dynamics or starting the integrator and the Set dynamic stream specifications in the background checkboxes Figure 1 129 Session Preferences H SYS PRF Simulation Assistant Set dynamic stream specifications in the background Options Desktop Controller Options Naming J Trace controller alarm messages Tool Tips Dynamics Pressure Flow Solver Pafomiances Ignore convergence failures up to five consecutive times Licensing Numerical errors will be ignored if sent to the trace window RTI Server Column Status Window Other Delete internal sub flo
170. P The fluid package contains a total of 44 components e 6 library pure components H2O plus five Light Ends components e 938 petroleum hypocomponents The new fluid package is assigned by default to the Main Flowsheet as shown in the Flowsheet Fluid Pkg Associations group Next you will install streams and operations in the Main Simulation environment Refining Tutorial 2 37 2 2 4 Entering the Simulation Environment 1 To leave the Basis environment and enter the Simulation environment do one of the following e Click the Enter Simulation Environment button on the Ok Simulation Basis Manager view e Click the Simulation Environment icon Simulation Environment icon When you enter the Simulation Environment the initial view that appears depends on your current preference setting for the Initial Build Home View Three initial views are available PFD Workbook and Summary Any or all of these can be displayed at any time however when you first enter the Simulation Environment only one appears For this example the initial Home View is the Workbook HYSYS default setting Figure 2 38 pd tut2 hsc HYSYS File Edit Simulation Flowsheet Workbook Tools Window Help PAX Osi Taag lt Kew ay oe Sed _ i amie Workbook Case Main New apour Fraction emperature F ressure psia Molar Flow Ibmole hr Mass Flow lb hr lt empty gt iquid Yolume Flow barrel day lt empty gt eat Flow Bt
171. PFD window by clicking the zoom buttons at the bottom left corner of the PFD view Some of these functions are illustrated here for more information see Chapter 7 25 PFD in the User Guide Calculation Status Before proceeding you will examine a feature of the PFD that allows you to trace the calculation status of the objects in your flowsheet If you recall the status indicator at the bottom of the property view for a stream or operation displays one of three possible states for the object Status Description Red Status A major piece of defining information is missing from the object For example a feed or product stream is not attached to a separator The status indicator is red and an appropriate warning message appears Yellow Status All major defining information is present but the stream or operation has not been solved because one or more degrees of freedom is present for example a cooler where the outlet stream temperature is unknown The status indicator is yellow and an appropriate warning message appears The stream or operation is completely defined and solved The status indicator is green and an OK message appears When you are in the PFD the streams and operations are colour coded to indicate their calculation status The inlet separator is completely calculated so its normal colours appear While installing the remaining operations through the PFD their colours and status changes appropriately a
172. PM i 22 01 z o Q T 5 gt o T z3 emperature F ressure psia Molar Flow Ibmole hr Name Material Steams PLT Flow FeederBlock Prop Oxide L Include Sub Flowsheets MIx 100 _ Show Name Only Number of Hidden Objects 12 Save the case 3 45 Steady State Simulation 3 2 7 Installing Equipment on the PFO 5 Besides the Workbook the PFD is the other main view in HYSYS you will use to build the simulation PFD Icon To open the PFD click the PFD icon on the toolbar The PFD item appears in the HYSYS menu bar whenever the PFD has focus When you open the PFD view it appears similar to the one shown below Figure 3 58 PFD Case Main of X Hi te HI 4 Kei p A D Default Colour Scheme x Like any other non modal As a graphical representation of your flowsheet the PFD shows the view the PFD view can be connections among all streams and operations also known as objects eee Seng ae Each object is represented by a symbol also known as an icon A dragging anywhere on the i ie outside border stream icon is an arrow pointing in the direction of flow while an operation icon is a graphic representing the actual physical operation The object name also known as a label appears near each icon The PFD shown above has been rearranged by moving the Prop Oxide feed stream icon up slightly so it does not overlap the Water Feed stream i
173. Percent Level Connections Process Object Process Variable Output Variable VLV 102 Parameters Configuration 0 PVmax 100 Action Mode O Direct Auto 50 J X oj U G1 28 Acid Gas Sweetening with DEA 129 Gas Sweetening with DEA G1 29 Level Controller Name Cond LC COL2 Tab Page Connections Process Object Condenser COL2 Process Variable Liquid Percent Level Output Variable Reflux To size the Control Valve for the Reflux stream select the Control Valve button FCV for Reflux Flow Type Mass Flow Min Available 0 0 Ib hr Max Available 5512 lb hr Parameters Configuration i G1 29 Dynamic Simulation Temperature Controllers Temperature Controller Name TIC 100 Tab Pagel inthis cele Connections Process Object DEA TO PUMP Process Variable Temperature Output Variable COOLER Q To size the Control Valve for the Cooler Duty stream select the Control Valve button To filter high frequency disturbances click the Parameter tab select the PV Conditioning page and change the First Order Time Constant from 15 to 50 0 0 Btu hr Parameters Configuration Ti 10 Connections Process Object Main TS Process Variable Stage Temperature Variable Specifics 18_Main TS Output Variable RBLR Q To size the Control Valve for the Reboiler Duty stream select the Control Valve button FCV for RBLR Q Flow Type Min Available 0 Btu hr Max Available 1 9e7 Btu hr Parameters Configuration
174. Preheat Crude column click in the Temperature cell and type 450 HYSYS displays the default units for temperature in this case E Figure 2 40 Workbook Case Main Preheat Crude Vapour Fraction lt empty gt 450 F z Pressure psia lt empty gt 3 Since this is the correct unit press the ENTER key HYSYS accepts the temperature HYSYS advances to the Pressure cell If you know the stream pressure in another unit besides the default of psia HYSYS will accept your input in any one of a number of different units and automatically convert the value to the default For example the pressure of Preheat Crude is 5 171 bar but the default units are psia 4 Inthe Pressure cell type 5 171 5 Press SPACEBAR The field containing the active cell units becomes active 6 Begin typing bar The field opens a drop down list and scrolls to the unit s most closely matching your input Figure 2 41 Workbook Case Main Temperature F Pressure psia 7 Once bar is selected press the ENTER key HYSYS accepts the pressure and automatically converts to the default unit psia 8 Click in the Liquid Volume Flow cell then type 1e5 The stream flow is entered on a volumetric basis in this case 100 000 bbl day 9 Press the ENTER key Refining Tutorial 2 41 The stream is now completely defined so HYSYS flashes it at the conditions given to determine the remaining
175. Processing Tutorial 1 123 19 In the Column sub flowsheet add a PID Controller operation that will serve as the Condenser level controller Specify the following details Tab Page In this cell Enter Connections Name CondLG o LC Source Percent Level 20 Click the Control Valve button The FCV for Reflux view appears 21 Enter the following details in the Valve Sizing group In this cell Enter Flow Type Molar Flow 22 Close the FCV for Reflux view 23 Click the Face Plate button Change the controller mode to Auto on the face plate view then close the view 24 Close the Cond LC controller view 25 Add another PID Controller operation that will serve as the Reboiler level controller Specify the following details Tab Page In this cell Enter Process Variable Reboiler Liq Percent Source Level Output Target Object RebDuty eooo o O m fme 1 123 1 124 Dynamic Simulation The values shown here do not use the default units Enter the values then select the correct units from the drop down list HYSYS automatically converts the values to the default units t Enter Parent Simulation Environment icon PID Controller icon 1 124 26 Click the Control Valve button The FVC for RebDuty view appears 27 In the Duty Source group select the Direct Q radio if it is not already selected 28 In the Direct Q group enter the following values In
176. Prop Oxide If you know the stream pressure in another unit besides the default of psia HYSYS will accept your input in any one of a number of different units and automatically convert to the default for you For example you know the pressure of Prop Oxide is 1 1 atm 8 Type 1 1 9 Press the SPACEBAR or click on J Begin typing atm HYSYS will match your input to locate the unit of your choice Figure 3 35 Workbook Case Main Prop Oxide Name Cd lt empty gt Temperature F 75 00 psi 41 100 lt empty gt f lt empty gt Liquid Volume Flow USGPM lt empty gt lt empty gt _ Material Streams Compositions Energ 2 D ProductBlock Prop Oxid C Include Sub Flowsheets FeederBlock_Prop Oxide L Show Name Only Number of Hidden Objects 0 3 29 Steady State Simulation 10 Once atm is selected in the list press the ENTER key and HYSYS accepts the pressure and automatically converts to the default unit psia Alternatively you can specify the unit simply by selecting it from the unit drop down list 11 Click in the Molar Flow cell for Prop Oxide enter 150 Ibmole hr then press ENTER Providing Compositional Input Now that the stream conditions have been specified your next task is to input the composition 12 In the Workbook double click the Molar Flow cell of the Prop Oxide stream The Input Composition for Stream view appears This view al
177. Property Balance Utility Property Table enecesesoleoesoeeWecosessseoesosesossossosscoseeossoseooee User Property fiew Utility Add Utility 2 119 Dynamic Simulation 3 Select Tray Sizing then click the Add Utility button The Tray Sizing view appears Tray Sizing Tray Sizing 1 Design Name Tray S ection Sunni Tray Sizing 1 Select TS Setup Specs Setup Sections a Mode O Limiting Stage ha Notes Liquid Draw 0 00 Use Tray Vapour to Size Ask Each Time a _ Design Dynamics eee ioo 4 Inthe Name field change the name to Main TS 5 Click the Select TS button The Select Tray Section view appears Figure 2 154 Select Tray Section E3 Flowsheet Object COL1 Object Fiter All C Streams C UnitOps C Logicals C ColumnOps C Custom L 6 In the Flowsheet list select T 100 then select Main TS in the Object list Click the OK button 7 Inthe Use Tray Vapour to Size drop down list select Always Yes 2 120 Refining Tutorial 8 Click the AutoSection button The AutoSection view appears The default tray internal types appear as follows Auto Section Information Internal Type C Sieve Valve C BubbleCap Packed Area Tolerance When the ratio between the curent calc d area and either of min max previous areas for the 0 6000 section exceeds this tolerance a new diameter section is started Hi
178. RT ES oroe An Energy stream could be attached to heat or cool the vessel contents For this tutorial however the energy stream is not required Gas Processing Tutorial 1 41 The Volume Hawd volum 12 Select the Parameters page The current default values for Delta P and Liquid Level default Volume Liquid Volume and Liquid Level are acceptable values generally apply only to vessels operating in dynamic mode or with reactions attached Figure 1 48 InletSep Design Connections Delta P Parameters 0 0000 psi User Variables Notes Liquid Volume Separator C 3 Phase Sep C Tank Design Reactions Worksheet Dynamics Delete EET ES Gro 13 To view the calculated outlet stream data click the Worksheet tab then select the Conditions page The table appearing on this page is shown below Figure 1 49 Name ooo 0 8976 2 775e 004 2 318e 004 4995 4342 3 807e 004 3 657e 004 35 66 25 87 36 7 4 180e 007 5 756e 006 3 605e 007 14 When finished click the Close icon to close the separator property view 1 41 1 Heat Exchanger Icon 1 42 Steady State Simulation Installing the Heat Exchanger Next you will install is the gas gas exchanger 1 Ensure that the Object Palette is visible if not press F4 2 On the Object Palette double click the Heat Exchanger icon The Heat Exchanger property view appears The C
179. Rate specification Click the Add button The Add Specs view appears 6 Select Column Draw Rate and click the Add Spec s button The Draw Spec property view appears 7 Inthe Name cell type WasteH2O Rate No further information is required as this specification is de activated and only estimated when you run the column Figure 2 87 Si Draw Spec WasteH20 Rate il x Name Draw gt lt lt Stream gt gt p Volume lt empty gt Parameters Summary Delete Refining Tutorial 8 Close the view The new specification appears in the Column Specifications group The Degrees of Freedom is now zero 9 Select the Connections page See Figure 2 86 The Connections page is similar to the first page of the Input Expert Currently the column is a standard type so this page shows a column schematic with the names of the attached streams When the side equipment is added to the column the page becomes non standard There are a large number of possible non standard columns based on the types and numbers of side operations that are added Therefore HYSYS modifies the Connections page into a tabular format rather than a schematic format whenever a column becomes non standard In the next section you will add the side equipment and observe how the Connections page is modified Installing the Side Strippers 1 Click the Side Ops tab of the Column property view Figure 2 88 L Column Atmos Tower COL1 Flu
180. Ratio Basis Perf PO tal en ae Ratio Flows Energy C Molar Mass Summary eboil Ratio 0 6324 Feeds Products F psia barrel da barrel da barrel da barrel da Condenser Plot Condenser 19 70 15463 7 I iii 267 1 28 70 97371 2 39243 3 311 2 28 84 62466 0 711493 334 9 28 99 65916 2 986245 6 346 1 23 13 66493 5 9695 8 353 8 29 27 66092 3 90273 1 360 7 29 41 65089 9 89871 9 368 0 29 56 63483 0 88869 4 376 8 29 70 61230 4 87262 6 387 5 29 84 44316 1 83715 9 401 2 29 99 425745 81096 1 412 8 30 13 41413 3 79354 6 422 0 30 27 40382 0 78193 4 3 MainTS 429 4 30 41 39117 8 77162 0 4__MainTS 436 2 30 56 37153 1 79897 8 5 Main TS 444 0 30 70 334937 739331 6_Main TS 455 7 30 84 782295 702737 7_Main TS 485 9 30 99 26157 4 821093 8 522 2 31 13 225198 79733 3 541 6 31 27 20331 8 760957 551 6 31 41 183236 733907 7 558 1 31 56 54614 3 718993 5 600 9 31 70 18660 5 66762 6 626 9 31 84 16370 8 741475 4__Main TS 637 8 31 99 13858 8 719857 8 5_MainTS 644 4 32 13 11644 2 69345 8 26_Main TS 649 3 3227 9171 81 67131 2 27__Main TS 654 2 32 41 3500 64 654658 8 Am a rT ere AA Pe MOI A ran gt Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dy
181. Ratio with the following new ones e Overflash specification for the feed stage Tray Net Liquid Flow specification e Kerosene side stripper reboiler duty specification 2 84 Si Add Specs Atmos Tow EG Column Specification Types Column Cold Properties Spec a Column Component Flow Column Component Fraction Column Component Ratio Column Component Recovery Column Cut Point Column Draw Rate Column DT Heater Cooler Spec Column Dt Spec Column Duty Column Duty Ratio Column Feed Ratio Column Physical Properties Spec Column Pump Around Column Reboil Ratio Spec Column Recovery Column Reflux Feed Ratio Spec Column Reflux Fraction Spec fad Add Spec s Refining Tutorial Adding the Overflash Specification 1 On the Design tab move to the Specs page Figure 2 104 O x Column Atmos Tower COL1 Fluid Pkg Basis 1 Peng Robinson Dea Column Specifications Specification Details Distillate Rate Vi ctive jew Connections Vap Prod Rate Spec Name WasteH 20 Rate ire fe Monitor Reflux Ratio Add Converged No Curent Specs FS ate C Delete Dry Flow Basis KeroSS Prod Flow Spec Type KeroSS BoilUp Ratio Specs Summary DieselSS Prod Flow Subcooling Fixed Ranged Spec Fixed Notes Primary Alternate Spec Primary Update Specs from Dynamics Values Specif
182. Reactor Prods 1 Prods Water Water Feed YLy Water Feed Feed 1 Coolant 16 Save the case as DynTUT3 2 hsc Enter Basis Environment icon The Simulation Basis Manager allows you to create modify and otherwise manipulate Fluid Packages in the simulation case 3 82 Dynamic Simulation 3 3 3 Modeling a CSTR Open to the Atmosphere The CSTR reactor is open to the atmosphere and the liquid level of the reactor can change in dynamic mode This means that the vapour space in the liquid reactor also varies with the changing liquid level In order to model this effect the Reactor Vent stream was set with a constant pressure specification However one additional modification to the Reactor Vent stream is required Since the liquid level in the CSTR can move up and down regular and reverse flow can be expected in the Reactor Vent stream When vapour exits the reactor vessel regular flow the composition of the Reactor Vent stream is calculated from the existing vapour in the vessel When vapour enters the vessel reverse flow the composition of the vapour stream from the atmosphere must be defined by the Product Block attached to the Reactor Vent stream It is therefore necessary to specify the Product Block composition The original steady state Chemicals tutorial used a Fluid Package which did not include any inert gases Therefore it is now necessary to return to the Simulation Basis Manager and add the
183. Reactor has one degree of freedom At this point either the outlet stream temperature or the cooling duty can be specified For this example you will specify the outlet temperature Initially the Reactor is assumed to be operating at isothermal conditions therefore the outlet temperature is equivalent to the feed temperature 75 F 12 In the Reactor Prods column click in the Temperature cell Type 75 then press ENTER HYSYS solves the Reactor Figure 3 69 Reactor Set 1 Worksheet Name Mixer Out Reactor Prods Reactor Yent Coolant ar Vapour 0 0000 0 0000 lt empty gt Conditions Temperature F 75 00 L any 00 lt empty gt Properties Pressure psia 16 17 16 17 L lt empty gt Molar Flow Ibmole hr 7606 700 2 lt empty gt Mass Flow lb hr 1 971e 004 1 971e 004 lt empty gt PF Specs Std Ideal Liq Vol Flow USGPM 42 84 41 10 0 0000 lt empty gt Molar Enthalpy Btu lbmole 1 086e 005 1 214e 005 5 030e 004 lt empty gt Molar Entropy Btu lbmole F 0 8824 0 6769 20 68 lt empty gt Heat Flow Btu hr 8 262e 007 8 499e 007 0 0000 2 372e 006 Composition Design Reactions Rating Worksheet Delete EE ooe There is no phase change in the Reactor under isothermal conditions since the flow of the vapour product stream Reactor Vent is zero In addition the required cooling duty has been calculated and is represented
184. SYS automatically created Column sub flowsheet streams with the same names For example when Bottom Steam was attached as a column feed stream HYSYS created an identical sub flowsheet stream named Bottom Steam In the Inlet Streams table on the Connections page the Main Flowsheet stream is the External Stream while the sub flowsheet stream is the Internal Stream Figure 2 103 Inlet Streams Internal Stream Split Bottom Steam 29 MainTS P H Flash Tower Feed TowerFeed 28 MainTS P H Flash Trim Duty Trim Duty 28 MainTS None Req d KeroSS_Energy lt lt Stream gt gt KeroSS_Reb None Reqd Diesel Steam Diesel Steam 3__DieselSS P H Flash AGO Steam AGO Steam 3 _AGOSS P H Flash If you scroll down the list of Inlet Streams notice that the two side stripper steam streams DieselSteam and AGOSteam are Internal and External meaning that these streams are attached to the Main Flowsheet streams that were created earlier For the purposes of this tutorial it is not required to export the pump around duty streams PA_1_Q PA_2_Q and PA_3_Q to the Main Flowsheet so their External Stream cells remain undefined Adding Column Specifications Select the Monitor page of the Column property view The current Degrees of Freedom is zero indicating the column is ready to be run Before you run the column however you will have to replace two of the active specifications Waste H20 Rate and KeroSS BoilUp
185. SYS provides the equilibrium data and all other pertinent information for the reaction C2 7 C2 8 In the table of reaction sets RXN 1 and RXN 2 appear in both the first and second reaction sets Add Set to Fluid Package C2 8 Setup Defining Reaction Sets In HYSYS each reactor operation may have only one reaction set attached to it however a reaction may appear in multiple reaction sets In this case you only have to provide three reaction sets for all five reactors In the Reaction Sets group click the Add Set button to add new reaction sets Define the following reactions sets Select the following reactions in the Active List group as indicated Reaction Set Name Active Reactions Reformer Rxn Set Rxn 1 Rxn 2 Combustor Rxn Set Rxn 1 Rxn 2 Rxn 3 Shift Rxn Set Figure C2 3 Simulation Basis Manager Rxn Components Reactions Reaction Sets View Ren Global Asn Set View Set Reformer Rxn Set Combustor Rxn Set Add Set Mai Shift Ren Set roots Delete Asn Delete Set Copy Set CoR Assoc Fluid Pkgs Import Set Export Set Alea Add to FP Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment Attaching Reaction Sets to the Fluid Package 1 On the Reactions tab of the Simulation Basis Manager select a Reaction Set then click the Add to FP button The Add view ap
186. Setup view This view allows you to customize how the data appears on the Strip Chart Close the Logger Setup view 14 Click the Strip Chart button in the View group to display the DataLoggerl strip chart You are now ready to begin dynamics calculations The DataLogger1 view should be visible 2 143 Start Integrator Icon To view a legend for the variables right click anywhere in the DataLogger window and select Legend from the menu that appears 2 144 Dynamic Simulation 15 16 18 Start the Integrator by clicking the Start Integrator Icon If you get a warning notice regarding the dynamics assistant click the No button Observe as the variables line out in the DataLogger1 view Move the cursor over the lines in the graph to view the variable label Maximize the DataLogger1 view if required Click the Stop Integrator icon when you want to stop the simulation Perform an analysis by manipulating design variables and using the Databook tools to observe the response of other variables Chemicals Tutorial 3 1 5 Chemicals Tutorial 31 RTRFOGUCTION Ssiticshaceiceis plea aa a aa a a aaa 3 3 2 Steady State Simulation vaio cciecseseiceedestisvescievn doce tesceecedgetervanereedlies 4 3 2 1 Process DeSCriptiQ de Mitta 2 cccccsetlicsecescsscesscesseseeees 4 3 2 2 Setting Your Session Preferences cccceeeeccceeeeeeeeeeeeeeeees 5 3 2 3 Defining the Fluid Package ccccsscccc
187. Sl Unit Set Name Field Display Units Tray Sizing Save Preference Set Load Preference Set 5 Click the Clone button A new unit set named NewUser appears and is automatically selected as the current unit set 6 Inthe Unit Set Name field rename the new unit set to Field density You can now change the units for any variable associated with this new unit set 7 Inthe Display Units group use the vertical scroll bar to find the Standard Density cell The current default unit for Standard Density is lb ft3 A more appropriate unit for this example is API_60 Click in the Standard Density cell on lb ft3 Press SPACEBAR or click the down arrow to open the drop down list of available units Refining Tutorial 2 9 10 In the unit list select API_60 Figure 2 7 Session Preferences D HY SYS hysys PRF l Available Unit Sets Units Field13 Field density Formats HoverT extUnitS et HoverT extUnitSet2 Unit Set Name Field density ew Users Display Units Variables Molar Volume l __ft3 lbmole Ht Tran Coeff Btu hr ft2 F S Large Heat Flow MMBtu hr D Standard Densit Mass Entropy g cm3 g mL elete SG_60 60api a SG_60 60nb Simulation Variables Reports SG 15 4 t Tray Sizing 11 Repeat steps 8 10 to change the Mass Density units to API Figure 2 8 Session Preferences D HYSYS hysys PRF E Oj x TETEE Available Uni
188. Specific Click the OK button 5 Repeat step 4 to add the Propane Variable Specific For illustration purposes the two remaining components will be added later using an alternative import method HYSYS assigned the imported variables to Spreadsheet cells Al through A3 by default 6 Change the cell locations to B3 through B5 as shown in the following figure the reason for doing so will become apparent on the Spreadsheet tab Figure 1 117 Imported Variables Variable Description Edit Import SalesGas Comp Mole Frac Methane SalesGas Comp Mole Frac Ethane SalesGas _____ Comp Mole Frac Propane Add Import Delete Import 1 89 Steady State Simulation 7 No information is required on the Parameters and Formulas tabs so click the Spreadsheet tab The HYSYS Spreadsheet 8 Enter the column headings as shown in the table below You can behaves similarly to move to a cell by clicking it or by pressing the arrow keys commercial spreadsheet packages you enter data and formulas in the cells and Column Row Heading calculated results are Component lance A1 Component B1 Mole Fraction Comp Heat Value Total Heat Value 9 Enter the components in the Component column as shown as shown in the table below Row Component 10 Enter the component net heating values in the Comp Heat Value column as shown in the figure below Figure 1 118 i Heating Yalue Current C
189. TS in this case stage 15 indicated by 15_Main TS However the feed stream needs to enter stage 28 5 Inthe Optional Inlet Streams group click in the Inlet Stage cell for TowerFeed 6 Type 28 and press ENTER or select 28_Main TS from the drop down list of stages 7 Click on lt lt Stream gt gt in the same table which was automatically advanced down one cell when you attached the Tower Feed stream 8 From the Stream drop down list select the Trim Duty stream which is also fed to stage 28 Figure 2 79 Tower Feed Trim Duty 9 Advance to the Bottom Stage Inlet field by clicking on it or by pressing TAB Refining Tutorial 10 In the Bottom Stage Inlet field click the down arrow 7 to open the drop down list of available feeds 11 From the list select Bottom Steam as the bottom feed for the column Entering Outlet Streams In the Condenser group of the Input Expert view the default condenser type is Partial To the right of this group there are two Overhead Outlets vapour and liquid In this case the overhead vapour stream has no flow and two liquid phases hydrocarbon and water are present in the condenser The hydrocarbon liquid product is attached in the liquid Overhead Outlets field while the water draw is attached using the Optional Side Draws table Figure 2 80 Condenser Overhead C Total a V r Ovhd Outlets apa Partial table The water draw C Full Afls product field
190. Temp lt empty gt Flow Rate lt empty gt 3 500e 007 Bt 2 81 2 82 Steady State Simulation Figure 2 100 Liquid Pump Around Summary Ee Draw Stage Return Stage Bie aE Export 2 Main e a ET lt empty gt 5 500e 007 lt empty gt lt empty gt 17 _ManTS 16_MainTS lt empty gt 3 500e 007 lt empty gt lt empty gt 22_MainTS 21_MainTS lt empty gt 3 500e 007 lt empty gt lt empty gt 13 Click the Design tab and select the Monitor page Re size the property view again so the entire Specifications table is visible Figure 2 101 Specifications L SpecifiedYalue Current Value Wt Eror Active Estimate Current Distillate Rate ____ lt empty gt lt empty gt lt empty gt Yap Prod Rate 0 0000 barrel day lt empty gt lt empty gt Reflux Ratio lt empty gt lt empty gt lt empty gt WasteH20 Rate lt empty gt lt empty gt lt empty gt KeroSS Prod Flow 1300 barrel day lt empty gt lt empty gt KeroSS Boillp Ratio 0 7500 lt empty gt lt empty gt DieselSS Prod Flow 17000 barrel day lt empty gt lt empty gt AGOSS Prod Flow 5000 barrel day lt empty gt lt empty gt PA_1_Fate Pa 5 000e 004 barrel day lt empty gt lt empty gt 6 500e 007 Btu hr 5 50e 007 0 0000 3 000e 004 barrel day lt empty gt lt empty gt 3 500e 007 Btu hr 3 50e 007 0 0000 Let 3 000e 004 barrel day lt empty gt lt e
191. The object name also known as a label appears near each icon The PFD shown above has been rearranged by moving the three utility stream icons below and to the left of the Separator To move an icon click and drag it to the new location You can click and drag either the icon arrow itself or the label stream name as these two items are grouped together Like any other non modal view the PFD view can be re sized by clicking and dragging anywhere on the outside border Dis lay Entire PFD icon Zoom In 25 icon Keep in mind that these are the HYSYS default colours you can change the colours in the Session Preferences Refining Tutorial Other things you can do while the PFD is active include the following e Access commands and features through the PFD toolbar e Open the property view for an object by double clicking on its icon e Move an object by click and dragging it to the new location e Access pop up summary information for an object simply by placing the cursor over it e Change an icon s size by clicking the Size Mode icon clicking on the icon and click and dragging the sizing handles that appear around the icon e Display the Object Inspection menu for an object by placing the cursor over it and right clicking This menu provides access to a number of commands associated with the particular object e Zoom in and out or display the entire flowsheet in the
192. Tutorials amp Applications 7 Copyright Notice 2002 Hyprotech a subsidiary of Aspen Technology Inc All rights reserved Hyprotech is the owner of and have vested in them the copyright and all other intellectual property rights of a similar nature relating to their software which includes but is not limited to their computer programs user manuals and all associated documentation whether in printed or electronic form the Software which is supplied by us or our subsidiaries to our respective customers No copying or reproduction of the Software shall be permitted without prior written consent of Aspen Technology Inc Ten Canal Park Cambridge MA 02141 U S A save to the extent permitted by law Hyprotech reserves the right to make changes to this document or its associated computer program without obligation to notify any person or organization Companies names and data used in examples herein are fictitious unless otherwise stated Hyprotech does not make any representations regarding the use or the results of use of the Software in terms of correctness or otherwise The entire risk as to the results and performance of the Software is assumed by the user HYSYS HYSIM HTFS DISTIL HX NET and HYPROP III are registered trademarks of Hyprotech PIPESYS is a trademark of Neotechnology Consultants Microsoft Windows Windows 95 98 Windows NT Windows 2000 Visual Basic and Excel are registered trademarks of
193. Vap CondDuty et Reactor Vent Reactor Pro Oxide Mixer Prods Out b Water Feed MIx 100 Coolant Reactor Glycol Tower The following pages will guide you through building a HYSYS case for modeling this process This example will illustrate the complete construction of the simulation including selecting a property package and components defining the reaction installing streams and unit operations and examining the final results The tools available in HYSYS interface will be utilized to illustrate the flexibility available to you Before proceeding you should have read Chapter A HYSYS Tutorials which precedes the tutorials in this manual 3 3 Steady State Simulation The simulation will be built using these basic steps 1 Create a unit set 2 Choose a property package 3 Select the components 4 Define the reaction 5 Create and specify the feed streams 6 Install and define the Mixer and Reactor 7 Install and define the Distillation Column The Workbook displays information about streams and unit operations in a tabular format while the PFD is a graphical representation of the flowsheet 3 4 3 2 Steady State Simulation c 1 Process Description The process being modeled in this example is the conversion of propylene oxide and water to propylene glycol in a CSTR Reactor The reaction products are then separated in a distillation tower A flowsheet for
194. a simulation in HYSYS Three complete tutorials are presented 1 Gas Processing e Steady State Models a sweet gas refrigeration plant consisting of an inlet separator gas gas heat exchanger chiller low temperature separator and de propanizer column e Dynamics Models the Gas Processing tutorial case in Dynamic mode This tutorial makes use of the recommendations of the Dynamic Assistant when building the case 2 Refining e Steady State Models a crude oil processing facility consisting of a pre flash drum crude furnace and an atmospheric crude column e Dynamics Models the Refining example problem in Dynamic mode 3 Chemicals e Steady State Models a propylene glycol production process consisting of a continuously stirred tank reactor and a distillation tower e Dynamics Models the Chemicals example problem in Dynamic mode This tutorial make use of the recommendations of the Dynamic Assistant when building the case Each of these tutorials will guide you step by step through the complete construction of a HYSYS simulation The tutorial you choose first will likely depend on which one is most closely related to your work or that you feel most comfortable with Regardless of the tutorial you work through first you will gain the same basic understanding of the steps and tools used to build a HYSYS simulation Each example contains detailed instructions for choosing a property package and components installing and
195. a unit set HYSYS does not allow you to change any of the three default unit sets listed however you can create a new unit set by cloning an existing one For this tutorial you will create a new unit set based on the HYSYS Field set then customize it 1 Inthe Available Units Sets list select Field The default unit for Liq Vol Flow is barrel day next you will change the Liq Vol Flow units to USGPM Session Preferences HYSYS PRF Variables A Units Formats Simulation Wariables Reports Files Resources Save Preference Set Available Unit Sets Display Units OO mmm 0st psia cee Ibmole hr Ib hr barrel day Btu hr Ibmole ts 1 Tray Sizing Oil Input Load Preference Set Extensions 2 Click the Clone button A new unit set named NewUser appears in the Available Unit Sets list 3 Inthe Unit Set Name field change the name to Field USGPM You can now change the units for any variable associated with this new unit set Find the Liq Vol Flow cell Click in the barrel day cell beside it 5 To open the list of available units click the down arrow J or press the F2 key then the Down arrow key Chemicals Tutorial 3 7 6 From the list select USGPM Figure 3 5 Session Preferences hysys PRF g ol x Variables Units Formats Available Unit Sets Field density Clone Field USGPM
196. ach and Move line appears between the PreFlashLiq stream icon and the cursor a by holding down the and a connection point appears at the Heater inlet CTRL key 2 59 Steady State Simulation 5 Place the cursor near the connection point of the heater and the trailing line snaps to that point As well a white box appears at the cursor tip indicating an acceptable end point for the connection Figure 2 67 r E 100 PreFlashLiq i i 6 Release the mouse button and the connection is made to the heater EE inlet Break Connection icon 7 Position the cursor over the right end of the heater icon The If you make an incorrect connection point and pop up Product appears connection _ I Cicnabraak 8 With the pop up visible click and hold the mouse button The white Connection icononine box again becomes black PFD toolbar 9 Move the cursor to the right of the heater A stream icon appears 2 Move the cursor over the with a trailing line attached to the heater outlet The stream icon stream line connecting the two icons A checkmark attached to the cursor appears indicating an Figure 2 68 acceptable connection to break E E 100 3 Click once to break the PreFlashLig connection indicates that a new stream is being created 10 With the stream icon visible release the mouse button HYSYS creates a new stream with the default name 1 11 Create the Heater energy stream starting the connect
197. al parameters Figure 1 124 ADJ 1 Parameters Solving Parameters Parameters Simultaneous Solution Secant 0 10000F 5 0000 F lt Unbounded gt lt Unbourded gt 10 Sim Adj Manager Optimizer Controlled as rt as ca baal Connections Parameters Monitor User Variables Delete Ignored Click the Monitor tab This allows you to view the calculations Click the Start button The Adjust converges on the target value within the specified tolerance in five iterations An LTS temperature adjusted variable of 4 4 F gives a sales gas dew point target variable of 10 F Figure 1 125 ADJ 1 Monitor mlteration History Tables Totallterations A e Plots Adjusted Value Target Value Residual 2 629 __ 2 332 2 187 0 6372 3 305e 004 i Connections Parameters Monitor User Variables Delete Ignored 1 96 Gas Processing Tutorial 97 0 Processing Tutorial 1 97 The Adjust has changed the LTS temperature from the original value of 0 F to 4 4 F The new sales gas heating value can now be compared to the previous value to see the effect of this change 7 Click the Close icon on the Adjust property view Results of the study Open the Workbook to access the calculated results for the entire flowsheet The Material Streams and Compositions tabs of the Workbook appear below Figure 1 126 Workb
198. ally you make one pressure flow specification per flowsheet boundary stream however there are exceptions to the rule One extra pressure flow specification is required for every condenser or side stripper unit operation attached to the main column This rule 2 136 For more information regarding Pressure Flow specifications in Column unit operations see Chapter 8 Column in Operations Guide Refining Tutorial applies only if there are no pieces of equipment attached to the reflux stream of the condenser or the draw stream of the side strippers Without other pieces of equipment i e pumps coolers valves to define the pressure flow relation of these streams they must be specified with a flow specification Pressure flow specifications for this case will be added to the following boundary streams e Atm Feed e Main Steam e AGO Steam e Diesel Steam e Off Gas e Waste Water e Naphtha e Kerosene e Diesel e AGO e Residue This simplified column has all the feed streams specified with a flow specification The Off Gas stream has a pressure specification which defines the pressure of the condenser and consequently the entire column The liquid exit streams of the column and the side stripper operations require pressure specifications since there are no attached pieces of equipment in these streams All the other exit streams associated with the column require flow specifications The following pump around streams re
199. ame to Key Variables1 3 93 3 94 Dynamic Simulation 8 Click the Active checkbox for each of the variables that you would like to monitor Keep the number of variables per Strip Chart to four or fewer for easier viewing Figure 3 122 DataBook File EI Available Strip Charts Individual Strip Chart Data Selection View DataLogger1 Logger Name DataLoagert Sample Int 000 00 20 00 Strip Chart raia i Object Variable Historical Coolant Cooling Duty i aa Reactor Prods Reactor Temp ctl Prop Oxide Mass Flow m Oe Water Feed Mass Flow Y Y y Add Reactor Vessel Temperature Reactor Prods Comp Molar Flow 12C30xide Delete Reactor Liquid Percent Level Setup You can change the configuration of each strip Variables Process Data Tables Strip Charts Data Recorder Case Studies chart by clicking the Setup button 9 Ifrequired add more strip charts 10 Click the Strip Chart button to view each strip chart 11 Click the Start Integrator icon and observe as the variables line out If you see a warning regarding the Dynamics Assistant click the No To view a legend for the Strip button Chart variables right click os eal inside the Stip Chart view When you are finished click the Integrator Holding icon to stop the and select Legend from the integrator une 12 At this point you can manipulate various variables within t
200. ange of the property package and the stream will turn yellow Since there is no DEA present in this stream the warning can be ignored without negatively affecting the results of this case Add a Cooler Add a cooler and define it as indicated below Cooler E 101 cools the lean DEA on its way to the main pump Cooler E 101 Tab Page inthis cells Design DEA TO COOL Energy Stream COOLER Q Design Delta P 5 psi Parameters Add a pump and define it as indicated below Pump P 100 transfers the regenerated DEA to the Contactor Pump P 100 Tab Page In this cell Enter Design DEA TO PUMP E a uae Worksheet Temperature F 95 F Conditions DEA TO RECY G1 13 Steady State Simulation The Cooler and the Pump operations will remain unconverged until the Set operation has been installed G1 14 Add a Set Operation Install a Set operation SET 1 to maintain the pressure of stream DEA TO RECY at 5 psi lower than the pressure of the gas feed to the absorber Set SET 1 Emere OO a a Parameters Multiplier Add a Recycle Operation A Recycle operation is installed with the fully defined stream DEA TO RECY as the inlet and DEA TO CONT as the outlet The lean amine stream which was originally estimated will be replaced with the new calculated lean amine stream and the contactor and regenerator will be run until the recycle loop converges To ensure an accurate solution reduce the
201. ange the name to 1500 O E and click the OK button to accept the new name 12 Click the View button and the Data Recorder appears displaying the new values of the variables Figure 2 144 Ni Data Recorder Main eflux Ratio 2 112 Refining Tutorial IB Tutorial 2 113 13 Record the process variables for Overflash rates of 5500 and 7500 barrels day Enter names for these variable states of 5500 O E and 7500 O E respectively The final Data Recorder appears below Figure 2 145 Si Data Recorder Main 3500 0 F 15000 F 55000 F 75000 F 0 7722 0 5857 0 9417 1 099 rim Duty Btu hr 3 172e 007 1 683e 007 4 304e 007 5 326e 007 STM 1160 Vac 5 389 5 377 8 398 6 405 7 Scenario 1 Delete Table Graph Re Number 2 113 Dynamic Simulation 2 3 Dynamic Simulation This complete dynamic case In this tutorial the dynamic capabilities of HYSYS are incorporated into has been pre built and is located in the file a basic steady state oil refining model A simple fractionation facility DynTUT2 hsc in your produces naphtha kerosene diesel atmospheric gas oil and HYSYS Samples directory atmospheric residue products from a heavy crude feed In the steady state refining tutorial preheated crude was fed into a pre flash drum which separated the liquid crude from the vapour The liquid crude was heated in a furnace and recombined with the vapour The combi
202. appears Figure 3 20 Reactions Fle x Conversion Heterogeneous Catalytic Kinetic Simple Rate Add Reaction 2 Inthe list select the Kinetic reaction type then click the Add Reaction button The Kinetic Reaction property view appears opened to the Stoichiometry tab On the Stoichiometry tab you Figure 3 21 can specify which of the Rxn Components are involved in X Kinetic Reaction Rixn 1 the particular reaction as well E Stoichiometry and Rate Info as the stoichiometry and the y Mole Wit reaction order hdd Cong Often you will have more than l one reaction occurring in your TT simulation case On the peels Reaction Heat 25 0 lt empty gt Stoichiometry tab of each reaction select only the Rxn Components participating in Delete Name Rin O No Reay that reaction a a z Stoichiometry Basis Parameters In the Component column click in the cell labeled Add Comp Select Water as a reaction component by doing one of the following e Open the drop down list and select H20 from the list of available reaction components e Type H2O HYSYS filters as you type searching for the component which matches your input When H20 is selected press the ENTER key to add it to the Component list 5 Repeat this procedure to add 12C3Oxide and 12 C3diol to the reaction table 3 18 Chemicals Tutorial Tutorial 3 19 The next task is to enter the stoichiometri
203. ar Entropy Btu Ibmole F lt empty gt Notes Heat Flow Btu hr lt empty gt Cost Parameters Liq Vol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 Composition Worksheet Attachments Dynamics 5 Unknown Compositions Delete Define from Other Stream a gt 3 33 3 34 Steady State Simulation 22 Select the Composition page to enter the compositional input for the new feed stream Figure 3 40 Water Feed Worksheet Won lt empty gt Conditions T lt empty gt 2 lt empty gt Properties Composition K Value User Variables Notes Cost Parameters Total 0 00000 Edit Edit Properties Basis i Worksheet Attachments Dynamics 5 Unknown Compositions i Define from Other Stream e For the current Composition 23 Click the Edit button near the bottom of the Composition page The Basis setting you want to Input Composition for Stream view appears enter the stream composition _ f on a mass flow basis 24 In the Composition Basis group change the basis to Mass Flows by selecting the appropriate radio button or by pressing ALT A 25 In the CompMassFlow cell for H20 type 11 000 lb hr then press ENTER Figure 3 41 Nil Input Composition for Stream Water Feed PEE z Composition Basis 2030 xide lt empty gt Mole Fractions i r ee adil aay Mass Fractions C Lig Volume Fractions C Mole Flows
204. ars Figure 3 112 ProductBlock_Reactor Yent x Associated Stream Reactor Yent Flow Reversal Conditions Pressure f 6 166 psia Yapour Fraction empty gt Temperature fi 40 00 F C Enthalpy Kempty C Entropy Kempty gt Export Conditions to Stream Update From Stream a aes Conditions Composition Ignored 12 Click the Composition tab 13 In the Compositions table specify the composition of the reverse flow stream as follows Component Mole Fraction 14 Click the Conditions tab Chemicals Tutorial 3 85 15 In the Flow Reversal Conditions group select the Temperature radio button 16 In the field beside the Temperature radio button enter 77 F These stream conditions will be used to flash the pure nitrogen stream when the Reactor Vent flow reverses 4 ProductBlock_Reactor Yent lol x Associated Stream Reactor Yent Flow Reversal Conditions Pressure 16 166 psia C Yapour Fraction Kempty Temperature 7000F C Enthalpy kempty gt C Entropy Kempy Export Conditions to Stream Update From Stream Conditions Ignored 17 Close the ProductBlock_Reactor Vent view 18 Close the Reactor Vent stream property view 19 Save the case as DynTUT3 3 hsc 3 85 Os Control Ops icon Q PID Controller icon 3 86 Dynamic Simulation 3 3 4 Adding Controller Operations In this section you will identify a
205. assBal SubFlowsheet s iaga a MPC Controller C Prebuilt Columns Ts ESE C Short Cut Columns Parametric Unit Operation C Sub Flowsheets ig oe Logicals ipe Segment planers Plug Flow Reactor Pump C User Ops Reboiled Absorber C Electrolyte Equipment oe n c efinery Assay Fixer Refinery Ops Refinery Blender 5 With Mixer selected click the Add button or press ENTER 3 37 3 38 Steady State Simulation The property view for the Mixer appears The default naming scheme Figure 3 46 for unit operations can be changed in your Session Preferences gt MIX 100 Design Name Mix no Connections Parameters User Variables Notes Inlets Outlet lt lt Stream gt gt x Fluid Package Basis 1 Design Rating Worksheet Dynamics The unit operation property view contains all the information required to define the operation organized into tabs and pages The Design Rating Worksheet and Dynamics tabs appear in the property view for most operations Property views for more complex operations contain more tabs HYSYS has provided the default name MIX 100 for the Mixer Many operations like the Mixer accept multiple feed streams Whenever you see a table like the one in the Inlets group the operation will accept multiple stream connections at that location When the Inlets table is active you can access a drop down list of available streams Next you will complete the Conn
206. at Flow Btu hr lt empty gt Cost Parameters Lig Vol Flow Std Cond barrel day _ lt empty gt Fluid Package Basis 1 p Worksheet Attachments Dynamics 6 Unknown Compositions Delete Define from Other Stream lt a gt 13 Select the Composition page to begin the compositional input for the new stream Figure 2 48 Worksheet Conditions Properties Composition i Pentane n Pentane K Value User Variables Notes NBF 0 188 l lt empty gt Cost Parameters Total 0 00000 Edit Edit Properties Basis i Worksheet Attachments Dynamics 5 Unknown Compositions i Define from Other Stream e The current Composition Basis setting is set to the Preferences Default of Mole Fractions The stream 14 Click the Edit button The Input Composition for Stream view composition is entered on a appears mass basis i 2 45 Steady State Simulation 15 In the Composition Basis group select the Mass Flows radio button 16 Click in the compositional cell for H20 17 Type 2500 for the steam mass flow then press ENTER As there are no other components in this stream the compositional input is complete Since only H20 contain any 18 Click the OK button to close the view and return to the stream significant value HYSYS property view automatically forces all other components value to be zero Figure 2 49 AGO Steam a
207. ate REACTOR unit operation Chemicals Tutorial 3 23 1 Inthe Reaction Sets group click the Add Set button The Reaction Set property view appears with the default name Set 1 Reaction Set Set 1 ex Name Set Set Info 7 SetType Unknown Not Ready Advanced paces Inactive List Operations Attached View Active View Inactive Make Inactive gt lt Make ctive The drop down list contains all 2 In the Active List click in the cell labeled lt empty gt reactions in the Global Reaction Set Currently Rxn 1 3 Open the drop down list and select Rxn 1 is the only reaction defined so it is the only available selection A checkbox labeled OK automatically appears next to the reaction in the Active List The reaction set status bar changes from Not Ready to Ready indicating that the new reaction set is complete Rxn 1 4 Close the Reaction Set view to return to the Simulation Basis l Manager The new reaction set named Set 1 now appears in the Reaction Sets group Figure 3 28 Simulation Basis Manager Asn Components _ sy Reactions Reaction Sets 12C30xide Rxn 1 Jiew Rgn Global Axn Set View Set 12 C3diol Set 1 i H20 Add Bsn Add Set Delete Ren Delete Set Copy Set ome Assoc Fluid Pkgs Import Set Export Set Add Comps Add to FP Components Fluid Pkgs Hypotheticals
208. ates a reference to a stream in the other case The stream s name is the value of the user variable LinkStream Creates a reference to stream currently in the primary feed list Sets the Temperature and Pressure values of Case2Strm to those of Case1Strm X1 13 Creating a User Unit Operation Oreye X1 14 Dim CaselCMFs As Variant CaselCMFs CaselStrm ComponentMolarFlowValue Dim Case2CMFs As Variant Case2CMFs Case2Strm ComponentMolarFlowValue On Error GoTo NoComp Dim Comp As Object i 0 For Each Comp In Case2FS FluidPackage Components Case2CMFs i 0 0 CompName Comp name n CaselFS FluidPackage Components index Co mpName Case2CMFs 1i NoComp LL Next Comp CaselcCMFs n Je On Error GoTo EarlyGrave Case2Strm ComponentMolarFlowValue Case2CMF s ActiveObject SolveComplete Bx Sub FarlyGrave MsgBox Execute Error Explanation Creates an array containing the molar flow of Case1Strm Note that Set was not used so changes made to Case1CMFs will not affect Case1Strm Creates an array containing the molar flow of Case2Strm Note that Set was not used so changes made to Case2CMFs will not affect Case2Strm For every component i in the Case2FS you set the molar flow of component i in the Case2CMFs array to the flow of the same component in Case1CMFs array This passes the value of Case2CMFs to the Case2Strm Signifies the Unit Operation has solved It
209. ation both unit operations would be listed in the box To access the property view for the Mixer double click on its name in the gray box Prop Oxide Water Feed Mixer Dut 0 0000 0 0000 0 0000 75 00 16 17 Molar Flow Ibmolehr 150 0 75 00 16 17 610 6 75 00 16 17 760 6 Mass Flow lb hr 8712 Liquid Yolume Flow USGPM 20 83 7 804e 006 Energy Streams 1 100e 004 22 01 7 481e 007 Unit Ops C Include Sub Flowsheets C Show Name Only Number of Hidden Objects 1 971e 004 42 84 8 262e 007 Chemicals Tutorial AB Tutorial 3 43 Adding a Tab to the Workbook When the Workbook is active the Workbook item appears in the HYSYS menu bar This item allows you to customize the Workbook Next you will create a new Workbook tab that displays only stream pressure temperature and flow 1 Doone of the following e From the Workbook menu item select Setup e Object inspect right click the Material Streams tab in the Workbook then select Setup from the menu that appears The Workbook Setup view appears Figure 3 53 Workbook Tabs Tab Contents Material Streams Add Object Compositions l Energy Streams TE Name M aterial Streams Order Unit Ops Type Material Stream New Type i J Variables Format Use Set 1 4 fixed Temperature 4 sig fig Add Pressure 4 sig fig Molar Flow 4 sig fig Delete Mass
210. ation active Specs page when you created it P par 11 Return to the Monitor page The new specification may not be visible unless you scroll down the table because it has been placed at the bottom of the Specifications list 1 71 1 72 Steady State Simulation 12 Click the Group Active button to bring the new specification to the top of the list directly under the other Active specification Figure 1 91 L Column De Propanizer COL1 Fluid Pkg Basis 1 Peng Robinson Profile Design jis Checks 7 Input Summary View Initial Estimates Connections Monitor E quilibriurn Heat Spec Specs Temp Press C Flows Specs Summary Subcooling Notes Specifications a Specified Value Current Value Wt Eror Active Estimate Current Reflux Ratio 1 000 lt empty gt lt empty gt Propane Fraction 2 000e 002 lt empty gt lt empty gt Ovhd Vap Rate 2 000 MMSCFD 2 00 0 0000 Reflux Rate lt empty gt lt empty gt lt empty gt Btms Prod Rate lt empty gt lt empty gt lt empty gt l View Add Spec i i Update Inactive Degrees of Freedom 0 E Design Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged J Update Outlets Ignored The Degrees of Freedom has returned to zero so the column is ready to be calculated
211. barrel day lt empty gt Fluid Package Basis 1 E Worksheet Dynamics E Delete Define from Other Stream lt a gt gt The change in Temperature generates the following results e The Sales Gas flow rate has increased e The Liquid Product flow rate has decreased e The sales gas dew point has increased to 15 9 F This temperature no longer satisfies the dew point specification of 15 F 7 Click the Close button on the ColdGas stream property view to return to the Databook Recording the New Variables in the Databook In this section you will record the key variables in their new state 1 Click the Data Recorder tab in the Databook 2 Click the Record button and the New Solved State view appears HYSYS provides you with the default name State 2 for the new state 3 Change the name to 10 Fin LTS then click the OK button to accept the new name 1 86 Gas Processing Tutorial 87 Processing Tutorial 1 87 4 Click the View button and the Data Recorder appears displaying the new values of the variables Figure 1 114 Si Data Recorder Main o 10F in LTS 10 00 15 91 7 361 451 3 Scenario 1 Delete Table Graph Re Number 5 Click the Close icon on the Data Recorder then on the Databook and finally on the Key Variables Table 6 Save the case The basic simulation for this example has now been completed You
212. ble Utilities view You should still be in the Column sub flowsheet environment If not double click the Column T 100 and then click the Column Environment button on the bottom of the Column property view 14 In the PFD double click the Kero_SS side stripper icon to open its property view 15 Click the Rating tab then select the Sizing page 16 Specify the following tray section parameters that were calculated in the previous table e Section Diameter e Tray Spacing e Weir Height e Actual Weir Length Figure 2 161 Tray Dimensions Tray Space m 0 6096 Tray Vol m3 1 676 5 080e 002 Weir Length m 1 362 C Yolume m3 I _ _ 8 836e 002 ctive Area m2 lt empty gt low Paths 1 EF Run Column Solver icon Refining Tutorial 17 Close the Kero_SS property view 18 Double click the Diesel_SS icon then specify the tray rating information using the table on the previous page Close the property view when you are done 19 Repeat the same procedure to specify the tray rating information for AGO_SS 20 After the column has been specified with the tray rating information converge the column by clicking the Run Column Solver icon in the toolbar 21 Save the case as DynTUT2 2 hsc Vessel Sizing The Condenser and Kero_SS_Reb operations require proper sizing before they can operate effectively in dynamic mode The volumes of these vessel operations are determined based on a 10 minute li
213. boiler To Stillageb Reboiler Another factor of interest is the concentration of heavy alcohols in the interior of the Rectifier These alcohols are normally referred to as Fusel oils and a small side liquid draw is provided in the Rectifier to recover these components There are two general steps in this process simulation 1 Setup The NRTL property package and the UNIFAC VLE estimation method will be used for this case The Components list includes Ethanol H20 CO2 Methanol Acetic Acid 1 Propanol 2 Propanol 1 Butanol 3 M 1 C4ol 2 Pentanol and Glycerol 2 Steady State Simulation This case will use a separator two absorbers a refluxed absorber and a distillation column se l e Setup From the Tools menu select 1 In anew HYSYS case set the units to SI peer oneee 2 Select the following components Ethanol H20 CO2 Methanol sles ie vatlanlies tap tren Acetic Acid 1 Propanol 2 Propanol 1 Butanol 3 M 1 C4ol 2 select the Units page ae Select SI from the Available Pentanol an ycerol Unit Sets list then close the 3 Select NRTL as the Property Package VIEW On the Binary Coeffs tab Fluid Package property view select the UNIFAC VLE radio button then click the Unknowns Only button to estimate the missing interaction parameters 1 3 Steady State Simulation 1 3 1 Adding Streams Enter the Simulation environment and add the material streams defined below Name Wash H20 FromFerm Steam
214. by the Heat Flow of stream Coolant The next step is to examine the Reactor conversion as a function of temperature Chemicals Tutorial 3 55 13 Click the Reactions tab then select the Results page The conversion appears in the Reactor Results Summary table Figure 3 70 Reactor Set 1 Reactions Reaction Results Summary Daa C Reaction Balance Details Design Reactions Rating Worksheet Dynamics Delete ES ono Under the current conditions the Actual Percent Conversion Act Cnv in the Reactor is 40 3 You will adjust the Reactor temperature until the conversion is in the 85 95 range 14 Click the Worksheet tab 15 In the Reactor Prods column change the Temperature to 100 E 16 Return to the Reactions tab to check the conversion which has increased to 72 28 as shown below Figure 3 71 Reaction Results Summary C Reaction Balance Cie Cry Base Comp 12C30 xide 17 Return to the Worksheet tab and change the Temperature of Reactor Prods to 140 E 3 55 3 56 Steady State Simulation cn Distillation Column Icon The Input Expert is a logical sequence of input views that guide you through the initial installation of a Column Complete the steps to ensure that you have provided the minimum amount of information required to define the column The Input Expert is a Modal view indicated by the absence of the Maximize Minimize icons You cannot
215. c Value 10 Molar The specifications views should appear as follows Figure R2 3 Figure R2 4 Reflux Ratio Spec Reflux Ratio x Sy Comp Frac Spec NH3 Mass Fra x NH3 Mass Frac Reboiler tage Reboiler Feflus Ratio iow Basis ole Fraction Flow Bass Malar hase a Spec Vee 10 00 Components 1 000e 005 Ammonia Condenser i Include Vapour lt lt Component gt gt C Stream Stage Target Type Parameters Summary Delete Delete For more information on 9 which damping factor is recommended for different systems refer to Chapter 8 Column of the Operations Guide Click the Parameters tab then select the Solver page Change the Fixed Damping Factor to 0 4 A damping factor will speed up tower convergence and reduce the effects of any oscillations in the calculations the default value is 1 0 9 Click the Run button The column will converge R2 7 R2 8 Results He o Hesults Workbook Case Main Materials Streams Tab Figure R2 5 Workbook Case Main Name SourH20 Feed Stripper Feed Stripper Bottom Effluent OffGas a Vapour Fraction 0 0000 0 0033 0 0000 0 0000 1 0000 7 Temperature F Pressure psia 100 0 40 00 200 0 30 00 255 3 32 70 S27 22 70 210 9 28 70 Molar Flow lbmole hr _ 3 996e 004 3 996e 004 3 905e 004 3 905e 004
216. c information A negative stoichiometric coefficient indicates that the component is consumed in the reaction while a positive coefficient indicates the component is produced 6 In the Stoich Coeff column click in the lt lt empty gt gt cell corresponding to H20 Type 1 and press the ENTER key Enter the coefficients for the remaining components as shown in the view below Figure 3 22 Kinetic Reaction Rxn 1 Stoichiometry and Rate Info H20 18 015 1 000 12C30xide 58 080 1 000 12 C3diol 76 096 1 000 Add Comp ag 0 00000 Aae Reaction Heat 25 C 3 9e 04 Btu Ibmole Stoichiometry Basis Parameters Delete Name Rant NotReady Once the stoichiometric coefficients are supplied the Balance Error cell will show 0 zero indicating that the reaction is mass balanced HYSYS will also calculate and display the heat of reaction in the Reaction Heat cell In this case the Reaction Heat is negative indicating that the reaction produces heat exothermic HYSYS provides default values for the Forward Order and Reverse Order based on the reaction stoichiometry The kinetic data for this Tutorial is based on an excess of water so the kinetics are first order in Propylene Oxide only 3 19 3 20 Notice that the default values for the Forward Order and Reverse Order appear in red indicating that they are suggested by HYSYS When you enter the new value for H20
217. cations that HYSYS has created In general a Distillation Column has three default specifications The overhead Vapour Rate and Reflux Ratio will be used as active specifications and later you will create a glycol purity specification to exhaust the third degree of freedom The third default specification overhead Liquid Rate will not be used The Flow Basis applies to the Vapour Rate so leave it at the default of Molar You can also change specification values and activate or de activate specifications used by the Column solver directly from the Monitor page Chemicals Tutorial 16 In the Vapour Rate field enter 0 lbmole hr In the Reflux Ratio field enter 1 0 Figure 3 76 Ni Distillation Column Input Expert x Vapour Rate 0 000000 Liguid Rate Flow Basis Molar x Reflux Ratio lt Prev Done Side Ops gt Specifications page 4 of 4 Cancel 17 Click the Done button The Column property view appears 18 On the Design tab select the Monitor page L Column Tower COL1 Fluid Pkg Basis 1 UNIQUAC Ideal Design r Profile i View Initial Estimates Connections mn Temp Monitor Equilibrium Heat Spec 5 C Press ais C Flows Specs Summary ae Subcooling Notes Specifications SpecifiedYalue Current Value Wt Error O oo semp lt empt gt Wo vw vw Ovhd Vap Rate 0 0000 Ibmole hr 7 94e 01
218. cell separately and are not f i included in these labeled lt empty gt The value you will enter in this cell is the upper hypocomponents cut point temperature for the first range and the lower cut point for the second range 10 Type 800 then press the down arrow key 11 Enter the remaining cut point temperatures and the Num of Cuts values as shown in the figure below Figure 2 31 Cut Ranges Cut Option Selection User Ranges X Ranges Selection Upper Temp Limit 1446 828F Starting Cut Point fi 00 000 F Cut Ean point 800 000 1200 000 1400 000 12 Once you have entered the data click the Submit button to calculate the Blend based on the current initial cut point and range values The message Blend Was Calculated appears in the status bar 2 32 Steady State Simulation HYSYS has provided the Initial Boiling Point IBP and Final Boiling Point FBP The IBP is the normal boiling point NBP of the heaviest component in the Light Ends in this case n Pentane The FBP is calculated by extrapolating the TBP Assay data to 100 distilled 2 32 13 Click the Tables tab to view the properties of the petroleum hypocomponents Figure 2 32 Si Blend Blend 1 Table Type Component ied Properties Component Properties Table Contro 6 01 EL 00 Main Properties __ NBP_1393 f US Z3 l 6 3480e 00 C Other Properties NBP_164 L L 6 801 6e 00 Dil NBP_188
219. cell for the Distillate Rate specification enter 2e4 bbl day Activate the Overflash specification by clicking its Active checkbox Activate the Kero Reb Duty specification Activate the Vapour Prod Rate specification If the column begins to run on its own before you click the Run button click the Stop button and continue activating or deactivating specifications Deactivate the Reflux Ratio specification Deactivate the Waste H20 Rate specification So o oe St e Deactivate the KeroSS BoilUp Ratio specification 2 88 2 88 Steady State Simulation 9 Click the Run button to begin calculations The information displayed on the page is updated with each iteration The column converges as shown in the figure below Figure 2 108 This matrix displays the Iteration number Step size Equilibrium error and Heat Spec error Column Atmos Tower COL1 Fluid Pkg Basis 1 7 Peng Robinson Design Connections Monitor Specs Specs Summary Subcooling Notes igy Design Side Ops Rating Worksheet Performance Delete Column Environment Run Reset The status indicator has changed from Unconverged to Converged The column temperature profile is shown here You can view the pressure or flow profiles by picking the appropriate radio button Input Summary View Initial Estimates Optional Checks Profile hter Step Equilibrium Heat Spec 3 0 0001 1 1 0000 0 001311 1 0
220. ch Mode Icon mode The Attach Mode button stays active until you click it again 2 Position the cursor over the right end of the Mixer Out stream icon A small white box appears at the cursor tip with a pop up When you are in Attach mode description Out indicating that the stream outlet is available for you will not be able to move connection objects in the PFD To return to Move mode click the Attach button again You can Figure 3 60 temporarily toggle between Attach and Move mode by holding down the CTRL key Prop Oxide Mixer Out VVater Feed MIX 100 CSTR 100 3 With the pop up Out visible click and hold the mouse button The transparent box becomes solid black indicating that you are beginning a connection Multiple connection points 4 Move the cursor toward the left inlet side of the CSTR 100 icon A appear Be J Reactor line appears between the Mixer Out stream icon and the cursor and a pow ieemne multiple connection points blue appear at the Reactor inlet 5 Place the cursor near a connection point until a solid white box appears at the cursor tip indicating an acceptable end point for the connection Figure 3 61 Pro Oxide Rakar MIX100 Feed 6 Release the mouse button and the connection is made between the stream and the CSTR 100 inlet 7 Position the cursor over top right hand corner of the CSTR 100 icon The white box and the pop up Vapour Product appear 8 With th
221. change any of the values provided by HYSYS if you have data of your own 3 15 Steady State Simulation In this case the only unknown coefficients in the table are for the 12C3Oxide 12 C3diol pair You can enter these values if you have available data however for this example you will use one of HYSYS built in estimation methods instead Next you will use the UNIFAC VLE estimation method to estimate the unknown pair 2 Inthe Coeff Estimation group ensure the UNIFAC VLE radio button is selected 3 Click the Unknowns Only button HYSYS provides values for the unknown pair The final Activity Model Interaction Parameters table for the Aij coefficients appears below Figure 3 18 Activity Model Interaction Parameters Coeff Matrix To View fe Ai 12030xide 12 C3diol H20 2030 xide 170 71 909 2 C3diol 787 060 335 033 20 823 550 5 027 4 To view the Bij coefficient table select the Bij radio button For this example all the Bij coefficients will be left at the default value of Zero 3 16 l Basis Icon These steps will be followed in defining our reaction 1 Create and define a Kinetic Reaction 2 Create a Reaction Set containing the reaction 3 Activate the Reaction set to make it available for use in the flowsheet Chemicals Tutorial 3 17 3 c 4 Defining the Reaction 1 Return to the Simulation Basis Manager view by clicking on its title bar or by cl
222. ck the Parameters page The Exchanger Design End Point is the acceptable default setting for the Heat Exchanger Model for this tutorial 6 Enter a pressure drop of 10 psi for both the Tube Side Delta P and Shell Side Delta P Figure 1 52 m Gas Gas Design Heat Exchanger Model Heat Leak Loss Connections Exchanger Design End Point None C Extremes Proportional Parameters Specs Tube Side Shell Side evar Detap fO00pi elta P Notes Delta P fi 0 00 psi UA lt Design Rating Worksheet Performance Dynamics HTFS TASC Delete Ne O Ode S gr 1 43 1 44 Steady State Simulation 7 Click the Rating tab then select the Sizing page 8 In the Configuration group click in the Tube Passes per Shell cell then change the value to 1 to model Counter Current Flow Figure 1 53 m Gas Gas OF xi Sizing Data Rating f e Overall C Shell C Tube F Accept any input data Sizing Parameters Configuration Calculated Information lt empty gt lt empty gt _ lt empty gt Horizontal Counter eat Trans Area per Shell ft2 Tube Volume per Shell t3 TEMA Tye A E L Shell Volume per Shell ft3 Ss Design Rating Worksheet Performance Dynamics HTFS TASC Delete NetSoved O o pdate Le 9 Close the Heat Exchanger property view to return to the Workbook 10 Click the Material Streams tab of t
223. click the OK button 38 In the Available Display group click the View button The Data Recorder appears displaying the new values of the variables Figure 3 102 Data Recorder Main 140 0 180 0 4520e 00E 4 111e 00 713 4 745 5 a Scenario 1 Delete Table Graph Re Number 39 Close the Data Recorder view then the Databook view and finally the Key Variables Data view This completes the HYSYS Chemicals Steady State Simulation tutorial If there are any aspects of this case that you would like to explore further feel free to continue working on this simulation on your own Further Study For other chemical case examples see the Applications section Applications beginning with C explore some of the types of chemical simulations that can be built using HYSYS 3 75 A completed dynamic case has been pre built and is located in the file DynTUTOR3 hsc in your HYSYS Samples directory This tutorial follows these basic steps for setting up a dynamic simulation case 1 Obtain a simplified steady state model to be converted to dynamic mode 2 Use the Dynamic Assistant to set pressure flow specifications modify the flowsheet topology and size the equipment 3 Modify the Reactor vent stream to account for reverse flow conditions 4 Set up temperature and level controllers around and in the Reactor vessel 5 Set up the Databook Make c
224. con To move an icon simply click and drag it to a new location You can click and drag either the icon arrow itself or the label stream name as these two items are grouped together 3 46 Chemicals Tutorial AT Tutorial 3 47 Other functions that can be performed while the PFD is active include iver Dat the following roe moleh Access commands and features through the PFD tool bar Fly by information e Open the property view for an object by double clicking its icon e Move an object by clicking and dragging it to the new location e Access fly by summary information for an object by placing the meee Size Icon cursor over it He e Size an object by clicking the Size icon selecting the object then Bs clicking and dragging the sizing handles that appear Zoom Out 25 e Display the Object Inspection menu for an object by placing the cursor over it and right clicking This menu provides access to a number of commands associated with the particular object Display Entire e Zoom in and out or display the entire flowsheet in the PFD PFD window by clicking the zoom buttons at the bottom left of the PFD view Zoom In 25 Some of these functions will be illustrated in this tutorial for more information refer to the User Guide Calculation Status HYSYS uses colour coding to indicate calculation status for objects both in the object property views and in the flowsheet If you recall the status bar indicat
225. ct group select InletSep In the Variable group select Liquid Percent Level Click the OK button Figure 1 152 Select Input P For Sep LC Flowsheet Object Variable Case Main Heating Value Aqueous Level DePropanizer COL1 Chiller Aqueous Yolume DePropanizer Boot Diameter Gas Gas Boot Height Object Filter Heater Chamber 2 Phase Leve C All InletSep LTS C Streams l LTS Valve Liquid Flow SP on Navigator Scope MIX 100 Liquid Holdup Thermo C Logicals MI gt lt 101 Liquid Level ColumnOps Pete Sep Valve Liquid Mass Flow ee C Case Tower Yalve Liquid Molar Flow Basis Custom C Utility j Variable Description Liquid Percent Level Cancel 8 Inthe Output Target Object group click the Select OP button The Select Op Object view appears 9 Inthe Flowsheet group select Case Main In the Object group select Sep Valve Click the OK button Figure 1 153 Flowsheet Object Case Main C3Duty OK DePropanizer COL1 CondDuty Feed 1 Object Filter Feed 2 All i G i C Streams LTSYap C UnitOps RebDuty C Logicals SepLiq e Sepa ColumnOps LTS Valve C Custom Tower Valve i Custom 1 f WISCOUNNTC Cancel 10 Click the Parameters tab then select the Configuration page 11 Enter the information specified in the following table In this cell Enter Action o Click the Direct radio button 1 121 1 122 Dynamic Simulation Object Navigato
226. ct stream Figure 2 52 I PreFlash Design Name PreFlash Connections Inlets Preheat Crude Vapour Outlet Parameters lt lt Stream gt gt User Variables Notes Energy Optional Fluid Package Liquid Outlet Basis 1 Design Reactions Worksheet Dynamics Delete eee lonoed 10 Click in the Vapour Outlet field or press TAB to move to the field 11 Type PreFlashVap in the field then press ENTER This stream does not yet exist so HYSYS creates this new stream 12 Click in the Liquid Outlet field and type PreFlashLiq HYSYS creates another new stream Figure 2 53 I PreFlash Design Name PreFlash Connections Inlets P t Vapour Outlet arameters lt lt Stream gt gt PreFlashVap v User Variables Notes Energy Optional x Fluid Package Liquid Outlet Basis 1 PreFlashLiq v Design Reactions Worksheet Dynamics Delete TT ioro 2 49 2 50 Steady State Simulation An Energy stream could be The status indicator displays a green OK message showing that the attached to heat or cool the operation and attached streams are completely calculated vessel contents however for the purposes of this 13 Select the Parameters page The default Delta P pressure drop of example the energy stream zero is acceptable for this example The Liquid Level is also is not required acceptable at its default value Figure 2 54 Since there is no energy stream attached to
227. d Pressure 4 sig fig Molar Flow 4 sig fig Delete Mass Flow 4 sig fig Std Ideal Liq Vol Flow 4 sig fig Format ___Heat Flow _ 4 sig fig_ Molar Enthalpy 4 sig fig Order Pepe BE 3 44 Chemicals Tutorial 4B Tutorial 3 45 The next task is to customize the tab by removing the variables that are irrelevant 6 Inthe Variables table select the first variable Vapour Fraction 7 Press and hold the CTRL key 8 Select the following variables Mass Flow Heat Flow and Molar Enthalpy 9 Release the CTRL key 10 Click the Delete button beside the table to remove the selected variables from this Workbook tab only The finished Setup appears If you want to remove in the figure below variables from another tab you must edit each tab individually Figure 3 56 Workbook Tabs r Tab Contents Material Streams Add Object P T Flow l Compositions Delete Name P T Flow Order E St i Unit Ops ai Type Material Stream New Type Variables Use Set Temperature 4 sig fig Pressure 4 sig fig Add Molar Flow 4 sig fig Std Ideal Lig Yol Flow 4 sig fig Order 11 Close the Setup view The new tab appears in the Workbook Figure 3 57 Workbook Case Main Water Feed Mixer Dut emperature F j 75 00 75 00 75 00 ressure psia 16 17 i 610 6 Std Ideal Lig Yol Flow USG
228. ditional ad lt none gt x aaplahe Sim Name Full Name Synonym Formula Fan i T Fil Hypothetical amily Type Fite Other lt Add Pure Hl lV Use Filter a Hydrocarbons N20 Solids _ lt Substitute N204 V Miscellaneous P Amines Alcohols Ketones amin S_Liq 150 Sulphur_Liq_150 I Aldehydes _Liq_190 Sulphur_Liq_190 IT Esters S_Liq_280 Sulphur_Liq_280 ee S_Vapour Sulphur_ apour J Caboxylic Acids Mercury Mercury P Halogens ae ee a T Nitriles M Show Synonyms Cluster Phenols J Ethers Selected Component by Type User Defined s All Delete Component List 1 Invert View lomponent 9 Check the Use Filter checkbox 10 CO2 does not fit into any of the standard families so check the Miscellaneous checkbox 11 Scroll down the filtered list until CO2 becomes visible 12 Double click the CO2 component to add it to the component list The Match feature remains active when you use a filter so you could also type CO2 in the Match cell select it then add it to the component list To select consecutive To add the remaining components C1 through nC4 using the filter components use the SHIFT uncheck the Miscellaneous checkbox and check the Hydrocarbons key To select non consecutive components use the cTr key box Gas Processing Tutorial 1 15 The following shows you a quick way to add components that appear consecutively in the libra
229. e 75 54 kgmole h fw Feeder block Worksheet Attachments Dynamics KR Delete Define from Other Stream 4 gt gt Once a pressure or flow specification has been made active the stream value turns blue and can be modified 2 138 Refining Tutorial 8 Set the following pressure or flow specifications for the following streams in the Main Flowsheet Material Stream Pressure Specification Flow Specification EVIE Mein Steam recive Molar Flow Active 188 8 komol oncas aeie fme ssa Maphina nacive Weal Liq Acve 1524mm Dese aee reme TP mo faee o free o fasea 9 Use the Object Navigator to enter the Column subflowsheet environment Click the Object Navigator icon in the tool bar The Object Navigator view appears In the Flowsheets group double click T 100 Every material stream in the column environment also requires either a pressure or flow specification Use the following procedure to set a pressure flow specification for the PA_1_Draw stream 10 In the PFD double click the PA_1_Draw stream icon to open the property view 11 Click the Dynamics tab then select the Specs page 2 139 240 Dynamic Simulation Dynamic Simulation Start Integrator icon 2 140 12 In the Flow Specification group select the Molar radio button then activate the Active checkbox Figure 2 173 PA_1_Draw Dynamics Dynamic Specifications Pressure
230. e Include Atmos Tower Reflux Ratio M Delete _TrmDuty Trim Duty Iv Residue BP Cui ASTM 1160 Vac 5 Residue Vv Avalane Wistlat Table f Graph VieV g Variables Process Data Tables Strip Charts Data Recorder Case Studies Click the Record button to record the variables in their current state The New Solved State view appears prompting you for the name of the new state Change the Name for New State from the default State 1 to 3500 O E denoting 3500 bbl day Overflash Click the OK button and you return to the Databook In the Available Display group select the Table radio button Refining Tutorial 2 111 7 Click the View button and the Data Recorder appears showing the values of the key variables in their current state Figure 2 142 Data Recorder Main State SooF 0 7720 3173 007 3896 a Scenario 1 Delete Table Graph Re Number Now you can make the necessary flowsheet changes and these current values remain as a permanent record in the Data Recorder unless you choose to erase them 8 Click the Minimize icon to reduce the Data Recorder to an icon Changing the Overflash Specification The value of the Overflash specification is going to be changed in the column and the changes is viewed in the process data table 1 Click the Navigator icon on the toolbar si 2 Select the UnitOps rad
231. e Licensing RTI Server Column Status Window Trace Window Simulation General Options J Use Input Experts J View New Streams upon Creation Jv Confirm Deletes Use Modal Property Views J Confirm Mode Switches J Record Time When Notes Are Modified Enable Single Click Actions V Enable Cross Hairs On PFD J Enable Cell Edit Button Errors Display Errors in Trace Window Display Numerical Errors in Trace Window Ignore Them in Dynamics Mode Show Property Package Warning MV Show Property Package Warning Property Correlations MV Activate Standard Property Correlations MV Confirm Before Adding if Active Correlations are Present Reports Resources Extensions Oillnput Tray Sizing Save Preference Set Load Preference Set 2 The Simulation tab Options page should be visible Ensure that the Use Modal Property Views checkbox is unchecked Click the Variables tab then select the Units page 3 5 3 6 Steady State Simulation The default Preference file is named HYSYS prf When you modify any of the preferences you can save the changes in a new Preference file by clicking the Save Preference Set button HYSYS prompts you to provide a name for the new Preference file which you can later recall into any simulation case by clicking the Load Preference Set button 3 6 Creating a New Unit Set The first task you perform when building the simulation case is choosing
232. e Main Flowsheet for this process appears in the following figure Figure 2 3 Naphtha TrimDuty WasteH20 TowerF eed PreFlash Kerosene Preheat BottomSteam Crude PreFlashVap DieselSteam Furnace Diesel L PreFlashLig HotCrude AGOSteam Residue CrudeDuty _ CondDuty Preheated crude from a preheat train is fed to the pre flash drum modeled as a Separator where vapours are separated from the crude liquids The liquids are then heated to 650 F in the crude furnace modeled as a Heater The pre flash vapours bypass the furnace and are re combined using a Mixer with the hot crude stream The combined stream is then fed to the atmospheric crude column for separation 2 5 Pa Steady State Simulation The Workbook displays information about streams and unit operations in a tabular format while the PFD is a graphical representation of the flowsheet 2 6 The crude column is modeled as a Refluxed Absorber equipped with three pump around and three side stripper operations The Column sub flowsheet appears in the figure below Figure 2 4 To Condenser Condenser WasteH20 _ Naphtha Kero S_Retum PA 2 Retum Kero _Energy PA Cooler Kero _BoilUp KeroS _Reb Kero _ToReb rr a gt PAB_0 Cooler Diesel _Retum PA_3_Retum PR_3_Cooler PA_3_Draw Tower Feed Trim Duty DieselSS_Draw q AGOSS_Retum Diesel Steam Die
233. e regenerated in a 18 tray distillation column with a condenser and reboiler The ACID GAS will be rejected from the top and the regenerated DEA will be send back to the DEA CONTACTOR G1 5 Steady State Simulation Before the amine contactor can be solved an estimate of the lean amine feed DEA TO CONT and the inlet gas stream SOUR GAS must be provided The DEA TO CONT stream will be updated once the recycle operation is installed and has converged DEA to Cont uses Mass fractions Sour Gas uses Mole fractions 01 3 1 Installing the DEA CONTACTOR Add Feed Streams Define the following material streams DEA TO CONT material stream inthis celhs Emere O Mame DEATOCONT Pressure ospa SOUR GAS material stream inthis eet Enters Mame somes Pressure 10000000 psa Molar Fow 5MMSCFD NeMoleFrec oos Has MoleFrac oo po Acid Gas Sweetening with DEA G1 7 Add a Separator Any free water carried with the gas is first removed in a separator operation V 100 Add and define the following separator operation Separator V 100 Tab Page In this cell ter Design Connections SOUR GAS Vapour Outlet GAS TO CONTACTOR Liquid Outlet FWKO Add an Absorber Column 1 Before installing the column select Preferences from the Tools menu On the Simulation tab ensure that the Use Input Experts checkbox is checked then close the view The contactor can now be installed 2 Install an
234. e 2nd Active Spec lt empty gt lt emply gt Return Stage Calculated Information Draw Stage lt empty gt 2_MainTS Return Temp lt empty gt Flow Rate lt empty gt lt empty gt Delete PA_1 Each cooled pump around circuit has two specifications associated with it The default Pump Around Specifications are circulation rate and temperature drop Dt between the liquid draw and liquid return For this example the Dt specification is changed to a Duty specification for the pump around cooler The pump around rate is 50 000 bbl day Ist Active 2nd Active Spec 6 Inthe empty cell under the PA_1_Rate Pa specification enter 5e4 P 1 Rate Pa lt empty gt 7 Double click in the blank space under the PA_1_Dt Pa specification and the Spec view appears In the Spec Type drop down list select Duty Notice the negative sign convention indicates cooling in the Spec Value cell enter 55e6 Figure 2 97 Ni Pump Around Spec PA_1_Duty BG EG Spec Type Duty PA_1_Duty Pa Name PA 5 500e 007 Btu hr E Parameters Spec Type Delete 2 80 1 Click the Add button Refining Tutorial 2 81 10 Click the Close icon to return to the Pump Around view Figure 2 98 Nil Pump Around PA_1 ist Active 2nd Active Spec PA_1_Fate Pa PA 1_Duty Pa 5 500e 00 Btu hr Return Stage 1_ Main TS A F Calculated Information AQUE Draw Stage lt empt
235. e Basis button and choosing another Composition Basis radio button 28 Click the Conditions page to view the calculated stream properties You can display the properties of all phases by resizing the property view at oe 29 Place the cursor over the right border of the view The cursor changes to a double ended sizing arrow EN GA 30 With the sizing arrow visible click and drag to the right until the horizontal scroll bar disappears making the entire table visible Figure 3 44 Water Feed j Worksheet Stream Name Water Feed Aqueous Phase ae Vapour Phase Fraction 0 00000 1 00000 bosss Temperature F pwj 76 000 Properties Pressure psia 16 170 16 170 61 060 61 060 1100 0 1100 0 K Value Std Ideal Liq Vol Flow USGPM f 2 2013 2 2013 User Variables Molar Enthalpy Btu Ibmole 1 225e 005 1 225e 005 Molar Entropy Btu Ibmole F 1 4989 1 4989 Composition die Heat Flow Btu hr 7 4813e 06 7 4813e 06 Cost Parameters Lig Vol Flow Std Cond barrel day 74 251 74 251 Fluid Package Basis 1 a Worksheet Attachments Dynamics L EL S S eae Define from Other Stream New or updated information In this case the aqueous phase is identical to the overall phase is automatically and instantly transferred among all 31 Close the Water Feed property view to return to the Workbook locations in HYSYS 3 36 Workboo
236. e Control Valve button The FCV for C3Duty appears 6 Inthe Duty Source group select the Direct Q radio button 7 Inthe Direct Q group enter the following details The values shown here do not use the default units Enter the values then select the correct units from the drop down list Min Available O Btu h HYSYS automatically converts Max Available 2 x 10 Btu h the values to the default units Close the FCV for C3Duty view Click the Face Plate button Change the controller mode to Auto on the face plate view then close the view In this cell Enter 10 Enter the Depropanizer Column sub flowsheet environment 11 Add a PID Controller operation that will serve as the Depropanizer Top Stage temperature controller 12 In the controller property view specify the following details Tab Page In this cell Enter oes correct temperature units from 130 F the units drop down list Ensure that you select the 13 Click the Control Valve button The FCV for CondDuty view appears 14 In the Duty Source group select the Direct Q radio button 1 125 1 126 Dynamic Simulation 15 in the Direct Q group enter the following details Ensure that you select the In this cell Enter correct units from the units drop down list Min Available 0 Btu h Max Available 3x10 Btu hr 16 17 18 19 20 21 2 Close the FCV for CondDuty view Click the Face Plate button T
237. e Normalizing feature is useful when you know the relative ratios of components 2 parts N2 2 parts CO2 etc Rather than manually converting these ratios to fractions summing to one enter the numbers of parts for each component and click the Normalize button HYSYS computes the individual fractions to total 1 0 Normalizing is also useful when you have a stream consisting of only a few components Instead of specifying zero fractions or flows for the other components enter the fractions or the actual flows for the non zero components leaving the others lt empty gt Click the Normalize button and HYSYS forces the other component fractions to zero These are the default Calculation As you input the composition the component fractions or flows colours yours can appear status colour initially appear in red indicating the final composition is unknown differently depending on These values become blue when the composition has been your settings on the Colours calculated Three scenarios result in the stream composition being page of the Session calculated Preferences view Input the fractions of all components including any zero components such that their total is exactly 1 0000 then click the OK button Input the fractions totalling 1 000 flows or relative number of parts of all non zero components then click the Normalize button then the OK button Input the flows or relative number of parts of all components including
238. e Reactor Prods property view change the value in the Temperature cell to 180 HYSYS automatically recalculates the flowsheet The new results appears below ioj x 101x 4 Key Variables Dz Variable Reactor ReactorT emp 180 0 F Worksheet Stream Name pose Coolant CooolingDuty 4 1112 006 ea _ Conditions Tapout nese Taction n Glycol GlycolProduction 745 5 barrel day Properties 16 166 KI PI aa Molar Flow lbmole hr JAH position Vien A Mass Flow lb hr 19712 __ VewDaaBok K Value Std Ideal Liq Vol Flow USGPM 38 565 User Variables Molar Enthalpy Btu Ibmole 1 41 7e 005 N Molar Entropy Btu lbmole F 6 2394 nor Heat Flow Btu hr 8 6728e 07 Cost Parameters Lig Vol Flow Std Cond barrel day 1414 7 Fluid Package Basis 1 b Worksheet SESS eae Delete Define from Other Stream gt gt Dynamics 3 74 Chemicals Tutorial 7B Tutorial 3 75 As a result of the change the required cooling duty decreased and the glycol production rate increased 34 Click the Close button on the Reactor Prods stream property view to return to the Databook You can now record the key variables in their new state 35 Click on the Data Recorder tab in the Databook 36 Click the Record button The New Solved State view appears 37 In the Name for New State field change the name to 180F Reactor then
239. e Specific OK Case Main DewPoint Vapour Mass De Propanizer COL1 Chiller Yapour Mass Flow Add De Propanizer Vapour Molar Flow 3 Gas Gas Vapour Moles Object Filter InletSep Vapour To Liquid Hee All LTS Vapour Yolume MIc 100 Vapour Volume Flow e forall MIX 101 Vessel Diameter Q UnitOps Navigator Scope Vessel Geometry Cyli C Logicals laare Vessel Length or Heic C ColumnOps Vessel Mole Frac Custom A Case Vessel Pressure Basis Vessel Pressure Drop Custom ic Utility Vessel Temperature i mm Volume Fixed Order Volume Sorted by D Vessel Temperature Cancel Variable Description 1 79 1 80 Steady State Simulation 7 Click the OK button to add this variable to the Databook The new variable Vessel Temperature appears in the Databook Figure 1 102 DataBook Available Data Entries Object Variable Vessel Temperature Variables Process Data Tables Strip Charts Data Recorder Case Studies Continue adding variables to the Databook 8 Click the Insert button and the Variable Navigator reappears 9 Inthe Object Filter group select the Streams radio button The Object list is filtered to show streams only 10 In the Object list select SalesDP The Variables list available for material streams appears to the right of the Object list 11 In the Variable list select Temperature 12 In the Variable Description field change description to Dew Point
240. e column environment a PFD icon 1 Click the Column Environment button at the bottom of the column property view Workbook icon 2 While inside the column environment you might want to e view the Column sub flowsheet PFD by clicking the PFD icon e view a Workbook of the Column sub flowsheet objects by clicking EN the Workbook icon e access the inside column property view by clicking the Column Runner icon This property view is essentially the same as the outside or Main Flowsheet property view of the column Column Runner icon The Column sub flowsheet PFD is shown below Figure 2 115 To PA 1_Q Cooler eenencet Condenser PA_1_Return KeroSS_Return Naphtha A 1 Cooler PA_1_Draw PA_2_ Q Cooler PA_2 Return PA 2 Cooler PA Draw PA_3_ Coole PA_3_Return ae PA_3_Draw KeroSS_Draw KeroSS_Eneray KeroSS_Reb ir Kerosene CTR Diesel DieselSS Tower Feed AGOSS_Return Trim AGOSS_Draw Duty 2 a p E z E z z Residue Bottom Steam AGO Steam 2 93 Maximize icon Steady State Simulation Customizing the Column PFO You can customize the PFD shown above by re sizing the column and hiding some of the column trays to improve the overall readability of the PFD To hide some of the trays in the main column 1 Click the PFD icon to ensure the column PFD is active 2 Click the Maximize icon in the upper r
241. e following three equilibrium reactors as shown below Equilibrium Reactor Combustor Shift Tab Pagel inthis cell Enter Design Connections Mid Combust Mid Com Liq Equilibrium Reactor Shift Reactor 1 Design Connections Shifti Feed Design Parameters Optional Heat Cooling Transfer Worksheet Conditions Shift2 Feed 850 F Temperature Reactions Details Shift Rxn Set Equilibrium Reactor Shift Reactor 2 Tab Page inthis cells Enter Design Connections Design Parameters Optional Heat Cooling Transfer Worksheet Conditions Synthesis Gas 750 F Temperature Reactions Details Shift Rxn Set C2 13 Steady State Simulation The same Adjust could be accomplished by selecting the temperature of the stream Shifti Feed C2 14 Ce 3 c Installing Adjust Operations Steam flow Rate To control the temperature of the combustion reaction the flow rate of steam to the Combustor is adjusted Since the Combustor is modeled as two separate reactors the temperature of the equilibrium reactor Combustor Shift is targeted An ADJUST operation is used to manipulate the Comb Steam flow rate to maintain the Combustor Shift temperature at 1700 F Adjust ADJ 1 Tab In this cell Enter Connections Adjusted Object Adjusted Variable Molar Flow Target Object Combustor Shift Sepse somom Click the Start button to begin the Adjust operation Air Flow Rate To control the H N mola
242. e input cell for the first component H20 2 42 Refining Tutorial The Input Composition for 3 Since the stream is all water type 1 for the H20 mole fraction then Stream view is Modal press ENTER The Input Composition for Stream view appears indicated by the absence of allowing you to complete the compositional input the Minimize Maximize icons in the upper right corner When a Modal view is visible you are unable to move outside the view until you are finish with it by clicking either the Cancel or ropane OK button LONN Figure 2 45 Si Input Composition for Stream Bottom Steam Composition Basis Mole Fractions Mass Fractions ABE co Co fy m C Lig Volume Fractions C Mole Flows Mass Flows C Lig Volume Flows Pentane Composition Controls Erase Normalize NBPIOIee e Cancel SSNS Sj Sj S SSS 2 2 5 Do oo o0 oloo DDD DUD a oloo oloo EE EE rE Sie Go Pere Poe brs bd Ro co ao Fafa BoM Fat Po x x x x x x The Input Composition for Stream view allows you to specify a stream composition quickly and easily The following table lists and describes the features available on this view Features Description Compositional You can input the stream composition in some fractional basis other Basis Radio than Mole Fraction or by component flows by selecting the Buttons appropriate radio button before providing your input Normalizing Th
243. e pop up visible left click and hold The white box again becomes solid black 3 49 Steady State Simulation TA Break Connection Icon If you make an incorrect connection break the connection and try again 1 Click the Break Connection icon on the PFD tool bar Place the cursor over the stream line you want to break The cursor shows a checkmark indicating an available connection to break Click once to break the connection 3 50 9 Move the cursor to the right of the CSTR 100 A stream icon appears with a trailing line attached to the CSTR 100 outlet The stream icon indicates that a new stream will be created when you complete the next step Figure 3 62 Mixer Out ij CSTR 100 10 With the stream icon visible release the left mouse button HYSYS creates a new stream with the default name 1 11 Place the cursor over the bottom right connection point on the reactor labeled Liquid Product then click and drag to the right to create the reactor s liquid product stream The new stream is given the default name 2 12 Place the cursor over the bottom left connection point on the reactor labeled Energy Stream then click and drag down and to the left to create the reactors energy stream The new stream is automatically named Q 100 The reactor displays a yellow warning status indicating that all necessary connections have been made but that the attached streams are not e
244. eams table by clicking on the lt lt Stream gt gt cell in the table or by pressing TAB 5 Open the drop down list of available feeds by clicking it or by pressing F2 then the Down or Up arrow key 6 Select TowerFeed as the inlet feed stream to the column HYSYS will supply a default feed location in the middle of the Tray Section TS in this case stage 5 indicated by 5_Main TS This default location is used so there is no need to change the Feed Stage This column has Overhead Vapour and Bottoms Liquid products but no Overhead Liquid distillate product 7 Inthe Condenser group select the Full Rflx radio button The distillate stream disappears This is the same as leaving the Condenser as Partial and later specifying a zero distillate rate 8 Enter the stream and Column names as shown in the figure below When you are finished the Next button becomes active indicating sufficient information has been supplied to advance to the next page of the Input Expert Figure 1 81 Ni Distillation Column Input Expert Condenser Energy Stream CondD uty Condenser C Total aa Column Name D ePropanizer C Partial Ovhd Vapour Outlet Full Afls Inlet Streams Inlet Stage i lt lt Stream gt gt t Reboiler Energy Stream RebDuty Bottoms Liquid Outlet Stage Numbering LiquidProd Top Down C Bottom Up HE Next gt Connections page 1 of 4 Cancel Gas Processing Tutorial
245. eave Oil Environment icon 2 34 Steady State Simulation 3 Type the name Preheat Crude then press the ENTER key HYSYS creates a new stream named Preheat Crude in the flowsheet associated with the fluid package associated with this oil Figure 2 34 Si Oil Characterization Oil Install Information p OIName Ready Install SteamName Flow Sheet Blendi M M Preheat Crude Case Main iz Assay Cut Blend User Property Correlation Install Oil Refinery Assay Clear All Calculate All Oil Output Settings Return to Basis Environment In this case there is only one fluid package Basis 1 and one flowsheet the main flowsheet so the stream is created in the main flowsheet HYSYS assigns the composition of the calculated oil and light ends to stream Preheat Crude The properties of the new stream can be viewed from the Simulation environment The characterization procedure is now complete 4 Return to the Basis environment by clicking the Leave Oil Environment icon 5 Click the Components tab of the Simulation Basis Manager view Select Component List 1 from the list in the Component Lists group Click the View button to open the component list property view Press and hold the CTRL key to select more than one component Refining Tutorial 7 The hypocomponents generated during the oil characterization procedure now appear in the Selected Component
246. ection icon in the PFD toolbar e Position the mouse pointer over the SepLig stream to the right of the stream arrow e When the mouse pointer has a checkmark beside it left click and the stream will disconnect from the MIX 101 17 Open the Object Palette by pressing F4 18 On the Object Palette right click and hold on the Valve icon 19 While holding the right mouse button drag the cursor over the PFD The mouse pointer becomes a bullseye Valve icon 20 Position the bullseye pointer beside the SepLiq stream and release the mouse button 21 A Valve icon named VLV 100 appears 22 Double click the VLV 100 icon on the PFD to open its property view 23 In the valve property view specify the following connections Tab Page In this cell Enter Design Connections Sep Valve 1 101 1 102 Dynamic Simulation 24 Click the Close icon to close the valve property view l 25 Connect the SepExit stream to the inlet of the MIX 101 unit Hi operation by doing the following ae e Click the PFD Attach Mode icon e Position the mouse pointer at the tip of the SepExit stream arrow A white box appears e Click and drag the pointer to the left side of MIX 101 A white box appears indicating a connection point e Release the mouse button to complete the connection e Click the Attach Mode icon again to exit from the attach mode Attach Mode icon Next you will insert a valve operation between t
247. ections page for the Mixer 6 In the Inlets table click in the lt lt Stream gt gt cell The status indicator at the bottom of the view indicates that the operation needs a feed stream 3 38 Chemicals Tutorial 3 39 7 Open the drop down list of inlets by clicking on or by pressing the F2 key then SPACEBAR Figure 3 47 MIX 100 Design Name Mix 00 Connections Parameters User Yariables Notes Inlets Outlet 7 v Prop Oxid Fhid Package Basis 1 Rating Worksheet Dynamics Delete k M Ignored Alternatively you can 8 Select Prop Oxide from the drop down list The Prop Oxide stream E e appears in the Inlets table and lt lt Stream gt gt automatically moves name in the lt lt Stream gt gt down to a new empty cell Cey MER pressing ENTER 9 In the Inlets table click the new empty lt lt Stream gt gt cell and select Water Feed from the list The status indicator now displays Requires a product stream 10 Move to the Outlet field by pressing TAB or by clicking in the cell 11 Type Mixer Out in the cell then press ENTER HYSYS recognizes that there is no existing stream with this name so it creates the new stream Figure 3 48 MIX 100 Design Name Mix 00 Connections Parameters User Variables Notes Inlets Outlet Prop Oxide Mixer Qui Water Feed Fluid Package E asis 1 Rating Worksheet Dynamics Delete TE oroi
248. ed for these side strippers are identical to the names of the utility steam streams that were created previously in the Main Flowsheet The conditions of these Steam Feed streams which reside in the Column sub flowsheet are unknown at this point The conditions of the Main Flowsheet streams are duplicated into these sub flowsheet streams when the stream attachments are performed The completed Side Stripper Summary table appears below Figure 2 94 Side Stripper Summary Outlet Flow Reboiler Duty 9_MainTS 8_MainTS lt empty gt lt empty gt 3 3 17_Main TS 16_Main TS lt empty gt lt empty gt 3 22 Main TS 21_ Main TS lt empty gt lt empty gt 13 Click the Design tab and select the Monitor page The Specifications table on this page has a vertical scroll bar indicating that new specifications have been created below the default ones Resize the view to examine the entire table 2 8 The addition of the side strippers has created four more degrees of freedom above the basic column resulting in a total of seven available degrees of freedom Currently however seven Specifications are Active so the overall Degrees of Freedom is zero Refining Tutorial 14 Click and drag the bottom border of the view down until the scroll bar disappears making the entire matrix visible Figure 2 95 Specifications E Distillate Rate Yap Prod Rate Reflux Ratio Current Value lt empty gt
249. ed so that the MIX 100 unit operation can calculate it s pressure based on the Prop Oxide stream specification 8 Double click the Water Feed stream icon to open its property view 9 On the Conditions page of the Worksheet tab click in the Pressure cell then press DELETE Dynamic Simulation 10 Close the Water Feed stream property view 11 Double click the MIX 100 icon to open its property view 12 Click the Design tab then select the Parameters page 13 In the Automatic Pressure Assignment group select the Equalize All radio button HYSYS solves for the stream and mixer operation 14 Close the mixer property view 15 Save the case 3 3 2 Using the Dynamics Assistant The Dynamics Assistant makes recommendations as to how the flowsheet topology should change and what pressure flow specifications are required in order to run a case in dynamic mode In addition it automatically sets the sizing parameters of the equipment in the simulation flowsheet Not all the suggestions the Dynamics Assistant offers need to be followed Figure 3 105 Ni Dynamics Assistant Make changes Disable stream pressure specifications Disable stream flow specifications Append new valves and streams About Preferences a General Streams Analyze Again The Dynamics Assistant will be used to do the following e Add Pressure Flow specifications to the simulation case e Add Valves to the Boundary
250. ee different states for the object Indicator Status Description Red Status A major piece of defining information is missing from the object For example a feed or product stream is not attached to a Separator The status indicator is red and an appropriate warning message appears Yellow Status All major defining information is present but the stream or operation has not been solved because one or more degrees of freedom is present for example a Cooler where the outlet stream temperature is unknown The status indicator is yellow and an appropriate warning message appears Sons seus earar geen anda OK message appa status indicator is green and an OK message appears When you are working in the PFD the streams and operations are also colour coded to indicate their calculation status The mixer and inlet separator are completely calculated so they have a black outline For the heat exchanger Gas Gas however the conditions of the tube side outlet and both shell side streams are unknown so the exchanger has a yellow outline indicating its unsolved status A similar colour scheme is used to indicate the status of streams For material streams a dark blue icon indicates the stream has been flashed and is entirely known A light blue icon indicates the stream cannot be flashed until some additional information is supplied Similarly a dark red icon indicates an energy stream with a known duty while a purple icon indicat
251. eeeeeeeeeeeeeens 13 X1 1 RR CaseLinking 2 Case Linking X1 2 Case Linking X1 3 XI Process Description This example uses the User Unit Operation to link two HYSYS cases together such that changes made to the first case LinkCase1 are automatically and transparently propagated to the second LinkCase2 This application demonstrates a method for copying the contents of a stream from one case to another automatically Figure X1 1 _ rich gas _ cooled_vap op 100 K 100 feed_vap precooled W101 expanded cold_vap compressed gt cooled _lig cold _lig2 cold_liq feed_liq shaft work The User Unit Op is pre configured with Visual Basic code Inside the User Unit Op you will define two subroutines e Initialize macro The Initialize macro sets the field names for the various stream feed and product connections and creates the following two text user variables e LinkCase contains the path and file name of the target case to be linked If the variable contains no value the Initialize code will set it to be the path to the currently open case and the file name LinkCase2 hsc e LinkStream names a stream in the second case that will have the T P Flow and composition copied to it from the User Unit Op s feed stream The target case and stream may optionally be changed explicitly from the Variables page of the User Unit Op e Execute macro The Execute
252. el Varnable Ie o Exportable a Variable Angles im ae a re a a a Component Mole Fraction Comp Heat Value Total Heat Value 1 90 Gas Processing Tutorial 81 Processing Tutorial 1 91 Importing Variables Second Method The next task is to import the remaining two variables mole fractions in the Sales Gas 1 Position the cursor over the empty Spreadsheet cell B6 reserved for the iC4 mole fraction Vien Associated Obieck 2 Right click once From the menu that appears select Import Import Variable Variable The Select Import for cell view appears Export Formula Result Bees eae 3 Select the SalesGas Object Comp Mole Frac Variable and i Butane Variable Specific Click the OK button to accept the input and close the view Import the mole fraction for nC4 e Position the cursor over cell B7 e Right click once and select Import Variable e Select the SalesGas Object Comp Mole Frac Variable and n Butane Variable Specific Entering Formulas The next task is entering the formulas for calculating the component and total sales gas heating values 1 Click in cell D3 Ailfonnulaktnueube 2 Type b3 c3 then press ENTER This multiplies the Methane mole preceded by a fraction by its Net Heating Value 3 Enter the following formulas in cells D4 through D7 Cell ere aanlel ts pe bere 1 92 Steady State Simulation 4 The table should appear as shown in the figure below
253. elect the components 1 Onthe Component List Selection drop down list select Component List 1 if it is not already selected 2 Click the View button The Component List View appears Figure 1 12 Component List View Efe x Add Component Selected Components Components Available in the Component Library Components Match i tis View Filters Traditional Electroly te Sim Name C Full Name Z Synonym C Formula Hypothetical Other lt Add Pure Methane Ethane Propane lt Substitute gt Butane n Butane i Pentane i n Pentane n Hexane n Heptane Sort List n Octane n Nonane n Decane n C11 n C12 J Show Synonyms Cluster Selected Component by Type Component List 1 There are a number of ways to select components for your simulation One method is to use the matching feature Each component is listed in three ways on the Selected tab Matching Method Description SimName The name appearing within the simulation FullName Synonym IUPAC name or similar and synonyms for many components The chemical formula of the component This is useful when you are unsure of the library name of a component but know its formula At the top of each of these three columns is a corresponding radio button Based on the selected radio button HYSYS will locate the component s that best matches the input you type in the Match cell Gas Processing Tutorial 1 13 For this tutorial you
254. emperature of CoolGas as 42 9 F All streams in the flowsheet are now completely known 8 Click the Performance tab then select the Details page where HYSYS displays the Overall Performance and Detailed Performance Figure 1 75 m Gas Gas Overall Performance Duy sd 4 705e 05 Btu hr Heat Leak 0 000e 01 Btu hr Performance Details Plats Heat Loss ___0 000e 07 Btu hr_ Tables UA 2 08e 04 Btu F hr Min Approach 10 000 F LMTD Error Msg Detailed Performance UA Curvature Error 0 0000 Btu F hr_ Hot Pinch Temp i Cold Pinch Temp R REEE E Ft Factor SESE Uncorrected LMTD ners lt empty gt Design Rating Worksheet Performance Dynamics HTFS TASC Delete Nr T Ignored Two parameters of interest are the UA and Lmtd logarithmic mean temperature difference which HYSYS has calculated as 2 08e4 Btu xF hr and 22 6 E respectively 9 When you are finished viewing the results click the Close icon to leave the Gas Gas property view Cheching the Sales Gas Dew Point The next step is to check the SalesGas stream to see if it meets a dew point temperature specification This is to ensure no liquids form in the transmission line A typical pipeline dew point specification is 15 F at 800 psia which will be used for this example You can test the current dew point by creating a stream witha composition identical to SalesGas specifying the dew poin
255. empty gt Not Spec d Critical Point TDep UserProp Delete Edit Properties Edit Vise Curve Chemicals Tutorial IB Tutorial 3 15 The Component property view provides you with complete access to the pure component information for viewing only You cannot modify any parameters for a library component however HYSYS allows you to clone a library component into a Hypothetical component which can then be modified as desired Refer to Chapter 3 Hypotheticals in the Simulation Basis manual for more information on cloning library components 3 Close the individual component view then close the Component List View to return to the Fluid Package Providing Binary Coefficients The next task in defining the Fluid Package is providing the binary interaction parameters 1 Click the Binary Coeffs tab of the Fluid Package view Figure 3 17 Fluid Package Basis 1 Activity Model Interaction Parameters Coeff Estimation UNIFAC VLE C UNIFAC LLE L 12030xide 12 C3diol H20 d o C Immiscible 71 909 _ 335 033 __Individual Pair l 4 l Unknowns Only ALL Binaries R 1 98721 cal gmol K Coeff Matrix To View Ai 823 550 5 027 In the Activity Model Interaction Parameters group the Aij interaction table appears by default HYSYS automatically inserts the coefficients for any component pairs for which library data is available You can
256. en 7 C1 3 gt Draw Strearn Location 2 1 B aaaea 12 C1 4 ARESUIIS cccccccnnneinncttll N oan cpg cccccnssssccnnssssscennensssess 13 C1 1 OR than Plant 2 Ethanol Plant To see this case completely solved see your HYSYS Samples directory and open the C 2 hsc file Ethanol and Water form an azeotropic mixture at 1 atm Therefore with simple distillation the ethanol and water mixture can only be concentrated up to the azeotropic concentration Ethanol Plant on FX Cl 1 Process Description Figure C1 1 CO2_Stream WWash_H20 am Light_Vent To_CO2VWash gt CondDuty _ _ To_Fermentor gt 2ndEtoH FromFerm CO2_Yent amp Rect vap To_Light To_Rect Reci Cond Rect_Dist Rect_Feed stProd Fisel 4 Rect_Reb p SteamA gt StillageB Stillage_A Typically an ethanol fermentation process produces mainly Ethanol plus small quantities of several by products methanol 1 propanol 2 propanol 1 butanol 3 methyl 1 butanol 2 pentanol acetic acid and COs The CO produced in the fermentation vessel carries some ethanol This CO stream is washed with water in a vessel CO2 Wash to recover the Ethanol which is recycled to the fermentor Figure C1 2 CO2 Stream p Wash_H20 To _CO2Wash To_Fermentor Ch Process Description Process Description Fusel oils are a mixture of propanols butanols and
257. en the Tools menu and Select Databook The Databook appears as shown below Figure 1 99 4 DataBook Available Data Entries Object Variable Insert E Variables Process Data Tables Strip Charts Data Recorder Case Studies 2 Click the Variables tab Here you will add the key variables to the Databook The Variable Navigator is used extensively in HYSYS for locating and selecting variables The Navigator operates in a left to right manner The selected Flowsheet determines the Object list the chosen Object dictates the Variable list the selected Variable determines whether any Variable Specifics are available Gas Processing Tutorial 1 79 3 Click the Insert button The Variable Navigator view appears Figure 1 100 Yariable Navigator Ioj Xx Flowsheet Object Variable Case Main DePropanizer COL1 id Object Filter All C Streams C UnitOps Navigator Scope C Logicals Flowsheet Ovhd ColumnOps C Case Custom C Basis Custom Utility Esm Variable Description In the Object Filter group select the UnitOps radio button The Object list will be filtered to show unit operations only In the Object list select LTS The Variable list available for the LTS appears to the right of the Object list In the Variable list select Vessel Temperature HYSYS displays this variable name in the Variable Description field _ ol x Flowsheet Object Variable Variabl
258. encies for stages 1 18 only 2 Select the Component radio button in the Efficiency Type group Parameters tab Efficiencies page then click the Reset H2S CO2 button Type the new efficiencies into the matrix 4 Specify a Damping Factor of 0 40 Parameters tab Solver page to provide a faster more stable convergence Distillation Column Regenerator DFE Finis cel Enters 1 0 Reboiler Parameters Solver Damping Factor 5 Add two new column specifications called Reboiler Duty and T Top Design tab Specs page Set the default specifications as shown below Delete the Reflux Rate and REGEN Bttms Rate specifications from the Column Specification list in the Column property view Regenerator Specifications Tab Page Inthis cel Enters Design Specs Name T Top Stage Condenser Spec Value 179 6 F Name Reboiler Duty Energy Stream RBLR Q COL2 Spec Value 1 356e7 BTU hr Name Reflux Ratio Stage Condenser Flow Basis Molar Spec Value 0 5 Name Ovhd Vap Rate Draw ACID GAS COL2 Flow Basis Molar Spec Value 2 0 MMSCFD G1 11 G2 Steady State Simulation 2 Steady State Simulation 8 Set the T Top and Reboiler Duty specifications to Active the Reflux Ratio and Ovhd Vap Rate specifications should be set as Estimates only The reboiler duty is based on the guidelines provided below which should provide an acceptable H2S and CO2 loading in the lean amine Recommended Steam Rates Ib Steam USGAL Lean A
259. eng Robinson and Soave Redlich Kwong Equations of State to ensure that these methods correctly model this system Figure P1 2 Condenser Duty To Condenser a L Reflux Condenser Propene Rectifier Reboiler To Reboiler Propane P1 3 PS tap 4 Setup P1 4 These splitters have many stages and are often built as two separate columns This simulation will contain two Columns a Stripper and a Rectifier The Stripper is modeled as a Reboiled Absorber and contains 94 theoretical stages The Rectifier is a Refluxed Absorber containing 89 theoretical stages The Stripper contains two feed streams one is the known stream FEED and the other is the bottoms from the Rectifier Propane is recovered from the Stripper bottoms 95 and Propene is taken off the top of the Rectifier 99 There are two basic steps in this process simulation Setup The Soave Redlich Kwong SRK property package will be used and the component list includes Propane and Propene Steady State Simulation The case will consist of a column divided into two tray sections a Refluxed Absorber as a Rectifier and a Reboiled Absorber as a Stripper Plc Setup Create a new HYSYS case Set the unit preferences to Field From the Tools menu select Preferences The Session Preferences view appears On the Variables tab Units page select Field from the Available Unit Sets list Close the Session Preferences view Create a component list containi
260. ent icon in the toolbar 51 Close the DePropanizer column property view The ADJ 1 and Dewpoint logical operations have calculated the Cold Gas stream temperature required to achieve a 10 F dewpoint in the SalesGas stream 52 In the PFD double click the ColdGas icon to open the stream property view Figure 1 133 ColdGas Stream Name Se e ColdGas Vapour Phase Fraction AE Sa Temperature F 4 4332 Pressure psia Molar Flow Ibmole hr 985 64 Mass Flow lb hr K Value Std Ideal Lig Vol Flow barrel day Molar Enthalpy Btu Ibmole Molar Entropy Btu Ibmole F Notes Heat Flow Btu h 3 7564e 07 Cost Parameters Liq Vol Flow StdCond barel day lt empty gt Fluid Package Basis 1 Worksheet Conditions Properties Composition User Variables E Worksheet Dynamics OR Delete Define from Other Stream lt a gt 53 Record the temperature of the ColdGas material stream so that it may be controlled in Dynamic mode VEUF lol Value Cold Gas Stream Temperature 4 43 F 54 Close the ColdGas property view 55 On the PFD click on the ADJ 1 logical operation icon then press the DELETE key HYSYS prompts you to confirm that you want to delete the object Click the Yes button 56 Delete the Dewpoint logical operation and the SalesDP material stream from the PFD 57 From the File menu select Save As Save the file as DynTUT1 1 hsc Gas Proce
261. er Bottoms This new stream Stripper Feed enters on tray 3 of an 8 tray distillation tower with a reboiler and a total reflux condenser A quality specification of 10 ppm wt ammonia on the tower bottoms Stripper Bottoms is specified The tower bottoms Stripper Bottoms exchanges heat with the incoming feed and exits as Effluent There are two basic steps in this process simulation 1 Setup This case uses the Sour Peng Robinson package and the following components H2S NH3 and H20 2 Steady State Simulation The case will consist of an 8 stage stripper used to separate H2S and NH3 and a heat exchanger to minimize heat loss Ae Setup Select the following components H2S NH3 and H20 2 Select the Sour Peng Robinson property package It combines the PR equation of state and Wilson s API Sour model for handling sour water systems 3 Set the units to Field in the Session Preferences Tools menu Sour Water Stripper R2 5 Ae 4 Steady State Simulation The following general steps will be taken to setup this case in steady state 1 Installing the SW Stripper An 8 stage distillation column will be used to strip the sour components from the feed stream The liquid leaving the bottom of the column heats the incoming feed stream in a heat exchanger 2 Case Study A case study will be performed to obtain steady state solutions for a range of stripper feed temperatures Ae 4 1 Installing the SW Stripper Feed St
262. er group is currently selected so only the Unit Operations appear in the list of objects To open a property view select the operation in the list then click the View button or double click on the operation name You can also search for an object by clicking the Find button When the Find Object view appears enter the object name then click the OK button HYSYS opens the property view for the object you specified 3 67 3 68 Steady State Simulation To edit any of the Objects in the Databook 1 Select the Object you want to edit 2 Click the Edit button 3 68 Using the Databook The HYSYS Databook provides you with a convenient way to examine your flowsheet in more detail You can use the Databook to monitor key variables under a variety of process scenarios and view the results in a tabular or graphical format 1 Before opening the Databook close the Object Navigator and any property views you might have opened using the Navigator 2 To open the Databook do one of the following e Press CTRL D e From the Tools menu select Databook The Databook view appears Figure 3 89 DataBook Available Data Entries Object Variable Ea Variables Process Data Tables Strip Charts Data Recorder Case Studies The first task is to add key variables to the Databook For this example the effects of the Reactor temperature on the Reactor cooling duty and Glycol production rate will be examined
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264. es an unknown duty 1 51 1 51 Steady State Simulation Installing the Chiller In this section you will install a chiller which will be modeled as a Cooler In this example you will install the operation by dropping it from the Object Palette onto the PFD Adding the Chiller to the PFD 1 Ensure that the Object Palette is visible if it is not press F4 The Chiller will be added to the right of the LTS so make some empty space available in the PFD by scrolling to the right using the horizontal scroll bar 7 2 Click the Cooler icon on the Object Palette If you click the wrong H Cooler icon button click the Cancel icon 3 Position the cursor over the PFD The cursor changes to a special eanesiicon cursor with a plus symbol attached to it The symbol indicates the location of the operation icon Figure 1 63 LTSVap SepvVap us _ CoalGas GasiGas SalesGas InletSep MixerOut MIX 100 Lu SepLiq Lu When you are in Attach mode 4 Click on the PFD where you want to drop the Cooler HYSYS you will not be able to move creates a new Cooler with a default name E 100 The Cooler has a epee MINE Sr Dro retur red status and colour indicating that it requires feed and product to Move mode click the Attach icon again You can streams temporarily toggle between Attach and Move mode by holding down the cTRL key Connecting the Chiller LTS Vap a F g 1 Click
265. es the possibility of cycling behaviour if the Simultaneous method is used Therefore it is advantageous to attempt to iterate on one Adjust and then solve the other C2 15 Bs gt 2 4 Results Workbook Case Main Energy Streams Tab Figure C2 5 Shift O 7 349e 006 Shift2 0 1 282e 006 Name 00 Reformer Q Heat Flow Btu h 2 238e 007 Material Streams Tab Figure C2 6 Comb Steam Combustor Feer Mid Combust Natural Gas Reformer Stearr Air Reformer Lig C2 16 Vapour Fraction 1 0000 1 0000 1 0000 1 0000 1 0000 0 0000 1 0000 Temperature F Pressure psia Molar Flow Ibmole hr Mass Flow Ib hr Liquid Volume Flow barrel day 700 0 500 0 200 0 733 8 _ 3209 475 0 500 0 520 0 9368 642 7 60 00 500 0 107 2 3092 244 7 475 0 500 0 55 22 994 8 68 26 1700 500 0 10 1 258e 004 1975 1700 500 0 0 0000 0 0000 0 0000 1479 500 0 1260 1 666e 004 2502 Heat Flow Btu hr Name Yapour Fraction Temperature F Pressure psia Molar Flow Ibmole hr 5 115e 006 Mid Liq 0 0000 Sse 500 0 0 0000 5 254e 007 Shit Feed 1 0000 1440 500 0 1260 2 5 4e 004 Mid Com Lig 0 0000 _1440 500 0 0 0000 5 580e 006 Shilt2 Feed 1 0000 _850 0 500 0 1260 3 528e 007 Shift Liq 0 0000
266. es you with complete access to the component information For pure components like H20 the information is provided for viewing only You cannot modify any parameters for a library pure component however HYSYS allows you to clone a library component into a Hypothetical component which you can then modify as required The petroleum hypocomponent shown here is an example of a hypothetical component You can modify any of the parameters listed for this component For this example the properties of the hypothetical components generated during the oil characterization are not changed 3 Close each of these two component property views 4 The fluid package is now completely defined so close the Component List view The Simulation Basis Manager view should again be visible if not click the Basis Manager icon to access it 5 Click the Fluid Pkgs tab to view a summary of the new fluid package Figure 2 37 Simulation Basis Manager Current Fluid Packages Flowsheet Fluid Pkg Associations Basis 1 NC 44 PP Peng Robinson View FlowSheet Fluid Pkg To Use Basis 1 Add Delete Copy Import E E Export Default Fluid Pkg Basis 1 v a OO a Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty The list of Current Fluid Packages displays the new fluid package Basis 1 showing the number of components NC and property package P
267. exit or move outside the Expert until you supply the necessary information or click the Cancel button 3 56 18 Click the Reactions tab again and check the conversion The conversion at 140 F is approximately 95 which is acceptable Reaction Results Summary C Reaction Balance BaseComp Ren Extent 12030xide 19 Close the Reactor property view Installing the Column HYSYS has a number of pre built column templates that you can install and customize by changing attached stream names number of stages and default specifications For this example a Distillation Column will be installed 1 Before installing the column click the Tools menu and select Preferences On the Simulation tab click on the Options page and ensure that the Use Input Experts checkbox is selected checked then close the view 2 Double click the Distillation Column icon on the Object Palette The first page of the Input Expert appears Figure 3 73 Ni Distillation Column Input Expert Condenser Energy Stream 7 Condenser Tf C Total Column Name T 1 00 haa Partial Ovhd Outlets Water Draw Inlet Streams Inlet Stage lt Stream gt gt Optional Side Draws o Reboiler Energy Stream Bottoms Liquid Outlet vv Stage Numbering Top Down C Bottom Up Connections page 1 of 4 Cancel When you install a column using a pre built template HYSYS supplies certain default information
268. fining Reactions In this example there are three conversion reactions and one equilibrium reaction Conversion Reactions The reforming reactions are as follows CH H O gt CO 3H C2 1 CH 2H O gt CO 4H C2 2 The combustion reaction is as follows CH 20 gt CO 2H O C2 3 Equilibrium Reaction The water gas shift reaction is as follows CO H 0 amp CO H C2 4 Synthesis Gas Production 1 Add the two reforming reactions and input the following data Reaction Rxn 1 Reaction Rxn 2 Tab inthiscell Enter Tab Intthisccell Enter Stoichiometry Component Stoichiometry Component Stoich Coeff Stoich Coeff Base Methane Base Methane Component Component 10 Co 30 Co 2 Add the combustion and equilibrium reactions and input the following data Reaction Rxn 3 e mths Stoichiometry Component Methane 1 Stoich Coeff Reaction Rxn 4 Oxygen 2 CO 1 Water 2 Base Methane Component 1 To add the Equilibrium reaction click the Add Rxn button The Reactions view appears Library Equilibrium Rxns ee 2 From the Reactions list select Equilibrium then click the Add SALUT aE Reaction button The Equilibrium Reaction view appears Ethylbenzene Styrene H2 ek eran a 3 Click the Library tab Add Library Ren 4 Inthe Library Equilibrium Rxns group select CO H20 CO2 H2 then click the Add Library Rxn button HY
269. freedom for this stream has now been used so HYSYS flashes ColdGas to determine its remaining properties 9 Click the Close button to return to the PFD The Chiller still has yellow status because the temperature of the CoolGas stream is unknown Figure 1 67 ColdGas Worksheet Stream Name ColdGas ES Vapour Phase Fraction BA 0 78182 onditions 0 00000 Properties 8 9765 Composition TSL a K Value Std Ideal Lig Vol Flow barrel day 4342 2 User Variables Molar Enthalpy Btu Ibmole ___3 823e 004 Molar Entropy Btu Ibmole F 33 423 a Heat Flow Btu hr _ 3 7685e 07 Cost Parameters Lig Vol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 a Worksheet Dynamics Delete Define from Other Stream lt a gt gt 10 Double click the energy stream icon Q 100 to open its property view The required chilling duty in the Heat Flow cell is calculated by HYSYS when the Heat Exchanger temperature approach is specified in a later section 1 56 Steady State Simulation um Separator icon Multiple connection points appear because the Separator accepts multiple feed streams V 100 m ColdGas R Feed Stream 11 Rename this stream C3Duty then close the view Figure 1 68 Energy Stream C3Duty Properties C3Duty Heat Flow Btu hr Ref Temperature F lt empty gt Installing the LTS Now that the chiller has been instal
270. ft 60 32 Max DP Tray psi i 0 082 Tray Spacing in Total weir Length in Weir Height in Active Area ft2 ars Design Performance Delete ES igncied VEUF Lol Value Section Diameter 2 5 ft Note the Max DP Tray value Tray Spacing 24 in on this page Total Weir Length 25 38 in You can view column profile information on the Tabl l Er a dii k 11 Click Design tab then select the Setup page Check the Active checkbox 12 On the Results page of the Performance tab click the Export Pressures button For now ignore any warnings by clicking the OK button 13 Close the Tray Sizing property view and the Available Utilities view 14 Double click the DePropanizer icon to open the Column property view Click the Column Environment button to enter the Column sub flowsheet 1 110 Gas Processing Tutorial tT Processing Tutorial 1 111 15 In the column PED double click the Main TS Column object to open the Main TS property view 16 Click the Rating tab then select the Sizing page 17 Enter the tray section parameters as follows Be aware that the units for each tray section parameter may not be consistent with the units appearing in the tray sizing utility Use the drop down list to select the units you want to input HYSYS automatically converts the value to the default unit VEUF lol Value Section Diameter 2 5 ft 24 in Total Weir Lengt
271. g these ratios to fractions summing to one simply enter the individual numbers of parts and click the Normalize button HYSYS computes the individual fractions to total 1 0 Normalizing is also useful when you have a stream consisting of only a few components Instead of specifying zero fractions or flows for the other components simply enter the fractions or the actual flows for the non zero components leaving the others lt empty gt Click the Normalize button and HYSYS forces the other component fractions to zero As you input the composition the component fractions or flows initially appear in red indicating the final composition is unknown These values become blue when the stream composition is calculated Three scenarios result in the stream composition being calculated e Input the fractions of all components including any zero components such that their total is exactly 1 0000 Click the OK button e Input the fractions totalling 1 000 flows or relative number of parts of all non zero components Click the Normalize button then click the OK button e Input the flows or relative number of parts of all components including any zero components then click the OK button 13 In the Composition Basis group ensure that the Mole Fractions radio button is selected 14 Click on the input cell for the first component 12C3Oxide This stream is 100 propylene oxide 15 Type 1 for the mole fraction then press
272. gher more sections lower fewer sections NFP Diam Factor When a new number of flow paths will result in a diameter diff gt diam fact old diameter a new 1 500 NFP section is started Not required for packed columns Lower more sections higher fewer sections Cancel The Valve tray type is sclacied as ihe deili 9 Keep the default values and click Next The next view displays the option This option is specific dimensions of the valve type trays a ane 10 Keep the default values and click the Complete AutoSection button Figure 2 156 Nil Tray Section Information Internals C Sieve tf Valve C Bubble Packed Valve Tray Straight Desin Manua Gitsch Valve Mat l Density 8220 kg m3 Valve Mat l Thickness 1 524 mm Hole Area of AA 15 30 Common Tray Properties 609 6 mm 3 175 mm a 152 4 mm 85 00 DC AWetr Info 042 mhm Vertical 38 10 mm Delete Complete AutoSection 2 121 222 Dynamic Simulation Dynamic Simulation 2 122 HYSYS calculates the Main TS tray sizing parameters based on the steady state flow conditions of the column and the desired tray types Two tray section sizes Section_1 and Section_2 appear in the Setup page of the Design tab Section_1 includes trays 1 to 27 Section_2 includes trays 28 and 29 Since there are different volumetric flow conditions at each of these sections two different tra
273. h 25 38 in Figure 1 140 3 Main TS 5 x Rating Tray Dimensions CE Tray Space ft 24 in z Tray Yol ft3 i PpaLER Efficiencies Pressure Drop Open this drop down list to select the proper units Internal Type C Sieve Valve C BubbleCap Packed Quick Size Design Rating Worksheet Performance Dynamics Delete REST Icnoied 18 In the Internal Type group select the Valve radio button 1 111 Dynamic Simulation The complete Main TS tray section property view appears below Figure 1 141 J Main TS Rating Tray Dimensions Sizing 2 000 Heat Loss 2500 Efficiencies Pressure Drop Weir Height ft Weir Lenath ft C Volume ft ctive Area ft2 lt empty gt low Paths 1 Internal Type C Sieve Valve C BubbleCap Packed Quick Size Design Rating Worksheet Performance Dynamics Delete EE ioro 19 Close the Main TS property view 20 Access the Column property view by clicking the Column Runner icon a Column Runner icon 21 In the Profiles page of the Parameters tab note the steady state pressure profile across the column The theoretical top and bottom stage pressure should be calculated so that the pressure on stage 5_Main TS the Tower Feed stage is about 203 psia while the total pressure drop across the column is about 0 7 psi 22 In the Profiles group Pressure column click in the Pressure cell for the Condenser and press the
274. hanges to key variables in the process and observe the dynamic behaviour of the model 3 76 Dynamic Simulation 3 3 Dynamic Simulation In this tutorial the dynamic capabilities of HYSYS will be incorporated into a basic steady state chemicals model In the steady state simulation a continuously stirred tank reactor CSTR converted propylene oxide and water into propylene glycol The reactor products were then fed into a distillation tower where the glycol product was recovered in the tower bottoms The dynamic simulation will take the steady state CSTR simulation case and convert it into dynamic mode If you have not built the simulation for the steady state simulation you can open the pre built case included with your HYSYS package A flowsheet of the completed dynamic simulation is shown in the figure below Figure 3 103 Reactor PropOxide TC FC pA Prop YLY Pro sa TA Reactor Oxide P Oxide 1 Lc Reactor Reactor Out Pe Mix 100 VLY Reactor Water Water Reactor Prods Prods Prods 1 Feed VLYV VVater Feed 1 Feed Coolant VaterFeed FC Only the CSTR reactor will be converted to dynamic mode The Column operation will be deleted from the simulation flowsheet The Dynamics Assistant will be used to make pressure flow specifications modify the flowsheet topology and size pieces of equipment in the simulation flowsheet This is only one method of preparing a steady state case for dynamic m
275. he Column Environment button at the bottom of the property view 2 Inthis environment you can do the following e Click the PFD icon to view the column sub flowsheet PFD a PFD icon Figure 1 94 onl PFD DePropanizer COL1 OF x HO He OA PF D ereu Colour Scheme I Workbook icon J h Ovhd 7 Condensar Condbuty Reflux Condenser Column Runner icon Main TS TowerFeed RebDuty Boilup Reboiler Lo LiquidProd To Reboiler mi Gas Processing Tutorial 1 75 e Click the Workbook icon to view a Workbook for the column sub flowsheet objects Workbook DePropanizer COL1 OF x To Condenser Boilup To Reboiler Ovhd apour Fraction 0 0000 1 0000 1 0000 0 0000 1 0000 a emperature F 48 74 84 42 190 6 187 8 48 74 i ressure psia 200 0 200 0 205 0 205 0 200 0 2 350 4 700 4 956 5 588 2 350 Mass Flow lb hr 1 115e 004 1 926e 004 3 134e 004 3 536e 004 8110 iquid Volume Flow barrel day 1561 2908 o 364 o 4245 o 1348 eat Flow Btu hr 1 359e 007 2 203e 007 2 927e 007 3 702e 007 1 034e 007 LiquidProd TowerFeed New apour Fraction 0 0000 0 0187 emperature F 190 6 20 84 ressure psia 205 0 580 0 Molar Flow MMSCFD i 0 6320 2 982 Mass Flow lb hr 4014 1 212e 004 Liquid Yolume Flow barrel day 480 4 1828 Material Streams Compositions E
276. he Draw Spec is entered so that the degrees of freedom is kept at zero throughout this tutorial It is good practice to keep the degrees of freedom at zero as you modify your column so that you can solve the column after every modification 2 74 Steady State Simulation Adding Specification Values 1 On the Design tab select the Monitor page The main feature of this page is that it displays the status of your column as it is being calculated updating information with each iteration You can also change specification values and activate or de activate specifications used by the Column solver directly from this page The current Degrees of Freedom is one indicating that only two specifications are active As noted earlier a Refluxed Absorber with a partial condenser has two degrees of freedom and therefore requires two active specifications In this case however a third degree of freedom was created when the Trim Duty stream was attached as a feed for which the heat flow is unknown HYSYS has not made a specification for the third degree of freedom therefore you need to add a water draw spec called WasteH20 Rate to be the third active specification 2 Select the Specs page Here you will remove two specifications and add one new specification 3 Inthe Column Specifications group select Reflux Rate and then click the Delete button Delete the Btms Prod Rate specification also Next you will add the WasteH2O
277. he LTSLiq stream and the MIX 101 unit operation 26 Break the line between the LTSLiq stream and the MIX 101 unit operation e Click the Break Connection icon in the tool bar e Click to the right of the arrow on the LTSLig stream 27 Install a second valve operation e On the Object Palette right click the Valve icon e Drag the cursor to the right of the LTSLig stream e Release the mouse button 28 Double click the valve icon to open its property view 29 Specify the following connections Tab Page In this cell Enter Design Connections LTS Valve Inlet LTSLig 30 Close the valve property view 1 102 Gas Processing Tutorial 1 108 Processing Tutorial 1 103 31 Attach the LTSExit stream to the MIX 101 unit operation e Click the Attach Mode icon e Move the cursor over the LTSExit stream icon A white box appears e Click and drag the cursor to the inlet side of the MIX 101 icon A white box appears indicating a connection point e Release the mouse button to complete the connection e Click the Attach Mode icon again to exit the attach mode Next you will add a valve operation between the MIX 101 unit operation and the TowerFeed stream 32 Break the line between the TowerFeed stream and the MIX 101 unit operation Be sure to break the line to the left of the TowerFeed stream arrow 33 Install a third valve operation with the following connections Tab Page In this cell Enter
278. he Oil Characterization Environment using the fluid package you just created Three steps are required for characterizing the oil 1 Define the Assay 2 Create the Blend 3 Install Oil in the Flowsheet Atmospheric Crude Tower R1 7 Define the Assay 1 On the Assay page of the Oil Characterization view click the Add button This will create a new assay and you will see the Assay view Change the Bulk Properties setting to Used Complete the Input data for the Bulk Properties as shown below Figure R1 3 Input Data lt empty gt 54 82 Ib tt3 lt empty gt Dynamic gt l 100 0F lt empty gt 210 0 F Viscosity 2 lt empty gt 4 Since the TBP data is supplied select TBP from the Assay Data Type drop down list Select Liquid Volume from the Assay Basis drop down list Click the Edit Assay button and enter the data as follows Figure R1 4 Assay Input Data Assay Percent Temperature 4500 9 000 14 50 20 00 30 00 40 00 50 00 60 00 70 00 76 00 80 00 85 00 lt Anntu gt lt emntu gt L All input curves except distillation are on midpoint basis Dependent curves will be shifted to middle Cancel OK 7 Inthe Assay Definition group click the Light Ends drop down list and select Input Composition 8 In the Input Data group click the Light Ends radio button RRB Setup 8 Setup 9 Enter the light ends data as follows Figure R
279. he Top Stage TC view appears Change the controller mode to Auto In the PV field enter a set point of 86 E HYSYS automatically converts this value to C Close the Top Stage TC face plate view Close the Top Stage TC property view Add another PID Controller operation that will serve as the Depropanizer 9th stage temperature controller In the controller property view specify the following details Tab Page In this cell Enter Connections Stage9 TC Process Variable Source Main TS Stage Temperature 9_Main TS Output Target Object Reboil Valve Ensure that you select the correct temperature units from the units drop down list 23 24 Click the Face Plate button The Stage 9 TC face plate view appears Change the controller mode to Auto In the PV field input a set point of 184 F You should be able to run the integrator at this point without any problems however you will probably want to monitor important variables in the dynamic simulation using strip charts ZO 26 1 126 Return to the Parent Environment Save the case as DynTUT1 4 hsc Gas Processing Tutorial 1127 Processing Tutorial 1 127 Monitoring in Dynamics Now that the model is ready to run in Dynamic mode you will create a strip chart to monitor the general trends of key variables The following is a general procedure for installing strip charts in HYSYS 1 Open the Databook by using the hot key combination CTRL D
280. he Workbook Notice how partial information Stream CoolGas has not yet been flashed as its temperature is unknown ee wee CoolGas is flashed later when a temperature approach is specified for CoolGas throughout the flowsheet HYSYS always the Gas Gas heat exchanger calculates as many properties as possible for the streams based on the available information Figure 1 54 Workbook Case Main MixerOut Sep ap 8976 1 0000 00 60 00 60 00 500 600 0 8 976 2 318e 004 3012 1983 4995 4342 2563e 007 1 628e 007 4180e 007 3 605e 007 Name 0 i CoolGas SalesGas LTSVap 0000 lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt 590 0 lt empty gt lt empty gt Molar Flow MMSCFD 024 8 976 lt empty gt lt empty gt 4 2 318e 004 lt empty gt lt empty gt 652 9 4342 lt empty gt lt empty gt 5 756e 006 lt empty gt lt empty gt lt empty gt Material Streams Energy Streams Unit Ops Faadediock sedi J Include Sub Flowsheets we oo C Show Name Only Number of Hidden Objects 1 44 Gas Processing Tutorial 1 45 l e 7 Using Workbook Features Before installing the remaining operations you will examine a number of Workbook features that allow you to access information quickly and change how information is displayed Accessing Unit Operations from the Workbook T
281. he design Son ean as ne mize We and observe the response of other variable Strip Chart views to see the details 3 94 HYSYS Applications B 1 B HYSYS Applications The Amines Property Package is an optional property package It is not included in the base version of HYSYS Contact your Hyprotech agent for more information or e mail us at info hyprotech com This section contains examples that illustrate many of the features of HYSYS The applications include aspects of Conceptual Design Steady State modeling and Optimization All aspects are not illustrated in every example so the areas of interest in each application are highlighted below The HYSYS Applications describe in general terms how to completely model particular processes using various features of HYSYS detailed methods of constructing the models are not provided If you require detailed descriptions on how to construct models in HYSYS see the comprehensive Tutorial section of this manual The examples in the Applications section provide a broad range of problems related to various segments of industry and are organized as follows bas Processing Gl Acid Gas Sweetening with DEA Steady State Modeling Optional Amines Package A sour natural gas stream is stripped of H2S and CO2 in a Contactor absorber tower The rich DEA diethanolamine is regenerated in a Stripping tower and the lean DEA is recycled back to the Contactor To solve this example
282. he next task is to create a Fluid Package A Fluid Package at minimum contains the components and property method that HYSYS will use in its calculations for a particular flowsheet Depending on what a specific flowsheet requires a Fluid Package may also contain other information such as reactions and interaction parameters Creating a Fluid Package 1 Click the Fluid Pkgs tab of the Simulation Basis Manager 2 Click the Add button The Fluid Package property view appears Figure 3 7 Fluid Package Basis 1 Property Package Selectiorr Property Package Filter All Types EOSs Activity Models C Chao Seader Models C Vapour Press Models C Miscellaneous Types Chao Seader Chien Null Esso Tabular Extended NRTL GCEOS General NATL x Advanced Thermodynamics Component List Selection Component List 1 x View Set Up Parameters Binary Coeffs StabTest Phase Order Tabular Name Basis 1 Property Pkg lt Nome gt COMThemo Segressic Chemicals Tutorial 3 9 The Fluid Package property view allows you to supply all the information required to completely define the Fluid Package In this tutorial you will use the following tabs Set Up Binary Coeffs Binary Coefficients and Rxns Reactions You choose the Property Package on the Set Up tab The currently selected property package is lt none gt There are a number of ways to select the desired base property package in th
283. here are several ways to open the property view for an operation directly from the Workbook In addition to using the Unit Ops tab you can use the following method 1 Click one of the Workbook streams tabs Material Streams Compositions or Energy Streams The box at the bottom of the Workbook view displays the operations to which the current stream Any utilities attached to the is attached Siream with WIE WVOrKDOOK For this example click on any cell associated with the stream active will also be displayed in and are accessible through SepVap The box at the bottom displays the names of the two this box operations InletSep and Gas Gas to which this stream is attached 3 To access the property view for either of these operations double click on the operation name Figure 1 55 Stream SepVap is the current Workbook location Workbook Case Main Feed 1 Feed 2 MixerOut apour Fraction 0 8952 0 9013 0 8976 1 0000 emperature F 60 00 60 00 60 00 60 00 ressure psia 600 0 600 0 600 0 600 0 6 000 4 000 10 00 8 976 Mass Flow lb hr 1 675e 004 1 100e 004 2 775e 004 2 318e 004 Liquid Volume Flow barrel day 3012 1983 4995 4342 Heat Flow Btu hr 2 553e 007 1 628e 007 4 180e 007 3 605e 007 CoolGas SalesGas zoz o a n o z w m z Z Material Streams Energy Streams Unit Ops inletSep C Include Sub Flowsheets Gas Gas L Show Name Only
284. his celle Enters Connections No of Stages Inlet Streams Stage To Rect 19 Rect_Feed 22 Side Draw Liquid Stage 1st Prod 2 Fusel 20 MoS Maaa Ps TO memea a oe 2 Delete the default Btms Prod Rate and Reflux Rate specifications before adding the new specifications Delete all specifications that do not appear in the following table C1 10 EthanolPlant Aa Plant C1 11 3 Define the following specifications Design tab Specs page Also set the damping factor to accelerate the convergence Specifications Tab Page In this cell Enters Design Specs Reflux Ratio Active Stage Condenser Flow Basis Molar Spec Value 7100 Ovhd Vap Rate Active Draw Rect_Vap Flow Basis Molar Spec Value 0 100 kgmole hr Draw Rate Active Draw Rect _Dist Flow Basis Mass Spec Value 2 00 kg hr Comp Frac Active Stage 2_Main TS Flow Basis Mass Fraction Phase Liquid Spec Value 0 95 Component Ethanol Fusel Draw Rate Active Draw Fusel Flow Basis Mass Spec Value 3 00 kg hr 1stProd Draw Rate Estimate Draw 1stProd Flow Basis Molar Spec Value 68 00 kgmole hr Parameters Damping Factor 0 25 Solver Fixed 4 Click the Run button to solve the column C1 11 612 Steady State Simulation Steady State Simulation 1 3 3 Draw Stream Location The side liquid draw Fusel is added at stage 20 To determine if this is an appropriate stage to recover the heavy alcohols view the stage by stage compos
285. ial stream to the PFD by doing one of the following e From the Flowsheet menu select Add Stream e Double click the Material Stream icon on the Object Palette 10 In the Stream Name cell type Store This stream will be used to store information from the Atm Feed stream Figure 2 148 avi Vapour Phase Fraction Conditions Temperature F lt empty gt Properties Pressure psia lt empty gt Molar Flow Ibmole hr lt empty gt Mass Flow lb hr lt empty gt K Value Std Ideal Liq Vol Flow barrel day lt empty gt User Variables Molar Enthalpy Btu lbmole lt empty gt Molar Entropy Btu Ibmole F lt empty gt Notes Heat Flow Btu hr lt empty gt Cost Parameters Lig Yol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 Composition Worksheet Attachments Dynamics prion Compositions Delete Define from Other Stream a gt 11 In the Store stream property view click the Define from other Stream button The Spec Stream As view appears 2 116 Refining Tutorial Tutorial 2 117 12 In the Available Streams group select Atm Feed Figure 2 149 Ni Spec Stream As Chosen Stream Conditions Available Streams AGO AGO Steam Diesel Steam Copy Stream Conditions a Vapour Fraction E Molar Enthalpy J Temperature Molar Entropy V Pressure J Composition J Correlations Iv Flow J Cost Parameters Flow Basis
286. ic Simulation 2 00011 MMiereccnnsssecnnnsssccnssessscnnessccennsssacees 98 1 3 1 Modifying the Steady State Flowsheet cccccccccsseeeeeeeee 99 Tse COMM SIZING anana ies n e eet yiusety adc 107 1 3 3 Using the Dynamics Assistant cccccccseeeeeeeeeeeeeeeaeeeees 113 1 3 4 Adding Controller Operations ccccceceeeseeeeeeeeeeeeeeeeeeeeees 119 Gas Processing Gas Processing Tutorial 1 3 1 1 Introduction The simulation will be built using these basic steps Create a unit set Choose a property package Select the components Create and specify the feed streams Install and define the unit operations prior to the column oe ee oe oS Install and define the column In this Tutorial a natural gas stream containing N2 CO2 and Cl A solved case is located in the through nC4 is processed in a refrigeration system to remove the heavier hydrocarbons The lean dry gas produced will meet a pipeline hydrocarbon dew point specification The liquids removed from the rich gas are processed in a depropanizer column yielding a liquid product with a specified propane content A flowsheet for this process is shown below file TUTOR1 HSC in your HYSYS Samples directory LTSVap C3Duty GasiGas 20 ColdGas LTS Sep ap CoolGas _ Chiller N Ovhd A CondDuty amp SalesGas Feed InletSep E 1 MixerOut 4 Feed Mix 100 Sik Dew Point RebDuty LiquidProd
287. ication Value lt empty gt Default Basis E Current Calculated Value lt empty gt Errors Degrees of Freedom 0 Weighted Tolerance 1 000e 002 Weighted Calculated Error l o lt empte Absolute Tolerance 151 0 barrel day Absolute Calculated Error lt empty gt Side Ops Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged Design Parameters Rating Worksheet Update Outlets Ignored 2 Inthe Column Specifications group click the Add button The Column Specifications view appears Select Column Liquid Flow as the Column Specification Type Click the Add Spec s button and the Liq Flow Spec view appears Change the name from its default to Overflash ao eS In the Stage cell select 27_Main TS from the drop down list of available stages A typical range for the Overflash rate is 3 5 of the total feed to the column In this case the total feed rate is 100 000 barrels day For the Overflash specification 3 5 or 3 500 barrels day is used 2 85 2 85 Steady State Simulation 7 Inthe Spec Value cell enter 3500 Figure 2 105 Ni Liq Flow Spec Overflash Name _Overflash 27_Main TS Volume Spec Value 3500 00 barrel day Parameters Summary Delete 8 Close the view to return to the Column property view The new specification appears in the list of Column Specifications group on the Specs page
288. icking the Basis icon 2 Click the Reactions tab This tab allows you to define all the reactions for the flowsheet Figure 3 19 Simulation Basis Manager Fizxn Components Reactions Reaction Sets 12C30 xide evs ut Global Asn Set View Set 12 C3diol H20 Add Ren Add Set elete Ayn Delete Set Assoc Fluid Pkgs Import Set Export Set Add to FP Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment The reaction between water and propylene oxide to produce propylene glycol is as follows H O C H 0 gt C3H 0 3 1 Selecting the Reaction Components The first task in defining the reaction is choosing the components that will be participating in the reaction In this tutorial all the components that were selected in the Fluid Package are participating in the reaction so you do not have to modify this list For a more complicated system however you would add or remove components from the list To add or remove a component click the Add Comps button The Component List View appears Refer to the Selecting Components section in Section 3 2 3 Defining the Fluid Package for more information Steady State Simulation Creating the Reaction Once the reaction components have been chosen the next task is to create the reaction 1 Inthe Reactions group click the Add Rxn button The Reactions view
289. id Pkg Basis 1 Peng Robinson Side Ops Side Stripper Summary Side Strippers Ta Stages Liq Draw Stage Yap Return Stage Outlet Flow aerarii ara Side Rectifiers Pump Arounds Yap Bypasses Side Draws When you install side Flow Basis equipment it resides in the Molar C Mass Volume Ew Add Delete Side Ops Input Expert Column sub flowsheet You can build a complex column ios Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics in the sub flowsheet while in the Main Flowsheet the column appears as a single operation You can then transfer any needed stream information from the sub Delete Column Environment Run Reset Unconverged V Update Outlets Ignored On this tab you can Install View Edit or Delete all types of Side flowsheet by simply attaching Equipment The table displays summary information for a given type of ah rae to the Main side operation depending on the page you are currently on owsneet 2 5 This is a reboiled 3 stage stripper with a 0 75 boil up ratio so leave the Configuration radio button at Reboiled and the k and Boil Up Ratio fields at their defaults 2 6 Steady State Simulation 2 Ensure that you are on the Side Strippers page 3 Click the Add button The Side Stripper view appears Figure 2 89 Nil Side Stripper 551 Name ssi Return Stage Configuration Reboiled C
290. iew displays all streams attached to the current operation Currently the Name cell for MIX 100 has focus so the box displays the three streams attached to this operation For example to open the property view for the Prop Oxide stream attached to the Mixer do one of the following e Double click on Prop Oxide in the box at the bottom of the view e Double click on the Inlets cell for MIX 100 The property view for the first listed feed stream in this case Prop Oxide appears Steady State Simulation Any utilities attached to the stream with focus in the Workbook are also displayed in and are accessible from this box 3 42 Workbook Features Before installing the remaining operations you will examine a number of Workbook features that allow you to access information quickly and change how information is displayed Accessing Unit Operations from the Workbook While you can easily access the property view for a unit operation from the Unit Ops tab of the Workbook you can also access operations from the Material Streams Compositions and Energy Streams tabs When your current location is a Workbook streams tab the gray box at the bottom of the Workbook view displays the operations to which the current stream is attached For example click on any cell associated with the stream Prop Oxide The gray box displays the name of the mixer operation MIX 100 If the stream Prop Oxide was also attached to another unit oper
291. iew to an icon and place it at the bottom of the Desktop Hecording Data Suppose you now want to make changes to the flowsheet but you would like to record the current values of the key variables before making any changes Instead of manually recording the variables you can use the Data Recorder to automatically record them for you To record the current values 1 Click on the Data Recorder tab Figure 2 140 4 DataBook Available Scenarios Data Recorder Data Selection Current Scenario Object Variable Include Reflux Ratio Trim Duty Trim Duty Residue BP Cur ASTM 1160 Vac 5 Residue Graph ca Variables j Process Data Tables Strip Charts Data Recorder CaseStudes 2 109 Steady State Simulation New Solved St EG Name for New State State 1 OK 2 110 When using the Data Recorder you first create a Scenario containing one or more of the key variables then record the variables in their current state 2 Click the Add button in the Available Scenarios group and HYSYS creates a new scenario with the default name Scenario 1 It is required to include all three key variables in this scenario Activate each variable by clicking on the corresponding Include checkbox Figure 2 141 DataBook Fae Ed Available Scenarios Data Recorder Data Selection Scenario 1 Record Current Scenario Scenario 1 Add pObject Variabl
292. ig fig Molar Enthalpy 4 sig fig Order AAAA 6 In the Object group click in the Name cell and change the name for the new tab from the default Material Streams 1 to PT Flow to better describe the tab contents 1 47 Steady State Simulation Next you will customize the tab by removing the irrelevant variables 7 Inthe Variables group select the first variable Vapour Fraction Figure 1 59 Tab Contents Object Name P T Flow Type Material Stream New Type se T Variables 1 4 fixed Temperature 4 sig fig Pressure 4 sig fig Molar Flow 4 sig fig Mass Flow 4 sig fig Std Ideal Lig Yol Flow 4 sig fig ___Heat Flow _ 4 sig fig Molar Enthalpy 4 sig fig g i Press and hold the CTRL key Click on the following variables Mass Flow Heat Flow and Molar Enthalpy These four variables are now selected 10 Release the CTRL key Deleting variables removes 11 Click the Delete button The unneeded variables are removed from them from the current the list The finished Setup appears below Workbook tab only lf you want to remove variables from another tab you must edit Figure 1 60 each tab individually Workbook Tabs Tab Contents Material Streams Add Object P T Flow l Compositions ree Name P 1 Flow Order E St Unit Ops as Type Material Stream New Type Variables The new tab now Use Set appears in
293. ight corner of the PFD view to make it full screen 3 Click the Zoom All icon at the bottom left of the PFD view to fill the re sized PFD view Zoom All icon 4 Object inspect right click the main column tray section and the object inspection menu appears View Properties 5 Select Show Trays from the object inspection menu The Stage Pidasorarineses Visibility view appears Cut Paste Objects b i 6 Select the Selected Expansion radio button xML Data Exchange TESA Hide stages 4 5 6 11 12 13 14 24 25 and 26 by deactivating their Hide Shown checkboxes X Delete Show Table Figure 2 116 Format Label gt Move Size Label ie Hs For Sizi Tray Section Representation aa aaa Full Expansion Selected Expansion G Transform b Charge loon Selected Control Auto Position g Check All Object Inspect menu 2 94 Draw Wire Frame Uncheck Al Show Trays Expand Vv Mo M a E M M a M 10_MainTS 8 Click the Close icon on the Stage Visibility view to return to the PFD The routing of some streams in the PFD can be undesirable You can improve the stream routing by completing the next step 9 From the PFD menu item select Auto Position and HYSYS rearranges the PFD in a logical manner Refining Tutorial 2 95 Enlarge Icon The next task in customizing the PFD is to enlarge the icon for the main column 1 Click on the icon for the main tray section Main TS
294. il You can use the Databook to monitor key variables under a variety of process scenarios and view the results in a tabular or graphical format To open the Databook do one of the following e press CTRL D e from the Tools menu select Databook The Databook appears below Figure 2 131 DataBook Available Data Entries Object Variable E Variables Process Data Tables Strip Charts Data Recorder Case Studies Adding Variables to Databook The first step is to add the key variables to the Databook using the Variables tab For this example the Overflash specification is varied and examined to investigate its effect on the following variables e D1160 Boiling Temperature for 5 volume cut point of stream Residue e heat flow of energy stream TrimDuty e column reflux ratio Click the Insert button and the Variable Navigator view appears 2 Select the UnitOps radio button in the Object Filter group The Object list is filtered to show unit operations only 3 Select Atmos Tower in the Object list and the Variable list available for the column appears to the right of the Object list 2 104 Refining Tutorial 2 105 The Variable Navigator is 4 Select Reflux Ratio in the Variable list used extensively in HYSYS for locating and selecting Figure 2 132 variables The Navigator operates in a left to right manner the selected Vee AVAN Flowsheet determines the Flowsheet Case Main ee the cles Atmos
295. ile the dependent y axis variable is the TBP in C Move the graph legend by double clicking inside the plot area then click and drag the legend to its new location 2 92 The completed Data Control view is shown below Figure 2 113 Data Control Ea Style Basis Multi Tray Molar Single Tray C Mass 2_DieselS Liquid Vol 3_DieselSS Phase Vapour V Light Liquid All Invert None M Heavy Liquid Sot Visible Points tf 15 Points 31 Points 11 Click on the Close icon Xj to close the Data Control view You return to the Boiling Point Properties view which now displays the TBP Curves 12 Make the Boiling Point Properties view more readable by clicking the Maximize icon in the upper right corner of the view or by clicking and dragging its border to a new view size The Boiling Point Properties view is shown below Figure 2 114 L Boiling Point Properties Boiling Point Properties Condenser Light 29_ tin TS Light Kero _Reb Light 3__Diesel Light 3__AGOSS Light babe aw a a E 60 00 70 00 80 00 90 00 100 00 Percent Liquid Yolume Composition Profile Data Control 13 When you are finished viewing the profiles click the Close icon Refining Tutorial 2 93 Moving to the Column Sub Flowsheel When considering the column you might want to focus only on the column sub flowsheet You can do this by entering th
296. ility 12 Size the Regenerator tray section following the same procedure described above for the DEA Contactor The Auto Section function may create two tray sections ensure that the column is sized with only one tray section for all trays Delete the section that does not match the specifications below 13 Confirm the following tray section parameters for Main TS in the Regenerator Variable Value Section Diameter 3 5 ft 14 In the Regenerator column property view click the Rating tab then select the Tray Sections page 15 Enter the Section Diameter value shown above Vessel Sizing The Condenser and Reboiler operations in the Regenerator column sub flowsheet require proper sizing before they can operate effectively in Dynamics mode The volumes of these vessel operations are determined using a 10 minute liquid residence time 1 Open the Regenerator property view then enter the Column Environment Open the Condenser property view Click the Worksheet tab then select the Conditions page Confirm the following Std Ideal Liquid Volumetric Flow Stream Std Ideal Liquid Volume Flow G1 23 G1 24 Dynamic Simulation 10 Calculate the vessel volume as follows assuming a 50 liquid level residence volume Total Liquid Exit Flow Residence Time G1 1 0 5 Vessel Volume Click the Dynamics tab then select the Specs page In the Model Details group specify the vessel volume as 15 97 ft as
297. information In this cell Enter Minimum Available 0 Btu hr Maximum Available 1 x 10 Btu hr Close the FCV for Coolant view Click the Face Plate button Change the controller mode to Auto and input a set point of 140 F Close the Reactor TC face plate view and property view Save the case as DynTUT3 4 hsc ewe Integrator icons Green Active Red Holding Chemicals Tutorial 3 91 10 The integrator can be run at this point Click the Integrator Active icon in the tool bar 11 When you are given the option to run the dynamic assistant first before running the integrator click the No button When the integrator is initially run HYSYS will detect that the Reactor does not have a vapour phase at the specified process conditions You have the option to select either the default which is to Increase Temperature or choose 100 Liquid in the Reactor Figure 3 118 Ni Reactor Liquid Level Initialisation This vessel has no vapour phase at the specified process conditions HYSYS can initialise this vessel with a vapour phase by increasing the total vessel temperature Alternatively the liquid level can be set to 100 but this can cause difficulties starting simulation RECOMMENDATION Increase temperature i 100 Liquid 12 Select the default setting which is Increase Temperature 13 Let the integrator run for a while then click the Integrator Holding icon to stop the Integrator At this point y
298. ing Duty 4 520e 006 Btuhr Glycol Glycol Production 713 4 barrel day I I I I gt View DataBook This table will be accessed again later to demonstrate how its results are updated whenever a flowsheet change is made 19 For now click the Minimize icon in the upper right corner of the Key Variables Data view HYSYS reduces the view to an icon and places it at the bottom of the Desktop 3 71 Steady State Simulation Before you make changes to the flowsheet you will record the current values of the key variables Instead of manually recording the variables you can use the Data Recorder to automatically record them for you 20 Click the Data Recorder tab in the Databook 3 72 DataBook Biel x Available Scenarios Data Recorder Data Selection Current Scenario Object Variable Include Reactor Temp Coolant Cooling Duty Glycol Glycol Production Variables Process Data T ables Strip Charts Data Recorder When using the Data Recorder you first create a Scenario containing one or more of the key variables then record the variables in their current State 21 In the Available Scenarios group click the Add button HYSYS creates a new scenario with the default name Scenario 1 22 In the Data Recorder Data Section group activate each variable by clicki
299. ing Face Plates see Section 12 13 Controller Face Plate in the Operations Guide Cond LC x Exec Int Sp L PY 50 000 lop lt empty gt Man Tuning If you cannot locate a stream or operation in the Select Input for PV view select the All radio button in the Object Filter group and look again Refining Tutorial 13 Click the Face Plate button The face plate for Cond LC appears Figure 2 170 Cond LC x Exec Int Sp L PY 50 000 oP lt empty gt 14 Change the controller mode to Auto on the face plate by opening the drop down list and selecting Auto 15 Double click the PV cell then input the set point at 50 Figure 2 171 I Co mn d Li Cc a xi Exec Int en L l 50 JOP 0 00 Auto x Tuning 16 Close the Cond LC property view but leave the face plate view open 17 Repeat the procedures you just learned to add a PID Controller operation which serves as the Kero_SS_Reb level controller Specify the following Tab Page In this cell Enter Process Variable Source Kero_SS_Reb Liq Percent Level une Target Object Kero SS Draw ii 18 Click the Control Valve button The FCV for Kero SS Draw view appears 2 133 Dynamic Simulation 19 In the Valve Sizing group enter the following In this cell Enter Flow Type MolarFlow 20 Close the FCV for Kero SS Draw view 21 Click the Face Plate button Change the contr
300. io button in the Filter group Navigator icon 3 Select Atmos Tower and click the View button The Atmos Tower property view appears Go to the Design tab and select the Monitor page Scroll down to the bottom of the Specifications table so the Overflash specification is visible A typical range for the Overflash rate is 3 5 of the tower feed A slightly wider range is examined 1 5 7 5 which translates to 1500 7500 bbl d 6 Change the Specified Value for the Overflash specification from its current value of 3500 barrel day to 1500 barrel day HYSYS automatically recalculates the flowsheet 2 111 Steady State Simulation 7 Double click on the Key Variables Data icon to restore the view to its full size The updated key variables are shown below Figure 2 143 Key Variables Data Object Variable Value Units Reflux Ratio 0 5858 Trim Duty Trim Duty 1 883e 007 Btu hr F gt l Residue BP Cur ASTM 1160 Vac 5 Resi 377 8 E View DataBook As a result of the change e the Trim Duty has decreased e the Residue D1160 Vacuum Temperature 5 cut point has decreased e the column reflux ratio has decreased 8 Press CTRL D to make the Databook active again You can now record the key variables in their new state 9 Move to the Data Recorder tab in the Databook 10 Click the Record button and HYSYS provides you with the default name State 2 for the new state 11 Ch
301. ion Sets 3 22 18 Close both the Kinetic Reaction property view and the Reactions view 19 Click the Basis icon to ensure the Simulation Basis Manager view is active On the Reactions tab the new reaction Rxn 1 now appears in the Reactions group Simulation Basis Manager Rxn Components Reactions Reaction Sets 12C30 vide Rixn 1 Global Rxn Set View Set 12 C3diol f i Add Set Delete Ren Delete Set Copy Set coe nips Assoc Fluid Pkgs Import Set Export Set Add Comps Add to FP Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment The next task is to create a reaction set that will contain the new reaction In the Reaction Sets list HYSYS provides the Global Rxn Set Global Reaction Set which contains all of the reactions you have defined In this tutorial since there is only one REACTOR the default Global Rxn Set could be attached to it however for illustration purposes a new reaction set will be created Creating a Reaction Set Reaction Sets provide a convenient way of grouping related reactions For example consider a flowsheet in which a total of five reactions are taking place In one REACTOR operation only three of the reactions are occurring one main reaction and two side reactions You can group the three reactions into a Reaction Set then attach the set to the appropri
302. ion from the bottom left connection point on the Heater icon labeled Energy Stream The new stream is automatically named Q 100 and the heater now has yellow warning status This status indicates that all necessary connections have been made but the attached streams are not entirely known Figure 2 69 PreFlashLig Q 100 12 Click the Attach icon again to return to Move mode 2 60 Refining Tutorial 2 61 The heater outlet and energy streams are unknown at this point so they appear light blue and purple respectively Modifying Furnace Properties 1 Double click the Heater icon to open its property view 2 Click the Design tab then select the Connections page The names of the Inlet Outlet and Energy streams appear in the appropriate fields Figure 2 70 S E 100 Design Name E 00 Connections Parameters Inlet Energy User Variables PreFlashLid v 0 100 Notes Outlet Fluid Package B asis 1 hd Design Rating Worksheet Performance Dynamics Delete J romby o Ct In the Name field change the operation name to Furnace Select the Parameters page 2 62 Steady State Simulation 5 In the Delta P field enter10 psi then close the view Figure 2 71 5 Furnace Design Connections Parameters User Variables Design Rating Worksheet Performance Dynamics Delete J romby T Cr The Furnace has one available degree
303. ions in a tabular format while the PFD is a graphical representation of the flowsheet Click the Workbook icon on the toolbar to ensure the Workbook window is active Installing the Feed Streams In general the first action you perform when you enter the Simulation environment is installing one or more feed streams The following procedure explains how to create a new stream 1 On the Material Streams tab of the Workbook type the stream name Feed 1 in the cell labelled New Gas Processing Tutorial 1 21 2 Press ENTER HYSYS will automatically create the new stream with the name defined in step 1 Your Workbook should appear as shown below Figure 1 21 Workbook Case Main apour Fraction lt empty gt emperature F lt empty gt ressure psia lt empty gt Molar Flow MMSCFD lt empty gt Mass Flow lb hr lt empty gt iquid Yolume Flow barrel day lt empty gt eat Flow Btu hr lt empty gt Material Streams Energy Streams Unit Ops Prackict ick react C Include Sub Flowsheets FeederBlock_Feed 1 L Show Name Only Number of Hidden Objects 0 Next you will define the feed conditions When you pressed ENTER after typing in the stream name HYSYS automatically advanced the active cell down one to Vapour Fraction 1 Move to the Temperature cell for Feed 1 by clicking it or by pressing the Down arrow key 2 Type 60 in the Temperature cell In the Unit drop down
304. is case UNIQUAC 3 Do one of the following e Begin typing UNIQUAC and HYSYS finds the match to your input e Use the vertical scroll bar to move down the list until UNIQUAC becomes visible then click on it Figure 3 8 Property Package Selection Property Package Filter OLI_Electrolyte Peng Robinson All Types C EOSs C Activity Models Chao Seader Models C Vapour Press Models Miscellaneous Types Wilson Zudkevitch Joffee The Property Pkg indicator bar at the bottom of the view now indicates UNIQUAC is the current property package for this Fluid Package Figure 3 9 Property Pkg UNIQUAC Ide SS Alternatively you can select the Activity Models radio button in the Property Pkg Filter group producing a list of only those property packages which are Activity Models UNIQUAC appears in the filtered list as shown here Figure 3 10 Property Package Selection Property Package Filter All Types Chao Seader Models Vapour Press Models C Miscellaneous Types 3 9 Steady State Simulation In the Component List Selection drop down list HYSYS filters to the library components to include only those appropriate for the selected Property Package In this case no components have yet been defined Selecting Components Now that you have chosen the property package to be used in the simulation your next task is to select the components 1 Inthe Component List Selection group click the
305. is used to minimize the number of times the User Unit Op s Execute is called Signifies the end of the initialization subroutine This line does not need to be added When you are finished activate the view by selecting the compressed stream as the Feed on the Connections page of the Design tab Ensure that the Link Stream stream name is also compressed The Unit Op will not appear solved on the flowsheet even though it is This is because HYSYS expects it to have a fully defined product stream
306. ise PFD Case main HA HR OAD amp yf he o T o am Ka sa amp ata a T amp C amp 4 ab 0 I 868 x gt Eta cas o e rz deh lt u cit o o E E gy gt E3 T O BEKI 0s O Z You can toggle the palette open or closed by pressing F4 or by selecting the Open Close Object Palette command from the Flowsheet menu j Save icon Gas Processing Tutorial 1 19 There are several things to note about the Main Simulation environment In the upper right corner the Environment has changed from Basis to Case Main A number of new items are now available in the menu bar and tool bar and the PFD and Object Palette are open on the Desktop These latter two objects are described below Objects Description The PFD is a graphical representation of the flowsheet topology for a simulation case The PFD view shows operations and streams and the connections between the objects You can also attach information tables or annotations to the PFD By default the view has a single tab If required you can add additional PFD pages to the view to focus in on the different areas of interest Object Palette A floating palette of buttons that can be used to add streams and unit operations Before proceeding any further save your case Do one of the following e Click the Save icon on the toolbar e From the File menu select Save e Press CTRL S If this is
307. ition profile l To examine this information click the Parameters tab in the Column property view 2 Select the Estimates page In this view you can see the Composition Figure C1 5 Estimates of each tray Column Rect COL4 Fluid Pkg Basis 1 NRTL Ideal Parameters Profiles Estimates Efficiencies Solver 2 3 Phase n Design Parameters Side Ops lol x Composition Estimates Ethanol Condenser _ 1_ Main TS H20 c02 2171e 006 2134e 009 2 095e 010 2 073e 010 Methanol 1 393e 003 8 988e 004 5 805e 004 2 162e 003 AceticAcid 2 378e 020 1 127e 019 5 344e 019 2 535e 018 1 Propanol 4 840e 006 9 438e 006 1 837e 005 3 568e 005 2 066e 010 3 892e 004 1 140e 017 6 693e 005 _ 2 053e 010 2 742e 004 5 075e 017 1 232e 004 2 051 e 010 2 050e 004 2 254e 016 2 242e 004 2 041e 010 1 634e 004 1 002e 015 4 048e 004 2 031e 010 1 384e 004 4 455e 015 262e 004 2 019e 010 1 235e 004 1 983e 014 1 295e 003 10__Main TS 2 006e 010 1 147e 004 8 833e 014 2 294e 003 11_Main TS 1 991e 010 1 096e 004 3 937e 013 4 030e 003 12_Main TS 1 975e 010 1 067e 004 1 756e 012 7 007 e 003 13_MainTS 1 957e 010 1 051 e 004 7 829e 012 1 201e 002 14_ Main TS 1 939e 010 1 041 e 0
308. k the Unit Ops tab should again be active 1 Click the Add UnitOps button The UnitOps view appears You can also access the Unit Ops view by pressing F12 In the Categories group select the Vessels radio button In the list of Available Unit Operations choose Separator Click the Add button The Separator property view appears displaying the Connections page on the Design tab 5 Inthe Name cell change the name to InletSep then press ENTER Move to the Inlets list by clicking on the lt lt Stream gt gt cell or by pressing ALT L Open the drop down list of available feed streams 8 Select the stream MixerOut by doing one of the following e Click on the stream name in the drop down list e Press the Down arrow key to highlight the stream name then press ENTER 1 39 Steady State Simulation 9 Move to the Vapour Outlet cell by doing one of the following e Click on the Vapour Outlet cell e Press ALT V 10 To create the vapour outlet stream type SepVap then press ENTER 11 Click on the Liquid Outlet cell type the name SepLig then press ENTER The completed Connections page appears as shown in the following figure Figure 1 47 InletSep Design Name inlets ep Connections Inlets Vapour Outlet Parameters SepVap User Variables Notes Energy Optional Fluid Package Liquid Outlet B asis 1 SepLig Design Reactions Rating Worksheet Dynamics Delete E
309. k Icon You can also filter the list by selecting the Piping Equipment radio button in the Categories group then use one of the above methods to install the operation Double clicking on a listed operation can also be used instead of the Add button or the ENTER key Chemicals Tutorial 3 37 Installing Unit Operations Now that the feed streams are known your next task is to install the necessary unit operations for producing the glycol Installing the Mixer The first operation is a Mixer used to combine the two feed streams As with most commands in HYSYS installing an operation can be accomplished in a number of ways One method is through the Unit Ops tab of the Workbook 1 Click the Workbook icon to ensure the Workbook is active 2 Click the Unit Ops tab of the Workbook 3 Click the Add UnitOp button The UnitOps view appears listing all available unit operations When you click the Add button or press ENTER inside this view HYSYS adds the operation that is currently selected 4 Select Mixer by doing one of the following e Start typing mixer e Scroll down the list using the vertical scroll bar then select Mixer Figure 3 45 UnitOps Case Main Categories Available Unit Operations All Unit Ops z Cancel Heater C Vessels HF Alkylation Hydrocracker Hydrocyclone Liquid Liquid Extractor C Heat Transfer Equipment C Rotating Equipment C Piping Equipment Solids Handling M
310. k the Setup tab In the Component List Selection group click the View button The Component List View appears Figure 3 111 Component List View Components Available in the Component Library View Filters Sim Name C Full Name Synonym Methane Ethane Propane i Butane n Butane i Pentane n Pentane n Hexane n Heptane n Octane n Nonane n Decane n C11 n C12 am Add Component Selected Components less T2C30xide yar aca 12 C3diol Traditional H20 Electrolyte Hypothetical Other Match C Formula lt Add Pure lt Substitute gt Sort List M Show Synonyms Cluster i Selected Component by Type Delete Basis 1 Component List 5 Inthe Components Available group select the FullLName Synonym radio button 3 83 View Downstream Operation icon 3 84 Dynamic Simulation 6 Inthe Match field start typing Nitrogen HYSYS filters the component list to match your input 7 When Nitrogen is selected in the list press the ENTER key Nitrogen is added to the Selected Components List Close the Component List view Close the Fluid Package Basis 1 property view In the Simulation Basis Manager view click on the Return to Simulation Environment button 10 On the PFD double click the Reactor Vent stream icon to open its property view 11 Click the Product Block button or the View Downstream Operation icon The Product Block view appe
311. l in the Name row 3 Type the new stream name Prop Oxide then press ENTER HYSYS automatically creates the new stream Figure 3 33 Name Prop Oxide New lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt Sea Material Streams Energy Streams Unit Ops ProductBlock Prop Oxid C Include Sub Flowsheets FeederBlock_Prop Oxide L Show Name Only Number of Hidden Objects 0 When you pressed ENTER after typing in the stream name HYSYS automatically advanced the active cell down one cell to Vapour Fraction Next you will define the feed conditions for temperature and pressure in this case 75 F and 1 1 atm 4 Clickin the Temperature cell for Prop Oxide Chemicals Tutorial 29 Tutorial 3 29 5 Type 75 in the Temperature cell In the Unit drop down list HYSYS displays the default units for temperature in this case E Figure 3 34 Workbook Case Main Df x Prop Oxide Yapour Fraction lt empty gt Temperature F Pressure psia lt empty gt Molar Flow Ibmole hr lt empty gt lt empty gt lt empty gt cm ia Material Streams Energy Streams Unit Ops ProductBlock Prop Oxid C Include Sub Flowsheets FeederBlock_Prop Oxide L Show Name Only Number of Hidden Objects 0 6 Since this is the correct unit press ENTER HYSYS accepts the temperature 7 Clickin the Pressure cell for
312. le Frac Workbook Pr 0 0448 0 2581 0 2592 0 0200 Comp Mole Frac Workbook i B 0 0078 0 1044 0 1259 0 4449 Comp Mole Frac Workbook n f Name Material Streams P T Flow Compositions FeederBlock_Feed 1 MIx lt 100 0 0049 xx New xx 0 0908 Energy Streams Unit Ops 0 1212 0 5351 C Include Sub Flowsheets L Show Name Only Number of Hidden Objects 1 97 1 98 You can continue to this dynamic section with the case you built during the steady state section or you can open the completed steady state version which is the starting point for this dynamic section called TUTOR1 hsc in the HYSYS Samples directory Feed 1 MixerOut Feed2 ax 100 This is only one method of preparing a steady state case for Dynamic mode A completed dynamic case has been pre built and is called dyntut1 hsc in the HYSYS Samples directory 1 98 InletSep Dynamic Simulation 1 3 Dynamic Simulation In this tutorial the dynamic capabilities of HYSYS will be incorporated into a basic steady state gas plant model The plant takes two different natural gas streams containing carbon dioxide and methane through n butane and combines and processes them in a simple refrigeration system A series of separators and coolers removes the heavier hydrocarbon components from the natural gas stream allowing it to meet a pipeline dew point specification
313. le list 11 In the Variable Description field change the description to Trim Duty and click the OK button The variable now appears in the Databook Figure 2 134 Yariable Navigator Flowsheet Variable Case Main Bottom Steam Heat Flow Atmos Tower COL1 Cond Duty Overall UA Crude Duty Power Diesel Temperature Approact Object Filter Diesel Steam User Variables All Utility flow rate Utility Fluid Cp j Utility Fluid Holdup C UnitOps Navigator Scope Utility Inlet Temp Logicals Flowsheet eta iad on EN ColumnOps ility minimum flow rat C Case Preheat Crude Utility Outlet Temp C Custom C Basis Residue Custom Utility Streams Variable Description Trim Duty Cancel 12 Click the Insert button again to add the third variable the ASTM D1160 cut point from the Residue BP Curves utility 13 Select the Utility radio button in the Navigator Scope group 14 Select Residue BP Curves in the Object list 15 Select ASTM D1160 Vac in the Variable list 16 Select the fifth item listed in the Variable Specifics column This corresponds to the 5 volume cut point 2 106 Refining Tutorial 17 In the Variable Description field change the variable name to ASTM 1160 Vac 5 Residue and click the OK button Figure 2 135 Yariable Navigator Case Variable Variable Specifics Case Kerosene BP Curves Acentric Factor a Cut Pt 0 0 Residue BP Curves Aromatic Mole Cut Pt 1 00 AST
314. led the next step is to install the low temperature separator LTS to separate the gas and condensed liquids in the ColdGas stream Adding and Connecting the LTS 1 Make some empty space available to the right of the Chiller using the horizontal scroll bar Position the cursor over the Separator icon on the Object Palette Right click and hold then drag the cursor over the PFD to the right of the Chiller The cursor changes to a special bulls eye cursor The bulls eye indicates the location of the operation icon 4 Release the right mouse button to drop the Separator onto the PFD A new Separator appears with the default name V 100 Click the Attach Mode icon on the PFD tool bar Position the cursor over the right end of the ColdGas stream icon The connection point and pop up Out appears 7 With the pop up visible left click and hold then move the cursor toward the left inlet side of the Separator Multiple connection points appear at the Separator inlet 8 Place the cursor near the inlet area of the Separator A solid white box appears at the cursor tip 9 Release the mouse button and the connection is made Hi Attach Mode icon Gas Processing Tutorial Adding Connections The Separator has two outlet streams liquid and vapour The vapour outlet stream LTSVap which is the shell side inlet stream for Gas Gas has already been created The liquid outlet will be a new stream 1 Inthe PFD
315. les gas heating value The two primary building tools the Workbook and the PFD will be used to install the streams and operations and to examine the results while progressing through the simulation Both of these tools provide you with a lot of flexibility in building your simulation and in quickly accessing the information you need The Workbook will be used to build the first part of the flowsheet starting with the feed streams and building up to and including the gas gas heat exchanger The PFD will be used to install the remaining operations from the chiller through to the column 1 5 Steady State Simulation All commands accessed via the toolbar are also available as menu items L New Case icon The Simulation Basis Manager allows you to create modify and manipulate fluid packages in your simulation case Most of the time as with this example you will require only one fluid package for your entire simulation 1 Setting Your Session Preferences 1 To start a new simulation case do one of the following e From the File menu select New Case e Click the New Case icon The Simulation Basis Manager appears Figure 1 3 Simulation Basis Manager Component Lists Master Component List View Add Delete Copy Import mot Export EE Refresh a Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Next you will set
316. list HYSYS displays the default units for temperature in this case E This is the correct unit for this exercise 3 Press the ENTER key Your active location should now be the Pressure cell for Feed 1 If you know the stream pressure in another unit besides the default unit of psia HYSYS will accept your input in any one of a number of different units and automatically convert the supplied value to the default for you For this example the pressure of Feed 1 is 41 37 bar 1 22 Steady State Simulation 1 Inthe Pressure cell type 41 37 2 Clickthe in the Unit drop down list to open the list of units or press the SPACE BAR to move to the Units drop down list Figure 1 22 Workbook Case Main iquid Volume Flow barrel day Heat Flow Btu hr lt empty gt 3 Either scroll through the list to find bar or begin typing it HYSYS will match your input to locate the required unit 4 Once bar is selected press the ENTER key HYSYS will automatically convert the pressure to the default unit psia When you press ENTER the active selection moves to the Molar Flow cell for Feed 1 5 Inthe Molar Flow cell type 6 and press ENTER The default Molar Flow unit is already MMSCFD so you do not have to modify the units Gas Processing Tutorial 238 Processing Tutorial 1 23 Providing Compositional Input In the previous section you specified the stream conditions Next you will input the c
317. llows you to supply values for the default column specifications that HYSYS has created 15 Enter a Vapour Rate of 2 0 MMSCFD and a Reflux Ratio of 1 0 The Flow Basis applies to the Vapour Rate so leave it at the default of Molar Figure 1 84 Si Distillation Column Input Expert x Vapour Rate 00000 Reflux Ratio 1 000 Flow Basis Molar lt Prev Done Side Ops gt Specifications page 4 of 4 Cancel 16 Click the Done button and the Distillation Column property view appears displaying the Connections page of the Design tab Figure 1 85 L Column DePropanizer COL1 Fluid Pkg Basis 1 Z Peng Robinson Design Column Name DePropanizer Sub Flowsheet Tag cou C Tan C Total Partial Full Reflux Condenser Energy Stream CondD uty v Delta P Ovhd Specs 0 0000 psi Ovhd Vapour Outlet Specs Summary Connections Monitor Subcooling Notes Optional Side Draws Inlet Streams 500 0 psi Opsa f Steam Type Draw Stage inet Stages Draw Stage Towereed lt Stream gt gt re P reb 205 0 psia n l EN Delta P 0 0000 psi Reboiler Energy Stream R ebDuty Stage Numbering TopDown BottomUp Edit Trays Bottoms Liquid Outlet LiquidProd v B Design Side Ops Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged V Update Outlets Ignored Gas Pr
318. low barrel day eat Flow Btu hr Name apour Fraction emperature F iquid Volume Flow barrel day Heat Flow Btu hr Material Streams P T Flow FeederBlock_Preheat Cr PreFlash Refining Tutorial 2 97 13 When you are finished working in the Column environment return to the Main Flowsheet by clicking the Enter Parent Simulation Environment icon 14 Open the PFD for the Main Flowsheet then select Auto Position All from the PFD menu item HYSYS arranges the Main Flowsheet PFD in a logical manner according to the layout of the flowsheet ap Preheat Crude PreFlash PreFlashLig Furnace CrudeDuty PreFlashVap HotCrude TrimDuty BottomSteam SL TowerFeed DieselSteam AGOSteam Atmos Tower 2 2 9 Viewing and Analyzing Results 1 Open the Workbook to access the calculated results for the Main Flowsheet The Material Streams tab of the Workbook appears below Figure 2 120 Preheat Crude Diesel Steam AGO Steam PreFlash ap PreFlashLigq Hot Crude OffG as Diesel AGO Tower Feed Naphtha Residue WasteH20 Kerosene _ CondDuty Bottom Steam 1 0000 375 0 1 0000 300 0 50 00 1 0000 300 0 50 00 1 0000 0 0000 450 0 75 00 0 5478 0 6040 650 0 65 00 641 6 65 00 L 166 5 2500 3431 3431 3814 1 144e 006 1
319. lows you to complete the compositional input Figure 3 36 The Input Composition for Stream view is Modal Ni Input Composition for Stream Prop Oxide indicated by the thick border i olek lactic Composition Basis and the absence of the amp Mole Fractions wee as lt empty gt e Minimize Maximize buttons in TRET Mass Fractions C Lig Volume Fractions C Mole Flows Mass Flows the upper right corner When a Modal view is visible you will not be able to move outside the view until you finish with it by clicking either the Cancel or OK button C Lig Yolume Flows Erase Normalize Cancel E E E D a E ae i Composition Controls ae a al 3 30 These are the default colours yours may appear differently depending on your settings on the Colours page of the Session Preferences The following table lists and explains the features available to you on the Chemicals Tutorial Input Composition for Stream view Features Compositional Basis Radio Buttons Normalizing Calculation status colour Description You can input the stream composition in some fractional basis other than Mole Fraction or by component flows by selecting the appropriate radio button before providing your input The Normalizing feature is useful when you know the relative ratios of components for example 2 parts N2 2 parts CO2 120 parts C1 etc Rather than manually convertin
320. lts Variables Process Data T ables Strip Charts Data Recorder Case Studies To automate the study the Dependent Variable range and Step Size must be given 6 Click the View button to access the Case Studies Setup view Define the range and step size for the Stripper Feed Temperature as shown below Figure R2 9 Sy Case Studies Setup Main Case Studies Temperature values are Case Study 1 Case Study 1 given in F DE Independent Yariables Setup Display Properties Failed States To begin the Study click the Start button Click the Results button to view the variables If the results are in graphical form click the Table radio button on the Case Studies view R2 11 RRB ase Study 2 Case Study R2 12 He 6 Results The results of this study appear below Figure R2 10 Case Studies Main Stripper Feed Temperature F Cooling Water Btu hr Steam Btu hr State 1 State 2 State 3 State 4 State 5 190 0 1 515e 008 2 091 e 008 195 0 1 542e 008 2 080e 008 200 0 1 568e 008 2 070e 008 205 0 1 597e 008 2 059e 008 210 0 1 626e 008 2 050e 008 Feed Bottoms UA Btu F hr Lig MF Tray 2 lb hr Lig MF Tray lb hr 1 054e 006 1 584e 005 9 229e 005 1 214e 006 1 611e 005 9 215e 005 1 408e 006 1 640e 005 9 202e 005 1 645e 006 1 668e 005 9 188e 005 1 959e 006 1 638e 005 9 175e 005 Yap M
321. lts 1 Click the Workbook icon to access the calculated results for the Main Flowsheet The Material Streams tab and Compositions tab of the Workbook appears below i Material Streams P T Flow Compositions FeederBlock_Prop Oxide MIx lt 100 Workbook Case Main OF x Energy Streams Unit Ops C Include Sub Flowsheets L Show Name Only Number of Hidden Objects Figure 3 87 Name Prop Oxide Water Feed Mixer Dut Reactor Vent 1 0000 0 0000 0 0000 100 75 00 75 00 75 00 140 0 16 17 16 17 16 17 16 17 150 0 610 6 760 6 0 0000 8712 1 100e 004 1 971e 004 0 0000 20 83 22 01 42 84 0 0000 7 G04e 006 7 481e 007 8 262e 007 0 0000 Reactor Prods Glycol OvhdVap RecyProds 0 0000 0 0000 1 0000 0 0000 140 0 375 7 159 0 159 0 16 17 17 00 15 00 15 00 618 5 142 8 4 369e 005 475 8 17te 004 1 082e 004 2 006e 003 8890 38 75 20 78 4701e006 17 97 8 714e 007 2 803e 007 2534 5700e 007 Name 22O O Water Feed Mixer Dut Reactor Vent T0000 0 0000 0 1972 0 3311 0 0000 0 0000 0 0000 0 0049 0 0000 1 0000 0 8028 0 6040 Name Reactor Prods Glycol Ovhd ap RecyProds 0 0129 0 0000 0 6962 0 0167 0 2296 0 9950 0 0000 0 0000 0 7575 0 0050 0 3038 0 9833 Name o New omp M
322. ly those components that match your input Figure 2 10 Components Available in the Component Library Match fwd View Filters Sim Name C Full Name Synonym C Formula H20 Water Naphthalene White_Tar Methanol Wood_Alcohol Methanol Wood_Naphtha M Show Synonyms Cluster 6 With Water selected add it to the Current Component List by doing one of the following e Press the ENTER key e Click the Add Pure button e Double click on Water Steady State Simulation You can also use the Family Filter to display only those components belonging to certain families Next you will add Propane to the component list using a Family Filter Filters x Property Package Filter I Recommended Onl lt none gt ikai Family Type Filter Use Filter 7 Ensure the Match field is empty and click the View Filter button The Filters view appears as shown on the left 8 On the Filters view check the Use Filter checkbox to activate the Family Filter 9 Check the Hydrocarbons checkbox The remaining components are known to be hydrocarbons 5 Figure 2 11 Components Available in the Component Library Filters E3 Match Property Package Filter On the i I Recommended O Component Sim Name C Full Name Synonym C Formula E a ER Hd a el a HY E Filters view View view Propane appears near the top of the filtered list M Show Synonyms Methane Ethane Propane i Butane
323. m AGO Steam 3_AGOSS P H Flash ie Split Inlets Outlet Streams Internal Stream Residue External Stream Residue Outlet Stage 29 Main TS Transfer Basis P H Flash dP Top 3 000 psi Naptha Off Gas Cond Duty Naptha Off Gas Cond Duty Condenser Condenser Condenser P H Flash P H Flash None Req d P Top f 9 70 psia dP Bot Kempty Waste H20_ _ WasteH20 P H Flash Le re TE TE P Bot 31 70 psia The Connections page of a standard refluxed absorber property view is essentially identical to the first page of the refluxed absorber Input Expert with a column schematic showing the feed and product streams Side equipment have been added to the standard refluxed absorber however making the column non standard The Connections page has therefore been modified to show tabular summaries of the Column Flowsheet Topology i e all equipment Feed Streams and Product Streams The column has 40 Total Theoretical Stages 29 in the main tray section 1 condenser for the main column 9 in the side strippers 3 side strippers with 3 stages each 1 reboiler for the Kerosene side stripper This topology results in 4 Total Tray Sections one for the main column and one for each of the three side strippers 2 83 Steady State Simulation Completing the Column Connections When the stream attachments were made on the initial page of the Input Expert HY
324. m of the environment view shows that the stream has an unknown pressure As you specify the conditions of Preheat Crude the message displayed in the Object Status window is updated appropriately Before specifying the feed conditions you can view the stream composition which was calculated by the Oil characterization Viewing the Feed Composition 1 In the Workbook click the Compositions tab to view the composition of the streams Figure 2 39 Workbook Case Main Name _ _ __ omp Mole Frac NBP 0 113 Comp Mole Frac NBP 0 139 Comp Mole Frac NBP 0 164 Material Steams Compositions Energy Streams Unit Ops ProductBlock_Preheat C L Include Sub Flowsheets FeederBlock_Preheat Cr L Show Name Only Number of Hidden Objects 0 Save icon If you enter a name that already exists in the current directory HYSYS ask you for confirmation before over writing the existing file Workbook icon Refining Tutorial The light ends and petroleum hypocomponents are listed by Mole Fraction To view the components which are not currently visible use the up and down arrow keys or the vertical scroll bar to advance down the component list Before proceeding any further to install streams or unit operations save your case 2 Doone ofthe following e Click the Save icon on the toolbar e Select Save from the File menu e Press CTRL S If this is the first time you have saved your case the
325. make the connection 9 Repeat steps 6 to 8 to connect the Hot Crude stream to the Mixer 10 Position the cursor over the right end of the mixer icon The connection point and pop up Product appears 11 With the pop up visible click and drag to the right of the mixer A white stream icon appears with a trailing line attached to the mixer outlet PreFlashVap 12 With the white stream icon visible release the mouse button HYSYS creates a new stream with the default name 1 13 Release the crri key to leave Attach mode E Ei 14 Double click on the outlet stream icon 1 to access its property view Hot MIX 100 When you created the mixer outlet stream HYSYS automatically combined the two inlet streams and flashed the mixture to determine the outlet conditions 15 In the Stream Name cell rename the stream TowerFeed then close the view Figure 2 74 Worksheet Tower Feed a Vapour Phase Fraction 0 60964 Conditions Temperature F _ l 639 29 Properties Pressure psia 65 000 Molar Flow Ibmole hr 3813 9 Mass Flow lb hr 1 1442e 006 K Value Std Ideal Liq Vol Flow barrel day 1 0000e 005 User Variables Molar Enthalpy Btu Ibmole 1 519e 005 Molar Entropy Btu Ibmole F 313 94 ae Heat Flow Btu hr 5 791 7e 08 Cost Parameters Liq Vol Flow Std Cond barrel day 100000 Fluid Package Basis 1 Composition Worksheet Attachments Dynamics ee Define from Other St
326. mber of components NC and property package PP The new Fluid Package is assigned by default to the Main Simulation as shown in the Flowsheet Fluid Pkg Associations group Now that the Basis is defined you can install streams and operations in the Simulation environment also referred to as the Parent Simulation environment or Main Simulation environment 3 25 3 26 Steady State Simulation 3 2 5 Entering the Simulation Environment To leave the Basis environment and enter the Simulation environment do one of the following tO e Click the Enter Simulation Environment button on the Simulation Basis Manager Enter Simulation e Click the Enter Simulation Environment icon on the toolbar Environment Icon When you enter the Simulation environment the initial view that appears is dependent on your current preference setting for the Initial Build Home View Three initial views are available namely the PFD Workbook and Summary Any or all of these can be displayed at any time however when you first enter the Simulation environment only one is displayed For this example the initial Home View is the Workbook HYSYS default setting Figure 3 32 J 4811 CHEMICAL ss hsc HYSYS 3 1 Beta File Edit Simulation Flowsheet Workbook Tools Window Help zy as Environment Case Main D SH Taal Ze Lee As Mode Steady State E Workbook Case Main Edf Case Main xi CE A gt gt Temperature F 7 Molar Flow Ibmole hr
327. me gt Design Name Connections Design Performance Dynamics Delete Ignored 2 102 Refining Tutorial Change the name from its default Utility 1 to Residue BP Curves Change the Basis to Liquid Volume by selecting it in the drop down list The next task is to attach the utility to a material stream 5 Click the Select Object button and the Select Process Stream view appears Figure 2 129 Select Process Stream x Flowsheet Object Case Main AGO OK Atmos Tower COL1 AGO Steam Bottom Steam Object Filter All C Streams C UnitOps C Logicals C ColumnOps C Custom Tower Feed Trim Duty WasteH20 Cancel 6 Select Residue in the Object list then click the OK button HYSYS calculates the boiling point curves The completed Performance tab appears below Figure 2 130 Notice that the stream name Residue now appears in the i Stream cell Performance m Results Results Cut Point TBP ASTM D86 D86 Crack Reduced AST a a F F F 417 6 458 6 458 6 Boiling Point Curves Residue BP Curves Critical Props Cold Props Plots Design Performance 7 Click the Close icon on the Residue BP Curves view and then on the Available Utilities view 2 103 Steady State Simulation o c 11 Using the Databook The HYSYS Databook provides you with a convenient way to examine your flowsheet in more deta
328. mine based on 1000 BTU Ib Steam Primary Amine e g MEA Secondary Amine e g DEA Tertiary Amine e g MDEA eee E Water make up is necessary since water will be lost in the absorber and regenerator overhead streams 9 Install a Mixer operation to combine the lean amine from the regenerator with the MAKEUP H20 stream These streams mix at the same pressure 10 Define the composition of MAKEUP H20 as all water and specify a temperature of 70 F and pressure of 21 5 psia The flow rate of the total lean amine stream will be defined at the outlet of the mixer and HYSYS will calculate the required flow of makeup water 11 Set the overall circulation rate of the amine solution by specifying a Standard Ideal Liquid Volume Flow of 190 USGPM in stream DEA TO COOL HYSYS will back calculate the flow rate of makeup water required Mixer MIX 100 Tab Page In this cel Enters Design Inlets MAKEUP H2O Connections LEAN FROM L R Design Parameters Automatic Pressure Assignment Set Outlet to Lowest Inlet ii Std Liq Vol Flow 190 5 USGPM a O Composition MAKEUP H20 Worksheet Temperature MAKEUP H20 G1 12 The Cooler and the Pump operations will remain unconverged until the Set operation has been installed Acid Gas Sweetening with DEA When you have finished specifying the DEA TO COOL stream you will receive a warning message stating that the temperature of the Makeup H20 stream exceeds the r
329. mpty gt P amp _3 Duty Pa 3 500e 007 Btu hr 3 50e 007 0 0000 View Add Spec Group Active Update Inactive Degrees of Freedom 0 kalkara lka lka ddd 714 kalkalkalkalka lkara lka lkakalkalkalkalka kalkakalkakakakalka lka ika ikalia 74 The addition of the pump arounds has created six TE n more degrees of freedom The addition of each pump around created two additional degrees of resulting in a total of 13 freedom As with the side strippers the specifications for the pump available degrees of arounds have been added to the list and were automatically activated freedom Currently 13 Specifications are active so the overall Degrees of Freedom is zero 2 82 Refining Tutorial 14 Select the Connections page Figure 2 102 L Column Atmos Tower COL1 Fluid Pkg Basis 1 Peng Robinson Column Name Atmos Tower Sub Flowsheet Tag co L1 Design Connections Monitor Specs Specs Summary Subcooling Notes Inlet Streams Internal Stream Bottom Steam External Stream _ Bottom Steam Inlet Stage 29 Main TS Transfer Basis P H Flash 2 83 O x Stage Numbering Top Down Tower Feed Tower Feed 28 Main TS P H Flash C Bottom Up Trim Duty Kero55_Energy Diesel Steam Trim Duty lt lt Stream gt gt Diesel Steam 28_ Main TS KeroSS_Reb 3__DieselSS None Req d None Req d P H Flash Edit Trays AGO Stea
330. mulation tab Options page ensure that the Use Input Experts checkbox is selected checked then close the view 3 Double click on the Distillation Column icon on the Object Palette The first page of the Input Expert appears Figure 1 80 Ni Distillation Column Input Expert Condenser Energy Stream Condenser C Total Ei Column Name T 00 Partial Ovhd Outlets C Full Rflg x Water Draw Inlet Streams Inlet Stage lt Stream gt gt Optional Side Draws gt lt lt Stream gt gt Reboiler Energy Stream Bottoms Liguid Outlet sj Stage Numbering Top Down C Bottom Up en coe Connections page 1 of 4 Cancel When you install a column using a pre built template HYSYS supplies certain default information such as the number of stages The current active cell is Numb of Stages Number of Stages indicated by the thick border around this cell and the presence of 10 default number of stages Steady State Simulation Some points worth noting e These are theoretical stages as the HYSYS default stage efficiency is one If you want to specify real stages you can change the efficiency of any or all stages later e The Condenser and Reboiler are considered separate from the other stages and are not included in the Numb Stages field For this example 10 theoretical stages will be used so leave the Number of Stages at its default value 4 Move to the Inlet Str
331. n Declares the myFeeds variable and sets it to the feed streams collection of the operation Checks if a linked stream name is already defined Dim myFeeds As Object Set myFeeds ActiveObject Feedsl Check if a stream name is already defined If Not LinkStream Variable IsKnown Then fener Rese ato Ole ee use that stream name as the linked stream name myFeeds Item 0Q name else If no stream is connnected as feed use the default LankStream Variab ke Value f eeq listed stream name of feed end if end if EZI Sub Catch MsgBox Initialize Error If myFeeds Count gt 0 Then If a feed stream is connected to the unit operation Signifies the end of the initialization subroutine This line does not need to be added 1 Once this code is entered press the OK button to close the Edit Existing Code view On the Code page of the Design tab click the Initialize button Select the Connections page of the Design tab It should contain their new designations 4 Select the Variables page The LinkCase should contain the case LinkCase2 including the path The LinkStream variable should contain feed 5 Select the Connections page If the feed drop down list is empty the value of LinkStream variable Variables page should be feed X1 12 Case Linking As Linking X1 13 Oreye X1 4 2 Operation Execution Sub Execute On Error Goto EarlyGrave Dim Sta
332. n at the bottom of the Assay view HYSYS calculates the Assay and the status message at the bottom of the view changes to Assay Was Calculated 2 21 2 28 Steady State Simulation The plot view can be re sized to make the plot more readable To re size the view do one of the following e Click and drag the outside border to the new size e Click the Maximize icon o Maximize icon 2 28 8 Click the Working Curves tab of the Assay property view to view the calculated results Figure 2 27 Ni Assay Assay 1 Assay Working Curves Point t Cum Moles pag Mole wt Mass Density Viscosity 1 ied 2 EL eL oe 0 00000 0 01000 T aI m0 0 01000 0 02000 0 01000 0 03000 0 01000 0 04000 0 01000 0 05000 0 01000 0 06000 omo00 0 07000 0 01000 0 08000 0 01000 0 09000 0 01000 0 10000 0 02500 0 12500 0 02500 0 15000 0 02500 0 17500 0 02500 0 20000 HYSYS has calculated 50 points for each of the Assay Working Curves To view the Assay data you input in a graphical format click the Plots tab The input curve that appears is dependent on the current variable in the Property drop down list By default HYSYS plots the Distillation TBP data This plot appears below Figure 2 28 Ni Assay Assay 1 Property Selection Input TBP Distillation Assay 1 Property Distillation v Temperature F om mo AD I m D AD D D AD io
333. n can be run for a range of Stripper Feed temperatures e g 190 F through 210 F in 5 degree increments by changing the temperature specified for Stripper Feed in the worksheet You can automate these changes by using the Case Studies feature in the DataBook Open the DataBook property view Tools menu 2 On the Variables tab enter the variables as shown below Flowsheet Object Variables Variables Description FeedBotoms UA UA T 100 Main TS Stage Liq Net Mass Liq MF Tray 2 SW Stripper Flow 2__ Main TS Main TS Stage Liq Net Mass Liq MF Tray 7 Flow 7__ Main TS Main TS Stage Vap Net Mass Vap MF Tray 2 Flow 2__ Main TS Main TS Stage Vap Net Mass Vap MF Tray 7 Flow 7__ Main TS Click the Case Studies tab In the Available Case Studies group click the Add button to create Case Study 1 Sour Water Stripper R2 11 5 Check the Independent and Dependent Variables as shown below Figure R2 8 lt DataBook Available Case Studies Case Studies Data Selection d Current Case Study Case Study 1 Delete Li Obiect Variable Ind Heat Flow a View pO Reb _ Heat Flow F Stripper Feed Temperature V Feed Bottoms UA T Main TS Stage Lig Net Mass Flow 2 Main TS F Main TS Stage Liq Net Mass Flow _Main TS F Main TS Stage Vap Net Mass Flow 2 Main TS Main TS Stage Vap Net Mass Flow 7__ Main TS kalkacak 14 Available Displays Table C Graph Resu
334. n tower modeled as a Refluxed Absorber and define as indicated below Refluxed Absorber Lights Tab Page inthis cel Emere Connections Reboiler Pressure 101 325 kPa Pressure Profile 2 Delete the default Btms Prod Rate and Reflux Rate specifications from the Column Specification group 3 Add the following new column specifications Design tab Specs page Specifications Tab Page inthis cel Enters Design Specs Vap Prod Rate Draw Flow Basis Spec Value Comp Fraction Stage Flow Basis Phase Spec Value Component Reflux Ratio Stage Flow Basis Spec Value Distillate Rate Draw Flow Basis Spec Value Active Light_Vent Molar 1 6 kgmole hr Active Condenser Mass Fraction Liquid 0 88 Ethanol Estimate Condenser Molar 5 00 Estimate 2ndEtOH Molar 2 10 kgmole hr C1 9 Steady State Simulation 4 Ifrequired click the Run button in the Column property view to calculate the Light Tower product streams Rectifier The primary product from a plant such as this would be the azeotropic mixture of ethanol and water The Rectifier serves to concentrate the water ethanol mixture to near azeotropic composition The Rectifier is operated as a conventional distillation tower It contains a partial condenser as well as a reboiler 1 Add the Rectifier column modeled as a distillation tower and define it using the following information Column RECT Tab Page IN t
335. nOps Flowsheet Reactor LC Lower Heating Valt eon j C Case Reactor TC Mass Density C Basis WaterFeed FC Cust steers ustom C Utility lire LV Prop Oxide Mass Heat Capacit VIRasetear Prades hd soo Host NEU amre Variable Description Mass Flow Cancel 3 92 Chemicals Tutorial 8B Tutorial 3 93 Select the Flowsheet Object and Variable for any of the suggested variables For Reactor Prods also select the Variable Specifics indicated A list of suggested variables appears below Variables to Manipulate VEET Variables to Monitor WElatele Variable Specifics Reactor Prods Comp Molar Flow 12C3Oxide Rector Liquid Percent Level 3 Click on the OK button to return to the Databook The variable will now appear on the Variables tab 4 Repeat the procedure to add all remaining variables to the Databook 5 Click the Strip Charts tab in the Databook view Figure 3 121 DataBook i Oo EI Available Strip Charts Individual Strip Chart Data Selection Vi Sample Int Cooling Duty Reactor Prods Reactor Temp Prop Oxide Mass Flow Water Feed Mass Flow Reactor Vessel Temperature Reactor Prods Comp Molar Flow 12C30xide Reactor Liquid Percent Level cane Variables Process Data Tables Strip Charts Data Recorder Case Studies 6 Click the Add button HYSYS will create a new strip chart with the default name DataLoggerl 7 Inthe Logger Name field change the n
336. namics Delete Column Environment Run Reset ES Update Cutlets I Ignored 2 89 2 90 Steady State Simulation Viewing Boiling Point Profiles for the Product Stream You can view boiling point curves for all the product streams on a single graph 1 On the Performance tab click on the Plots page Figure 2 110 Column Atmos Tower 7 COL1 Fluid Pkg Basis 1 7 Peng Robinson Performance m Tray by Tray Properties F aizi Core ew Gish Column Tray Ranges ummary Pressure All Column Profiles Flow View Table Transport Properties Feeds Products Composition Plots K Values P Live Updates C Single Tower Light Heavy Key C From To Refinery Assay Curves View Graph Molecular Wt Assay Density Assay View Table User Properties Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Distop Delete Column Environment Run Reset Converged MV Update Outlets Ignored 2 Inthe Refinery Assay Curves group select Boiling Point Assay 3 Click the View Graph button and the Boiling Point Properties view appears Figure 2 111 Boiling Point Properties No Tray Attach Pim EG Boiling Point Properties No data is plotted on ji the graph since there is currently No Tray Attached as shown in the title bar 5 gt E B tt ete Perceni Composiiion 2 90 Refining Tutorial 4 Click the Profile Data C
337. nd Cut is automatically calculated based on the current Cut Option In this case the Blend was calculated based on Auto Cut the default Cut Option HYSYS calculated the Blend based on the following default values for the boiling point ranges and number of cuts per range e IBP to 800 F 25 F per cut generating 800 IBP 25 hypocomponents e 800 to 1200 F 50 F per cut generating 8 hypocomponents e 1200 to 1400 F 100 F per cut generating 2 hypocomponents The IBP or initial boiling point is the starting point for the first temperature range The IBP is the normal boiling point NBP of the heaviest component in the Light Ends in this case n Pentane at 96 9 E The first range results in the generation of 800 96 9 25 28 hypocomponents All the cut ranges together result in a total of 28 8 2 38 hypocomponents 5 Click the Tables tab to view the calculated properties of these hypocomponents Ni Blend Blend 1 Of x Table Type Component Physical Properties Com onent Properties NBP Density Viscosity Viscosity2 P P Comp Name F Mole Wt API oP oP Table Contrat 111 2 82 07 92 55 0 12785 5 9949e 00 Main Properties __NBP_136 136 0 89 45 91 24 0 13306 6 3050e 00 Other Properties NBP_161 160 8 105 9 85 75 0 14056 6 7445e 00 Dil NBP_185 184 9 122 4 81 14 0 15061 7 3233e 00 Benn i NBP_210 210 4 137 4 76 89
338. nd implement key control loops using PID Controller logical operations Although these controllers are not required to run in dynamic mode they will increase the realism of the model and provide more stability Level Control First you will install a level controller to control the liquid level in the CSTR Reactor operation 1 Press F4 to activate the Object Palette if required 1 Inthe Object Palette click the Control Ops icon A sub palette appears 2 Inthe sub palette click the PID Controller icon The cursor changes to include a frame and a sign 3 Inthe PFD click near the Reactor icon The IC 100 icon appears This controller will serve as the Reactor level controller 4 Double click the IC 100 icon The controller s property view appears Figure 3 114 1C 100 Name fic 00 Process Variable Source Object OO Select PY Variable Optional i E Output Target Object Select OP Remote Setpoint Source C Connections Parameters Monitor Strpchart User Variables Delete Face Plate Chemicals Tutorial 3 87 5 Inthe Connections tab click in the Name field and change the name to Reactor LC 6 Inthe Process Variable Source group click the Select PV button The Select Input PV view appears 7 Inthe Object group list select Reactor In the Variable list select Liquid Percent Level Click the OK button Figure 3 115 Select Input P For Reactor LC Flowsheet
339. nd view the results in the monitored variables in the strip charts 1 129 1 130 Dynamic Simulation 1 130 Refining Tutorial c Refining Tutorial ZA INTOdUCHON iani a a aa aaa aaa a Eaa 3 2 2 Steady State Simulation cccccceesseeeeeesseceeenseeseeenseeeeeenseeeeeennees 5 2 2 1 Process DeSCrip ti ieeM Mtn oe cecccSleccescseceseseeeneeeeeens 5 2 2 2 Setting Your Session PreferenCes cccccceeseeeeeeeeeeeeeeeeaees 7 2 2 3 Builciaggire Simulation QA aeaaeae 10 2 2 4 Entering the Simulation Environment c ccccccseeeeeeeeeees 37 2 2 5 sing the WorkbDOok niinen M on aaaea 39 2 2 6 Installing Unit Operations ccccecceeeeeeeeeeeeeeeeeeeeeeeeeeeeeeas 47 2 2 7 Using Workbook Features ccccccesecceeceeeeeeeeaeeeeeesseeeeeeeens 52 2 2 8 sing tne REDRE se 56 2 2 9 Viewing and Analyzing Results ccceeeeeeeseeeeeeeeeeeeeeeees 97 2 2 10 Installing a Boiling Point Curves Utility 0 0 ee 99 2 2 11 Using ihesBDatabook 46OF cccccccecccccllBiccsceseeesscseees 104 2 3 Dynamic SIMUTAMION 2200 000001 Mansccccnnsssccscnssssccnsssssecenssssccnnessecees 114 2 3 1 Simplifying the Steady State Flowsheet eeee 115 2 3 2 Adding Equipment amp Sizing COlUMNS cccseeeeeeeeeeeeees 119 2 3 3 Adding Controller Operations cccceceeeeeeeeeeeeeeeeeeeeeees 130 2 3 4 Adding Pressure Flow Specifications
340. ned stream was then fed to the atmospheric crude column for fractionation The dynamic refining tutorial only considers the crude column That is the crude preheat train is deleted from the flowsheet and only the crude column in the steady state refining tutorial is converted to dynamics Figure 2 146 To Com iter Remy Conde ier Haphtha TER Pa 1 Peter PA 1 Cooker TERET A 2 oO PA 2 Peter pa ook p p Dezel S5 Retr The main purpose of this tutorial is to provide you with adequate knowledge in converting an existing steady state column to a dynamics column The tutorial provides a single way of preparing a steady state case for dynamics mode however you can also choose to use the Dynamic Assistant to set pressure specifications size the equipment in the plant and or add additional equipment to the simulation flowsheet 2 114 In this tutorial you follow this basic procedure in building the dynamic model In this tutorial you are working with SI units The units are changed by entering the Preferences property view in the Tools menu bar In the Units tab specify SI in the Current Unit Set group Refining Tutorial This tutorial comprehensively guides you through the steps required to add dynamic functionality to a steady state oil refinery simulation To help navigate these detailed procedures the following milestones have been established for this tutorial 1 Obtain a
341. nents amp Fluid Package I Create a new component list and add the following components methane water carbon monoxide carbon dioxide hydrogen nitrogen and oxygen Create a fluid package defined as Peng Robinson On the Fluid Package view click the Rxns tab add the Global Rxn set then close the Fluid Package view Refer to Chapter 5 Reactions in the Simulation Basis manual for more information about how to define reactions and reaction sets The Rxn Components group only shows the components associated with the Fluid Package s To add or edit components select the Add Comps button The new components will automatically be added to any fluid package that uses the reaction Synthesis Gas Production Ce 2 c Defining the Reactions On the Reactions tab of the Simulation Basis Manager you can define the required reactions and attach them to reaction sets Selecting Reaction Components The reaction components are attached based on the associated fluid package and are listed in the Rxn Components group Figure C2 2 Rxn Components Reactions Methane l Add Rn Copy Rn Add Comps Components FluidPkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment C2 5 5 You can also define reactions and attach reaction sets in the Main Environment by selecting Reaction Package under Flowsheet in the main menu De
342. nergy Streams Unit Ops Main TS Condenser L Show Name Only Number of Hidden Objects 0 e Click the Column Runner icon to access the inside column property view This property view is essentially the same as the outside or main flowsheet property view ra 3 When you are finished in the column environment return to the main flowsheet by clicking the Enter Parent Simulation Enter Parent Simulation Environment icon in the tool bar or the Parent Environment button Environment icon on the column Worksheet view 1 75 1 76 Steady State Simulation 1 2 9 Viewing and Analyzing Results 1 Open the Workbook for the main case to access the calculated results for all streams and operations 2 Click the Material Streams tab Figure 1 96 Workbook Case Main OF Xx Feed 2 MixerOut Sep ap SepLig CoolGas SalesGas apour Fraction 0 8952 0 9013 0 8976 1 0000 0 0000 0 9388 1 0000 Temperature F 60 00 60 00 60 00 60 00 60 00 42 97 50 00 Pressure psia 600 0 600 0 600 0 6000 600 0 590 0 570 0 Molar Flow MMSCFD 6 000 4 000 10 00 8 976 1 024 8 976 7 018 Mass Flow Ib hr 1 675e 004 1 100e 004 2 775e 004 2 318e 004 4564 2318e 004 1 562e 004 Liquid Volume Flow barrel day 3012 1983 4995 4342 652 9 4342 3167 Heat Flow Btu hr 2 553e 007 1 628e 007 4 180e 007 3 605e 007 5 756e 006 3 652e 007 2 678e 007 LTS ap ColdGas LTSLig SalesDP TowerFeed Ovhd LiquidProd ap
343. ng 50 Comments Add this valve between the vapour outlet of the absorber DEA Contactor and the stream SWEET GAS in the absorber sub flowsheet VLV 100 COL2 DEA TO VALVE DEA TO COOL Design Parameters Rating Sizing Comments Tab Page Design Connection 2 COL2 Design Parameters 1 psi Rating Sizing Valve Opening 50 Comments Add this valve between the vapour outlet of the distillation column REGENERATOR and the stream ACID GAS in the Regenerator Column sub flowsheet Before proceeding any further ensure that the case is completely solved 1 Open the valves property view and move to the Sizing page of the Rating tab 2 Select the User Input radio button and specify the Valve Opening as indicated Click the Size Valve button Repeat for all valves in the simulation G1 20 For more information regarding Pressure Flow specifications in Column unit operations see Chapter 8 Column in the Operations Guide The pressure flow specification must be activated in the Dynamics tab on the Specs page by selecting the Active checkbox The steady state pressure flow values should be used as a specification Acid Gas Sweetening with DEA Adding Pressure Flow Specifications In order to run the integrator successfully the degrees of freedom for the flowsheet must be reduced to zero by setting the pressure flow specifications Normally you would make one pressure flow specification per flowsheet
344. ng Property T able l lear Pramarhi Add Utility The Envelope Utility view appears HYSYS creates and displays a phase envelope for the stream Just as with a Stream a Utility has its own property view containing all the information needed to define the utility Initially the Connections page of the Design tab appears To make the envelope property view more 4 Click the Performance tab then select the Plots page ace ee ues Or ie The default Envelope Type is PT size the view 5 To view another envelope type select the appropriate radio button in the Envelope type group Depending on the type of envelope selected you can specify and display Quality curves Hydrate curves Isotherms and Isobars To view the data in a tabular format select the Table page Figure 1 37 Envelope Envelope Utility 1 OF x Curves Plots th im AA lt empty gt Table its a Hydrate a Clear Envelope Type f PT C TY C PY TH PH TS TPS Performance Pressure pe i Design Performance Delete Ignored 1 32 Gas Processing Tutorial 1 33 6 Click the Design tab The Design tab allows you to change the name of the Utility and the stream that it is attached to and view Critical Values and Maxima Figure 1 38 A Utility is a separate entity i z N Envelope Utility 1 from the stream to which it Design Nare A is attached if you delete it Connections Stream Feed2 __ Select
345. ng Propane and Propene It may be easier to search by chemical formula C3H8 and C3H6 as the entire list is quite extensive Once these components are selected close the view Select the Soave Redlich Kwong SRK equation of state EOS as the property method for this case Ensure that the selected component you just created appears in the Component List Selection drop down list P1 3 Steady State Simulation The case will be setup in steady state using the Custom Column option Both the Rectifier and Stripper columns will be built in the same column environment P1 3 1 Starting the Simulation Defining the Feed stream In the Main Simulation environment define the conditions and compositions of the Feed stream as shown in the following table This example uses Field units If you need to change R the units go to the Tools Material Stream Feed men And AEA ne In this cell Enter Preferences command On ihe Variables tab chando your units to Field Comp Mole Frac Propene 08 Installing the Column 1 Click the Custom Column icon on the Object Palette The Custom Column feature will be used to build both columns in a single column environment 2 Click the Start with a Blank Flowsheeet button The column appears in the PFD Double click the column in the PFD to open the Column view 4 Click the Design tab and select the Connections page In the Inlet Streams group enter stream Feed as an External Feed
346. ng Robinson would appear in this filtered list In the Component List Selection group you could use the drop down list to find the name of any component lists you had created currently empty The View button opens the Component List View view of the selected component list If the selected component list contains components not appropriate for the selected property package HYSYS opens the Components Incompatible with Property Package view On this view you have the options of HYSYS removing the incompatible components from the component list or changing to a different property package using the drop down list or the Cancel button 2 15 Steady State Simulation 3 Close the Fluid Package Basis 1 view to return to the Simulation Basis Manager view Figure 2 15 Simulation Basis Manager Curent Fluid Packages Flowsheet Fluid Pkg Associations Basis 1 NC 6 PP Peng Robinson Vit FlowSheet Case Main Basis 1 Import Export Default Fluid Pkg Basis 1 v S Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation Environment The list in the Current Fluid Packages group displays the new fluid package Basis 1 showing the number of components NC and property package PP The new fluid package is assigned by default to the main flowsheet as shown in the Flowsheet Fluid Pkg Associations group Creating Hypocom
347. ng on the corresponding Include checkbox Figure 3 98 DataBook Scenario 1 Record Current Scenario Available Scenarios Data Recorder Data Selection Add Object Variable Bel x Scenario 1 Reactor Temp Vv Delete Cooling Duty v Glycol Production y Variables Process Data Tables Strip Charts Data Recorder Chemicals Tutorial 373 Tutorial 3 73 23 Click the Record button to record the variables in their current state EE The New Solved State view appears prompting you for the name of State 1 the new state x 24 In the Name for New State field change the name to Base Case then click OK You return to the Databook 25 In the Available Display group select the Table radio button then click the View button The Data Recorder view appears showing the values of the key variables in their current state Figure 3 99 Xi Data Recorder Main Base Case 140 0 4520e 00E 713 4 a Scenario 1 Delete Table Graph Re Number Now you can make the necessary flowsheet changes and these current values remain as a permanent record in the Data Recorder unless you choose to erase them 26 Click the Minimize icon on the Data Recorder view 27 Click the Restore Up icon E on the Key Variables Data title bar to restore the view to its regular size Next you will change the temperature of stream Reac
348. nt List 1 There are a number of ways to select components for your simulation One method is to use the matching feature Notice that each component is listed in three ways on the Selected tab Matching Method Description SimName The name appearing within the simulation FullName Synonym IUPAC name or similar and synonyms for many components The chemical formula of the component This is useful when you are unsure of the library name of a component but know its formula 2 10 The Component List View view contains two tabs In this example the Selected tab is the only tab used because it contains all the functions you need to add components to the list You can also move to the Match field by pressing ALT M Refining Tutorial At the top of each of these three columns is a corresponding radio button Based on the selected radio button HYSYS will locate the component s that best matches the input you type in the Match cell 2 Optional To rename the component list click in the Name field at the bottom of the view and type a new name For this tutorial example you will add the following non oil components H20 C3 iC4 nC4 iC5 and nC5 First you will add H2O using the match feature 3 Ensure the Sim Name radio button is selected and the Show Synonyms checkbox is checked Click in the Match field 5 Begin typing water HYSYS filters through its library as you type displaying on
349. nt associated with a Eo tmay ne NECASSATY Next you will add a valve to the LiquidProd stream in the Column sub to enter the Column sub flowsheet environment flowsheet 41 Double click the DePropanizer column to open its property view Figure 1 131 1 Column DePropanizer COL1 Fluid Pkg Basis 1 7 PengRobinson Parameters Steady State Profiles Flow Basis Profiles Optional Estimates amp Molar Mass C Volume Pressure Net Vapour Estimates Pressure ws Tray Number Efficiencies Solver 2 3 Phase Clear Tray Clear All Trays Lock Unlock Stream Estimates i Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Converged J Update Outlets Ignored 1 104 Gas Processing Tutorial 16105 Processing Tutorial 1 105 42 Click the Column Environment button to enter the Column Sub flowsheet environment Next you will inset a valve operation between the LiquidProd stream and the Reboiler unit operation 43 In the PFD of the column sub flowsheet break the connection between the LiquidProd stream and the Reboiler unit operation The Object Palette in the 44 Press F4 to open the Object Palette Column Environment contains i ie a fewer available unit operations 45 Install a valve operation between the Reboiler and
350. nthe Ovhd Vap Rate row click the Active checkbox to clear it leaving the Estimate checkbox checked The Degrees of Freedom will increase to 1 indicating that another active specification is required For this example a 2 propane mole fraction in the bottoms liquid will be specified 1 69 1 70 Steady State Simulation 2 Select the Specs page This page lists all the Active and non Active specifications which are required to solve the column Figure 1 87 Column Specifications View snssenressenssenssennenannsssansenseceneseneesenessenssennscnssce Ovhd Yap Rate Reflux Rate Btms Prod Rate E ow Delete Update Specs from Dynamics Default Basis Molar v Degrees of Freedom f 3 In the Column Specifications group click the Add button The Add Specs view appears 4 From the Column Specification Types list select Component Fraction Column Specification Types Column Cold Properties Spec 5 Click the Add Spec s button and the Comp Frac Spec view appears Column Component Ratio Column Component Recovery Column Cut Point Figure 1 88 Column Draw Rate Column DT Heater Cooler Spec Column Dt Spec Column Duty Comp Frac Spec Comp Fraction PG EG Column Duty Ratio Column Feed Ratio Column Gap Cut Point tage lt lt Stage gt gt Column Liquid Flow low Basis Mole Fraction Column Physical Properties Spec h aud gt Column Pump 4round si Liquid Col
351. ntirely known CSTR 100 Q 100 13 Click the Attach Mode icon again to return to Move mode 14 Double click the steam icon 1 to open its property view 15 In the Stream Name cell enter the new name Reactor Vent then close the property view 16 Double click the stream 2 icon Rename this stream Reactor Prods then close the property view 17 Double click the Q 100 icon rename it Coolant then close the view The reactor outlet and energy streams are unknown at this point so they are light blue and purple respectively Chemicals Tutorial 3 51 Completing the Reactor Specifications Double click the CSTR 100 icon to open its property view 2 Click the Design tab then select the Connections page if required The names of the Inlet Outlet and Energy streams that were attached before appear in the appropriate cells 3 Inthe Name cell change the operation name to Reactor Figure 3 64 Reactor Design Name Reactor Connections Parameters Inlets Vapour Outlet User Variables Mixer Out Reactor Vent X Notes Energy Optional Liquid Outlet Coolant Reactor Prods X Fluid Package Basis 1 Design Rating Worksheet Delete ERR M Ignored 4 Select the Parameters page For now the Delta P and the Volume parameters are acceptable at the default values 3 52 Steady State Simulation 5 Select the Cooling radio button This reaction is exothermic
352. o the Fermentor however the recycle is not a concern in this example 1 Before installing the column select Preferences from the HYSYS Tools menu On the Options page of the Simulation tab ensure that the Use Input Experts checkbox is checked then close the view 2 Install the CO2 Wash Tower as a simple Absorber Absorber CO2WASH Tab Page In this cell Emters Top Stage Inlet Wash H2O wno Meeme emsa e Steady State Simulation 3 Click the Run button in the Column property view to calculate the CO2 Wash Tower product streams Concentrator 1 Install the Concentrator as an Absorber with a side vapour draw Absorber CONC Tab Page inthis Enters Pressure Profile 101 325 kPa Temperature Estimates Condenser 90 C Temperature Reboiler Reboiler Temperature 2 Create and define the following specifications to fully specify the column You might have to deactivate the default Rect Feed Rate specification to converge the Specifications E Terrase f mseo Temere Design Specs Comp Recovery Active Draw Rect Feed SpecValue 0 95 Component Ethanol Draw Rate 1 Estimate Draw Rect Feed Flow Basis Mass Spec Value 5000 kg h Draw Rate 2 Estimate Draw To_Light Flow Basis Molar Spec Value 1000 kgmole h 3 Click the Run button in the Column property view to calculate the Concentrator product streams Ethanol Plant on Ee Lights 1 Add the Lights Tower purificatio
353. ocessing Tutorial 69 Processing Tutorial 1 69 17 Select the Monitor page Figure 1 86 Column DePropanizer COL1 Fluid Pkg Basis 1 7 Peng Robinson Design Optional Checks Profile i View Initial Estimates Connections i Monitor Temp C Press Specs C Flows Specs Summary Subcooling Notes Reflus Ratio 1 000 lt empty gt lt empty gt Ovhd Vap Rate 2 000 MMSCFD lt empty gt lt empty gt Reflux Rate lt empty gt lt empty gt lt empty gt Btms Prod Rate O lt empty gt lt empty gt lt empty gt t t t View Add Spec Group Active Update Inactive Degrees of Freedom fo Design Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged J Update Outlets Ignored The Monitor page displays the status of your column as it is being calculated updating information with each iteration You can also change specification values and activate or de activate specifications used by the Column solver directly from this page Adding a Column Specification The current Degrees of Freedom is zero indicating the column is ready to be run The Vapour Rate you specified in the Input Expert however is currently an Active specification and you want to use this only as an initial estimate for the solver for this exercise 1 I
354. ode It is also possible to set your own pressure flow specifications and size the equipment without the aid of the Dynamic Assistant 3 3 1 Simplifying the Steady State Flowsheet The distillation column in the Chemicals Tutorial will be deleted in this section 1 Open the pre built case file TUTOR3 hsc located in your HYSYS Samples directory if you are not continuing from the Steady State Simulation section of this tutorial From the Tools menu select Preferences Click the Variables tab then select the Units page In the Available Unit Sets group select Field Close the Session Preferences view 5 From the File menu select Save As Save the case as DynTUT3 1 hsc 6 Delete all material streams and unit operations downstream of the ANEN oe ete Sean Reactor Prods stream The following 6 items should be deleted unit or logical operation from the flowsheet HYSYS will ask you to confirm the Material Streams Energy Streams Unit Operations deletion To delete the object click the Yes button Ovhd Vap CondDuty Tower If not click the No button RecyProds RebDuty Glycol 7 The steady state simulation case should solve with the deletion of the above items The PFD for the dynamic tutorial should appear as shown below Figure 3 104 Reactor Vent n Mixer Out aaa Reactor Coolant Reactor Prods Water MIxX 100 Before entering dynamics the pressure specification on the Water Feed stream should be remov
355. of freedom Either the outlet stream temperature or the amount of duty in the energy stream can be specified In this case you will specify the outlet temperature 6 Double click the outlet stream icon 1 to open its property view 7 Inthe Stream Name field change the name to Hot Crude 8 Inthe Temperature field specify a temperature of 650 E Figure 2 72 Hot Crude Worksheet Stream Name Hot Crude Vapour Phase Fraction 0 53553 Conditions 650 00 Properties Molar Flow lbmole hr J 321 0 Mass Flow Ib hr 1 0796e 006 K Value Std Ideal Liq Vol Flow barrel day 93718 User Variables Molar Enthalpy Btu Ibmole 1 624e 005 Molar Entropy Btu Ibmole F 343 48 Composition ae Heat Flow Btu hr 5 3950e 08 Cost Parameters Liq Vol Flow Std Cond barrel day 93457 Fluid Package Basis 1 Worksheet Attachments Dynamics Se ee Delete Define from Other Stream 2 62 Refining Tutorial 2 63 The remaining degree of freedom in the Furnace has now been used so HYSYS can flash Hot Crude and determine its remaining properties 9 Close the view to return to the PFD view The Furnace now has green status and all attached streams are known 10 Double click on the energy stream icon Q 100 to open its property view The required heating duty calculated by HYSYS appears in the Heat Flow cell 11 In the Stream Name cell rename this energy stream Crude Duty then close the pr
356. of only a few components Instead of specifying zero fractions or flows for the other components enter the fractions or the actual flows for the non zero components leaving the others lt empty gt Click the Normalize button and HYSYS will force the other component fractions to zero As you input the composition the component fractions or flows initially appear in red indicating the final composition is unknown These values will become blue when the composition has been calculated Three scenarios will result in the stream composition being calculated e Input the fractions of all components including any zero components such that their total is exactly 1 0000 Then click the OK button Input the fractions totalling 1 000 flows or relative number of parts of all non zero components Click the Normalize button then the OK button Input the flows or relative number of parts of all components including any zero components then click the OK button 1 25 1 25 1 26 Steady State Simulation 1 Click on the Mole Fraction cell for CO2 type 0 01 then press ENTER 2 Enter the remaining fractions as shown in the figure below When you have entered the fraction of each component the total at the bottom of the view will equal 1 00000 Ni Input Composition for Stream Feed 1 x Composition Basis Mole Fractions Mass Fractions Lig Yolume Fractions C Mole Flows Mass Flows C Lig Volume Flows
357. of the following e Start typing PENG ROBINSON and HYSYS will find the match to your input Gas Processing Tutorial 1 11 e Use the up and down keys to scroll through the list of available property packages until Peng Robinson is selected e Use the vertical scroll bar to move down the list until Peng Robinson becomes visible then select it Figure 1 9 Property Package Selection Lee Kesler Plocker Property Package Filter All Types l JEGSs Activity Models C Chao Seader Models Vapour Press Models C Miscellaneous Types The Property Pkg indicator at the bottom of the view now indicates that Peng Robinson is the current property package for this Fluid Package Figure 1 10 PropertyPka Peng Robinson Alternatively you could have selected the EOSs radio button in the Property Package Filter group which would produce a list of only those property packages which are Equations of State You could have then selected Peng Robinson from this filtered list as shown in the following figure Figure 1 11 Property Package Selection Kabadi Danner Lee Kesler Plocker MBWR Peng Robinson PRS SRK Zudkevitch Joffee Property Package Filter C All Types C Activity Models Chao Seader Models C Vapour Press Models C Miscellaneous Types Steady State Simulation Selecting Components Now that you have chosen the property package to be used in the simulation the next step is to s
358. ole Frac 12 C3diol T Material Streams P T Flow Compositions Unit Ops FeederBlock Prop Oxide J Include Sub Flowsheets MIx 100 L Show Name Only Number of Hidden Objects 0 3 66 ih Navigator Icon You can control which objects appear by selecting a different Filter radio button For example to list all streams and unit operations select the All button You can start or end the search string with an asterisk which acts as a wildcard character This lets you find multiple objects with one search For example searching for VLV will open the property view for all objects with VLV at the beginning of their name Chemicals Tutorial 3 67 Using the Object Navigator If you want to view the calculated properties of a particular stream or operation you can use the Object Navigator to quickly access the property view for any stream or unit operation at any time during the simulation To open the Navigator do one of the following e Press F3 e From the Flowsheet menu select Find Object e Double click on any blank space on the HYSYS Desktop e Click the Navigator icon The Object Navigator view appears Figure 3 88 Bil ES Object Navigator Unit Operations Filter C All C Streams UnitOps C Logicals C Custom Setup Custom Build Find Cancel Flowsheets Tower COL1 The UnitOps radio button in the Filt
359. oll down the list of Streams and select Kerosene 4 Click the View button and the property view for stream Kerosene appears 5 On the Attachments tab move to the Utilities page of the stream property view 6 Click the Create button The Available Utilities view appears presenting you with a list of HYSYS utilities Figure 2 122 Available Utilities Bile x Cold Properties Critical Property Depressuring Envelope Hydrate Formation Pipe Sizing Property Table User Property Add Utility 7 Find BP Curves and do one of the following e Select BP Curves then click the Add Utility button e Double click on BP Curves 8 HYSYS creates the utility and opens the BP Curves view 9 On the Design tab go to the Connections page Change the name of the utility from the default Boiling Point Curves 1 to Kerosene BP Curves 2 99 Steady State Simulation A Utility is a separate entity 10 Change the curve basis to Liquid Volume by selecting it in the Basis from the stream it is drop down list attached to if you delete it the stream is not affected Likewise if you delete the Figure 2 123 stream the Utility remains but cannot display any Boiling Point Curves Kerosene BP Curves information until you attach another stream using the ___ Design Name Kerosene BP Curves Select Object button Connections Object Type Steam gt Notes Stream Kerosene Select Object Basis Design Perf
360. oller mode to Auto on the face plate then input a set point of 50 Leave the face plate view open 22 Close the Reb LC property view Adding a Flow Controller In this section you will add flow controllers to the product streams of the column These controllers ensure that sufficient material is leaving the column 1 Click the PID Controller icon in the Object Palette then click in the PFD near the Off Gas stream The controller icon appears 2 Double click the controller icon to access the property view Specify the following details Tab Page In this cell Enter i i 3 Click the Control Valve button The FCV for Atmos Cond view appears 4 Inthe Duty Source group ensure that the Direct Q radio button is selected 2 134 Refining Tutorial 5 Inthe Direct Q group enter the following details In this cell Enter Minimum Available 0 kJ h Maximum Available 2 x 108 kJ h Close the FCV for Atmos Cond view Click the Face Plate button The Off Gas FC face plate view appears Change the controller mode to Auto then input a set point of 5 kgmole h 8 Close the Off Gas FC property view but leave the face plate view open 9 Inthe Object Palette click the PID Controller icon then click in the PFD near the Diesel stream The controller icon appears in the PFD 10 Double click the controller icon to access the property view then specify the following details Tab Page In
361. omposition information 1 Close the Workbook view The PFD becomes visible and displays a light blue arrow on it labeled Feed 1 That arrow is the stream Feed 1 that you just created Be 2 Double click the blue arrow The Feed 1 view appears Figure 1 23 Worksheet Feed1 M Vapour Phase Fraction lt empty gt Bees Temperature F 60 000 Properties Pressure psia 600 02 Molar Flow MMSCFD 6 0000 Mass Flow lb hr lt empty gt K Value Std Ideal Liq Vol Flow barrel day lt empty gt User Variables Molar Enthalpy Btu Ibmole lt empty gt Molar Entropy Btu lbmole F lt empty gt Composition Notes Heat Flow Btu hr lt empty gt Cost Parameters Liq Vol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 Worksheet Attachments Dynamics 6 Unknown Compositions i i Define from Other Stream G gt 1 23 Steady State Simulation 3 Click on the Composition page By default the components are listed by Mole Fractions Figure 1 24 Worksheet Conditions Properties Composition K Value al lt empty gt User Variables Notes Cost Parameters Tota 0 00000 Edit Edit Properties Basis z Worksheet Attachments Dynamics Delete Define from Other Stream Click on the Mole Fractions cell for the first component Nitrogen Type 0 01 and press ENTER HYSYS will dis
362. on In the second part of the application the steady state case will be converted into dynamics The general steps that will be used to navigate through this detailed procedure are as follows 1 Converting from Steady State To prepare the case for dynamic simulation valves will be installed to define pressure flow relations and PF specifications will be added to selected streams The tray sizing utility will be implemented for sizing tray sections all other unit operations will be sized 2 Adding Controllers In this step appropriate controllers will be installed and defined manually 3 Preparing the Dynamics Simulation In the last step the Databook will be set up Changes will be made to key variables in the process and the dynamic behaviour of the model will be observed 01 6 1 Converting from Steady State H Changing the PFD Break Connection icon Use the Break Connection A few changes will have to be made to the PFD in order to operate in icon to break the connection Dynamic mode between streams and unit operations 1 Delete the Set 1 unit operation i 2 Set the pressure of the DEA TO RECY stream to 995 psia i 3 Install a Recycle operation between the REGEN BTTMS stream and the E 100 exchanger Attach Mode icon Use the Attach Mode icon to reconnect them The Recycle operation only functions in Steady State mode Its sole purpose in this case is to provide a suitable solution before entering
363. on for the new Separator V 100 to open its are now known as shown by the change in their PFD colour propeny vi from light blue to dark blue 15 In the Name field change the name to LTS 16 Click the Close icon to close this view At this point the outlet streams from heat exchanger Gas Gas are still unknown 17 Double click on the Gas Gas icon to open the exchanger property view 18 Click the Design tab then select the Specs page Figure 1 71 m Gas Gas Solver Unknown Variables R 1 000e 04 Ooo dl lt empty gt Temperature of CoolGas Parameters 25 Temperature of SalesGas lt empty gt Specs Iterations Di nknown Variables 2 ae 1 Notes Degrees of Freedom 1 Specifications Sd Specified Value _ Curent Value Relative Error Active Estim ____ lt empty gt 1 0 lt empty gt lt empty gt lt empty gt es Delete Rating Worksheet Performance Dynamics HTFS TASC Dee O Udesi o pdas I Ignored 1 58 Gas Processing Tutorial 159 Processing Tutorial 1 59 The Specs page allows you to input specifications for the Heat Exchanger and view its calculation status The Solver group on this page shows that there are two Unknown Variables and the Number of Constraints is 1 so the remaining Degrees of Freedom is 1 HYSYS provides two default constraints in the Specifications group although only one has a val
364. on tab Errors group you can direct these errors to the trace window and have the simulation continue regardless After a few minutes the integrator will stop and an error message will appear in the trace window 1 From the Simulation menu select Equation Summary View 2 Click the Uncoverged tab and click the Update Sorted List button The top equation refers to pump P 102 If you examine this pump in the PFD you will see that it is fully on but its downstream valve has been completely shut by a controller As an advanced exercise you can refine the control scheme to address this issue G1 33 References Gl 7 References Gerunda Arthur How to Size Liquid Vapour Separators Chemical Engineering Vol 88 No 9 McGraw Hill New York 1981 G1 34 Atmospheric Crude Tower R1 1 Al Atmospheric Crude Tower R1 1 Process Description inasi aaa aa ea 3 R12 SQUID iaa a lel bated A 6 R1 2 1 Components amp Fluid Package ccceceeseeeeeeeeeeeeeeeeaees 6 R1 2 2 Oil CharacteriZation ccccccccsseececseseeceeeeeeseeeeeseeeeeeaeeeeens 6 R1 3 Steady State Simulation 0ct1 Meeeeb sssscsnsssesccnnsssseesessesees 10 R1 3 1 Simulate the Pre Fractionation Train cccccccseeeeeeeeees 10 R1 3 2 Install Atmospheric Crude Fractionator cccee 12 ar ATC T o M Mie cennssecnnesscnnssscensessennesss 18 R1 1 a Atmospheric Atmospheric Atmospheric Crude Tower R1 3 Al
365. onnections page on the Design tab is active Figure 1 50 E 100 Name E o0 Shell Side Inlet Design _ Tube Side Inlet Connections Parameters SE Tube Side Shell Side User Variables Tubeside Flowsheet Shellside Flowsheet Notes Case Main Case Main Sa Tube Side Outlet Shell Side Outlet Specs Tube Side Fluid Pkg Shell Side Fluid Pkg Basis 1 Basis 1 Rating Worksheet Performance Dynamics HTFS TASC Delte eT Losie Ignored 3 Inthe Name field change the operation name from its default E 100 to Gas Gas Gas Processing Tutorial 4 Attach the inlet and Outlet streams as shown below using the You will have to create all streams except SepVap methods learned in the previous sections which is an existing stream that can be selected from the Tube Side Inlet drop down Tigure 1 91 list m Gas Gas Create the new streams by selecting the appropriate Design Tube Side Inlet Name Gas Gas Shell Side Inlet input field typing the name TERNER Sevap tst i is LTSVap then pressing ENTER Parameters Specs Tube Side Shell Side Tubeside Flowsheet Shellside Flowsheet Notes Case Main Case Main User Variables Tube Side Outlet Shell Side Outlet CoolGias x SalesGas Tube Side Fluid Pkg Shell Side Fluid Pkg Basis 1 Basis 1 io Design Rating Worksheet Performance Dynamics HTFS TASC Delete SUnknownDetaP SS SCw date S gr 5 Cli
366. ontrol button and the Data Control view appears as shown below Figure 2 112 Data Control x Style Basis C Multi Tray Molar Single Tray C Mass C Liquid Yol Properties i Phase Mee Vapour ASTM D86 M Light Liquid D86 Crack Reduce Heavy Liquid M D1160 Vac F D1160 ATM D28857 Visible Points 15 Points C 31 Points You can view boiling point 5 Select the Multi Tray radio button in the Style group The Data properties pi a Sing e tray of Control view is modified showing a matrix of column stages with a multiple trays The boiling point properties of all stages checkbox for each stage KOPAE pronus ara 6 Activate the following stages by clicking on their blank checkboxes drawn are important for this Tutorial e Condenser Naphtha product stage e 29 Main TS Residue e KeroSS_Reb Kerosene e 3 DieselSS Diesel e 3 AGOSS AGO The TBP profile for the light liquid phase on each stage can be viewed on a liquid volume basis 7 Select TBP in the drop down list under the tray matrix in the Style group In the Basis group select the Liquid Vol radio button Activate the Light Liquid checkbox in the phase group to activate it 10 Leave the Visible Points at its default setting of 15 Points You can display more data points for the curves by selecting the 31 Points radio button 2 92 Steady State Simulation The independent x axis variable is the Assay Volume Percent wh
367. ook Available Data Entries Object Variable Reactor Temp Cooling Duty Glycol Production a Variables Process Data Tables Strip Charts Data Recorder Case Studies Now that the key variables have been added to the Databook the next task is to create a data table in which to display these variables 14 Click the Process Data Tables tab 3 70 Chemicals Tutorial 3 71 The three variables that you 15 In the Available Process Data Tables group click the Add button added to the Databook HYSYS creates a new table with the default name ProcDatal appear in the table on this tab Figure 3 94 DataBook OF x Available Process Data Tables gt Individual Process Data Selection ProcDatal View Process Data Table ProcD atal i Reactor Temp Delete L _ Cooling Duty Glycol Production Setup Add All Variables Invert All Yariables Remove All Variables Variables Process Data Tables Strip Charts Data Recorder Case Studies 16 In the Process Data Table field change the name to Key Variables 17 In the Show column activate each variable by clicking on the corresponding checkbox Figure 3 95 Individual Process Data Selectio Process Data Table key Variables ov 18 Click the View button to view the new data table Figure 3 96 Key Variables Data Object Variable Value Units Reactor Temp 140 0 F Coolant Cool
368. ook Case Main Name Feed 1 Vapour Fraction 0 8952 Feed 2 MixerOut SepVap SepLig 3 LTSVap O x 0 9013 0 8976 1 0000 0 0000 1 0000 0 9424 CoolGas a i Temperature F 60 00 60 00 60 00 60 00 60 00 4 444 43 94 Pressure psia 600 0 600 0 600 0 600 0 600 0 580 0 t 590 0 Molar Flow MMSCFD 6 000 4 000 10 00 8 976 1 024 7 172 8 976 Mass Flow lb hr 1 675e 004 1 100e 004 2 775e 004 2 318e 004 4564 1 613e 004 318e 004 Liquid Volume Flow barrel day 3012 1983 4995 4342 652 9 3253 4342 Heat Flow Btu hr Name 2 553e 007 SalesGas 1 628e 007 ColdGas 4 180e 007 LTSLig 3 605e 007 SalesDP 5 756e 006 Tower Feed 2 791e 007 Ovhd 3 649e 007 LiquidProd Vapour Fraction 1 0000 0 7990 0 0000 1 0000 0 0168 1 0000 0 0000 Temperature F 50 00 4 444 mde 4 444 9 999 24 73 50 98 190 7 Pressure psia 570 0 590 0 590 0 800 0 590 0 200 0 205 0 Molar Flow MMSCFD 7 172 8 976 1 805 7 172 2 828 2 212 0 6160 Mass Flow lb hr 1 613e 004 2 318e 004 7054 1 613e 004 1 162e 004 7705 Bole Liquid Volume Flow barrel day 3
369. ooler operations 7 Save the case as DynTUT2 3 hsc 2 5 5 Adding Controller Operations Controller operations can be added before or after the transition to dynamic mode Key control loops are identified and controlled using PID Controller logical operations Although these controllers are not required to run the design in dynamic mode they increase the realism of the model and provide more stability 2 130 PID Controller icon For more information regarding PID Controller see Section 12 4 4 PID Controller of the Operations Guide Refining Tutorial Adding a Level Controller In this section you will add level controllers to the simulation flowsheet to control the levels of the condenser and reboiler First you will install the Condenser controller l Zi 3 If the Object Palette is not visible press F4 In the Object Palette click the PID Controller icon In the PFD click near the Condenser operation The controller icon named IC 100 appears in the PFD Double click the IC 100 icon to open the controller property view On the Connections tab click in the Name field and change the name of the Controller to Cond LC In the Process Variable Source group click the Select PV button then select the information as shown in the figure below Click the OK button when you are done Figure 2 167 Select Input P For Cond LC Flowsheet Variable Variable Speci Case Main 4GO_SS Boot height
370. operty view Figure 2 73 Energy Stream Crude Duty Properties Heat Flow Btu hr 1 8626e 08 Ref Temperature F lt empty gt Installing the Mixer In this section you will install a Mixer operation The Mixer is used to combine the hot crude stream with the vapours bypassing the furnace The resulting stream is the feed for the crude column 1 Make some empty space available to the right of the Furnace using the horizontal scroll bar Move other objects if necessary 2 Click the Mixer icon on the Object Palette Position the cursor over the PFD to the right of the Hot Crude stream sees icon Mixer icon 4 Click to drop the mixer onto the PFD HYSYS creates a new mixer with the default name MIX 100 5 Press and hold the CTRL key to temporarily enable the Attach mode while you make the mixer connections you will not release it until step 13 6 Position the cursor over the right end of the PreFlashVap stream icon The connection point and pop up Out appears 2 63 2 64 Steady State Simulation Multiple connection points 7 With the pop up visible click and hold the mouse button then drag appear because the Mixer the cursor toward the left inlet side of the mixer Multiple accepts multiple feed h in EE connection points appear at the mixer inlet 8 Place the cursor near the inlet area of the mixer and when the white box appears at the cursor tip release the mouse button to
371. or at the bottom of a property view for a stream or operation indicates the current state of the object Indicator Status Description Red Status A major piece of defining information is missing from the object For example a feed or product stream is not attached to a Separator The status indicator is red and an appropriate warning message is displayed These are the HYSYS default colours you may change the colours in the Session Preferences Yellow Status All major defining information is present but the stream or operation has not been solved because one or more degrees of freedom is present For example a Cooler whose outlet stream temperature is unknown The status indicator is yellow and an appropriate warning message is displayed The stream or operation is completely defined and solved The status indicator is green and an OK message is displayed When you are in the PFD the streams and operations are colour coded to indicate their calculation status If the conditions of an attached stream for an operation were not entirely known the operation would have a yellow outline indicating its current status For the Mixer all streams are defined so it has no yellow outline 3 47 Steady State Simulation Notice that the icons for all streams installed to this point are dark blue B CSTR Icon X Cancel Icon 3 48 Another colour scheme is used to indicate the status of streams For mate
372. or this example is MMSCFD Gas Processing Tutorial 1 9 6 To view the available units for Flow click the drop down arrow in the Flow cell Figure 1 6 Session Preferences HYSYS PRF e x Available Unit Sets 3 EuroS a Cl Units Field one Formats Field13 E ete NewlUser Unit Set Name Newser SC S lew Users Display Units E 3 t ey View Unitless F Add psia Yariables Delete Mass Flow y Simulation Wariables Reports Resources Extensions Oillnput Tray Sizing Save Preference Set Load Preference Set 7 Scroll through the list using either the scroll bar or the arrow keys select MMSCED then press ENTER Figure 1 7 Ol x Session Preferences HYSYS PRF Available Unit Sets Variables 3 wer EuroS a Cl Units Field one Formats Field13 E aie Newser Unit Set Name New Ser Display Units Vapour Fraction Mass Flow o Simulation Wariables Reports Resources Extensions Oillnput Tray Sizing Save Preference Set Load Preference Set Your new unit set is now defined x 8 Click the Close icon in the top right corner to close the Session Close icon Preferences view You will now start building the simulation 1 9 1 10 HYSYS has created a Fluid Package with the default name Basis 1 You can change the name of this fluid package by typing a new name in
373. ork through these pages the first time you build a crude column in HYSYS Once you are comfortable working with side equipment try using the template Instructions on using the crude column template are given in an annotation on the next page 2 66 Adding an Energy Stream In this section you will add an energy stream Prior to installing the column an energy stream must be created to represent the trim duty on stage 28 of the main tower 1 Double click on the Energy Stream icon on the Object Palette HYSYS creates a new energy stream with the default name Q 100 and display its property view In the Stream Name field change the name to Trim Duty Close the view 4 Save your case by doing one of the following e press CTRL S e from the File menu select Save e click the Save icon Installing the Column HYSYS has a number of pre built column templates that you can install and customize by changing attached stream names number of stages and default specifications and adding side equipment One of these templates is going to be used for this example a crude column with three side strippers however a basic Refluxed Absorber column with a total condenser is installed and customized in order to illustrate the installation of the necessary side equipment 1 Before installing the column select Preferences from the HYSYS Tools menu Click the Simulation tab 2 On the Options page ensure the Use Input Experts
374. ormance Dynamics Delete Ignored 11 You can scroll through the matrix of data to see that the TBP ranges from 267 F to 498 F by going to the Performance tab and selecting Results page Figure 2 124 Boiling Point Curves Kerosene BP Curves Performance Results ASTM D86 D86 Crack Reduced AST a F Z F _ Critical Props Cold Props Plots Design Performance Dynamics Delete 2 100 Refining Tutorial This boiling range predicted by the utility is slightly wider than the ideal range calculated during the Oil characterization procedure for Kerosene 356 F to 464 E Figure 2 125 Cut Distributions see ETE 158 0 0 033 Naphtha 356 0 0 172 Kerosene 4640 0 129 Light Diesel 554 0 e089 Ideal boiling Heavy Diesel 644 0 0 083 gt range calculated Atm Gas Oil 698 0 0 049 Rea 14 044 eunng a Characterization 12 Select the Plots page on the Parameters tab of the utility property view to view the data in graphical format Figure 2 126 Boiling Point Curves Kerosene BP Curves Performance Dependent Variable BP Curves X Results Critical Props Cold Props Plots Temperature F Volume Percent Design Performance Ignored To make the envelope more 13 When you move to the Plots view the graph legend can overlap the readable maximize or plotted data To
375. orting the stream composition into the Spreadsheet then multiplying the mole fraction of each component by its individual heating value Gas Processing Tutorial 89 Processing Tutorial 1 89 Importing Variables First Method In this section you will import variables on the Connections tab 1 Click the Add Import button and the Select Import view appears NO2 and CO2 are not 2 Choose the SalesGas Object Comp Mole Frac Variable and Methane included in the calculation i Pa as their individual heating Variable Specific as shown values are negligible Figure 1 116 Select Import for cell Flowsheet Variable Variable Specifics Case Main LTSVap ActualGas Flow a DePropanizer COL1 MixerOut Actual Liquid Flow Ovhd Actual Volume Flow i RebDuty Average Liquid Der pObject Filter SalesDP Comp K Value He All SalesGas Comp K Value Lig i SepLig Comp K Value Mir s SLES Sep ap Comp Mass Flow C Unit ps Navigator Scope TowerFeed Comp Mass Frac Logicals regi sien ee DewPaint Comp Molar Flow C ColumnOps Chiller Comp Mole Frac Qos A ean DePropanizer Comp Volume Flow asis Gas Gas Comp Volume Frac Custom Utility InletSep Correlation Value Csom iii IETS Cp Cv MI gt lt 100 Dynamic P F Spec halse 1 11 i xl Variable Description Comp Mole Frac Methane Cancel 3 Click the OK button Click the Add Import button again then select the SalesGas Object Comp Mole Frac Variable and Ethane Variable
376. ou can make changes to key variables in the process then observe the changes in the dynamic behaviour of the model Next you will monitor important variables in dynamics using strip charts 3 91 3 92 Dynamic Simulation 3 3 9 Monitoring in Dynamics Now that the model is ready to run in dynamic mode you will create a strip chart to monitor the general trends of key variables Add all of the variables that you would like to manipulate or model Include feed and energy streams that you want to modify in the dynamic simulation 1 Open the Databook by using the hot key combination CTRL D The following is a general procedure to install strip charts in HYSYS Figure 3 119 DataBook Available Data Entries Object Variable Edit Reactor Prods Reactor Temp Insert Delete o Variables Process Data Tables Strip Charts Data Recorder Case Studies 2 On the Variables tab click on the Insert button The Variable Navigator appears Figure 3 120 Yariable Navigator Flowsheet Variable Case Main Coolant Dynamic P F Spec a Mixer Out Heat Flow Prop Oxide Heat Of Yapourizat Prop Oxide 1 Heavy Liquid Fetal Object Filter Reactor Prods Higher Heating Vali All Reactor Prods 1 Kinematic Viscosity Reactor Vent Light Liquid Fractioi 2 Streams Water Feed Liq Mass Density UnitOps Navigator Scope _ Water Feed 1 Lig Yol Flow Std C Logicals z PropOxide FC Liquid Fraction C Colum
377. our Fraction 1 0000 0 7818 0 0000 1 0000 0 0187 1 0000 0 0000 Temperature F ooo 0 0000 oo 529 20 84 48 74 190 6 Pressure psia 580 0 580 0 580 0 800 0 580 0 200 0 205 0 Molar Flow MMSCFD 7 018 8 976 1 959 7 018 2 982 2 350 0 6320 Mass Flow Ib hr 1 562e 004 2 318e 004 7561 1 562e 004 1 212e 004 8110 4014 Liquid Volume Flow barrel day 3167 4342 1175 3167 1828 1348 480 4 Heat Flow Btu hr 2 725e 007 3 769e 007 1 043e 007 2 744e 007 1 619e 007 1 034e 007 4 185e 006 lt Material Streams P T Flow Compositions Energy Streams Unit Ops PaSeser REEN J Include Sub Flowsheets we oo C Show Name Only Number of Hidden Objects 3 Click the Compositions tab Figure 1 97 Workbook Case Main OF x Feed 2 MixerOut SepLiq SalesGas omp Mole Frac Nitrogen 0 0100 0 0179 0 0132 0 0017 0 0179 p omp Mole Frac C02 0 0100 0 0000 0 0060 0 0034 0 0066 omp Mole Frac Methane 0 6000 0 6244 0 6098 aji 0 1905 0 7664 omp Mole Frac Ethane 0 2000 0 1666 0 1866 0 2044 0 1565 omp Mole Frac Propane 0 1000 0 1136 0 1054 0 2612 0 0414 omp Mole Frac i Butane 0 0400 0 0431 0 0412 0 1640 0 0070 omp Mole Frac n Butane 0 0400 0 0345 0 0378 0 1748 0 0043 LTS ap ColdGas LTSLig TowerFeed LiquidProd omp Mole Frac Nitrogen 0 0179 0 0145 0 0021 0 0020 0 0000
378. pear below Name i Vapour Fraction pam m7 l Temperature F Bzz z Pressure psia 65 00 Molar Flow lbmole hr baer Mass Flow lb hr 1 282e 006 Liquid Volume Flow barel day 1 000e 005 77 46de 008 Heat Flow Btu hr R1 11 Steady State Simulation An energy stream can be installed by selecting the appropriate icon from the palette or a material stream converted to an energy stream on the Util page of the stream property view These streams could be installed inside the Column Build Environment as well By taking this approach you will need to attach these streams to the Column Flowsheet so that they can be used in the calculations R1 12 The Pre Fractionation train is shown as follows Figure R1 8 PreFlash Yap PreFlash Crude Heater Atm Feed PreFlash Liq Hot Crude Mixer l Crude Duty gt Raw Crude Al 3 2 Install Atmospheric Crude Fractionator Steam and Irim Duty Streams Before simulating the atmospheric crude tower the steam feeds and the energy stream Q Trim representing the side exchanger on stage 28 to the column must be defined The Q Trim stream does not require any specifications this will be calculated by the Column Three steam streams are fed to various locations in the tower Specify the steam streams as shown below Define the composition for each as H O 1 0000 Stream Name
379. pears 2 Selecta fluid package from the list then click the Add Set to Fluid Package button Repeat the procedure for the other two reaction sets Click the Enter Simulation Environment button Synthesis Gas Production 2 3 Steady State Simulation Installing Streams Here you will define the two feed streams to the first reactor Natural Gas and Reformer Steam The Comb Steam stream and the Air stream will also be defined The pressures of the steam and air streams will be specified later using SET operations Install and define the streams as indicated Name Natural Gas Reformer Steam Air Comb Steam Temperature 7000 4750 Jeo aso COMMENTS signifies initialized values the molar flows of Air and Comb Steam will be manipulated by Adjust 2 and Adjust 1 respectively C2 9 Steady State Simulation Le 3 1 Building the Flowsheet Set Operations Install the following Set operations to specify the pressures of the steam and air streams Install these before installing the Reformer so the An alternative method for a reactor is calculated when you install it setting the steam and air pressures is to import the Natural Gas pressure to a Set SET 1 Spreadsheet copy the value and export the copied values Connections Target Object Reformer Steam to the streams Target Variable Source Object Natural Gas Parameters Multiplier Offset Set SET 2 Tab inthis cell Enter Connec
380. pecify the vessel volume Rating tab Sizing page Tank VATE ST Mises Temer Worksheet Conditions LigVol Flow DEA TO VALVE 194 4 USGPM Design Parameters Liquid Level Heat Exchanger Sizing The Shell and Tube heat exchanger E 100 will be sized with a 10 minute residence time for both the shell and the tube side enter respective sizes on the Rating tab Parameters page Heat Exchanger E 100 Tube Side Sizing Worksheet Conditions Std Ideal Lig Vol Flow 498 27 USGPM RICH TO L R G1 25 G1 26 Dynamic Simulation Heat Exchanger E 100 Shell Side Sizing Worksheet Conditions Std Ideal Liq Vol Flow 691 3 USGPM REGEN BTTMS TO L R A 10 minute liquid residence time will also be used for sizing the cooler E 101 Dynamics tab Specs page Cooler E 101 Tab Page Worksheet Conditions Std Ideal Liq Vol Flow 194 4 USGPM DEA TO COOL Dynamics Specs 259 8 ft Running the Integrator 1 Switch to the Dynamic mode by clicking the Dynamic Mode button Click No when asked if you want the Dynamics Assistant to help you resolve items in Steady State before switching to Dynamic mode Open the Product Block for stream Nitrogen Flow Ensure that the radio button for temperature is selected and the value is specified as 70 F 4 Click the Composition tab and set the composition to 100 Nitrogen 5 Return to the Conditions tab and press the Export to Stream button 6 Open the In
381. pentanols that have a potential value superior to that of ethanol Accumulation of fusel oils in the Rectification Tower can cause the formation of a second liquid phase and subsequent deterioration of performance for these trays so small side liquid draws of fusel oils are installed on the rectifier to avoid this problem The Ethanol rich product stream from the fermentor is sent to a concentration Conc tower An absorber with a side vapour draw can be used to represent this tower The top vapour is fed to a light purification tower Lights where most of the remaining CO2 and some light alcohols are vented The bottom product of this light tower is fed to the Rectifier To_Light P Light_Vent o Condenser p p CondDuty mp 2ndEtOH acho Condenser Rect_Feed p T Tashi o_Lig liA To Rect The side vapour draw from the Concentrator is the main feed for the Rectifier The Rectifier is operated as a conventional distillation tower The product of this tower is taken from Stage 2 so to have an azeotropic ethanol product with a lesser methanol contamination Methanol concentrates towards the top stages so a small distillate draw is provided at the condenser Also a small vent for CO is provided at the condenser Ethanol Plant CB Plant C1 5 gt Rect_Vap To Condenser Rect_Cond Rect_Dist RefluxCondenser gt istProd To_Rect Fusel Rect_Feed Rect_Reba Re
382. play the Input Composition for Stream view where you will complete the compositional input Figure 1 25 Ni Input Composition for Stream Feed 1 Composition Basis Mole Fractions C Mass Fractions C Lig Volume Fractions C Mole Flows C Mass Flows C Lig Volume Flows Composition Controls Erase Normalize Cancel 1 24 Gas Processing Tutorial This view allows you to access certain features designed to streamline the specification of a stream composition The following table lists and describes the features available on this view Composition Input Composition Basis Radio Buttons Normalizing Calculation status These are the default colour colours yours may appear different depending on your settings on the Colours page of the Session Preferences view Feature Description Allows you to input the stream composition in some fractional basis other than Mole Fraction or by component flows by selecting the appropriate radio button before providing your input The Normalizing feature allows you to enter the relative ratios of components for example 2 parts N2 2 parts CO2 120 parts C1 etc Rather than manually converting these ratios to fractions summing to one enter the individual numbers of parts and click the Normalize button HYSYS will compute the individual fractions to total 1 0 Normalizing is also useful when you have a stream consisting
383. plays the specific dimensions of the valve type trays 9 Keep the default values click the Complete AutoSection button Figure 1 138 Ni Tray Section Information Internals C Sieve Valve C Bubble Packed Valve Tray Straight Glitsch alve Mat l Density 513 2 Ib ft3 Valve Mat l Thickness 0 060 in Hole Area of AA 15 30 Common Tray Properties 24 00 in 0 1250 in 1 000 6 000 in 85 00 DC Wetr Info TAO USGPM A Vertical 1 500 in 50 00 Delete Complete AutoSection 1 109 Dynamic Simulation HYSYS calculates the Main TS tray sizing parameters based on the steady state flow conditions of the column and the desired tray types HYSYS labels the DePropanizer tray section as Section_1 10 To confirm the dimensions and configuration of the trays for Section_1 click the Performance tab then select the Results page Confirm the following tray section parameters for Section_1 which will be used for the Main TS tray sections Figure 1 139 o x Section Results hiatal Trayed C Packed Export Pressures View Warnings Results feed Tray Results Section_1 Table Internals Valve Plot Section Diameter ft 2 500 Max Flooding 80 61 Sectional Area ft2 4 909 20 00 oma Number of Flow Paths 1 Flow Lenath in 16 00 Flow Width in 28 51 Max DC Backup 37 42 Max Weir Load USGPM
384. ponents Your next task is to create and add the hypocomponents to the component list In this example you will characterize the oil Petroleum Fluid using the given Assay data to create the hypocomponents 2 16 Refining Tutorial Characterizing the Oil In this section you will use the following laboratory Assay data Bulk Crude Properties API Gravity 48 75 Light Ends Liquid Volume Percent n Pentane TBP Distillation Assay Percent Distilled K 8 C A E 2 API Gravity Assay 2 17 Steady State Simulation The Associated Fluid Package drop down list indicates which fluid package is used for the oil characterization Since there is only one fluid package HYSYS has made Basis 1 the Associated Fluid Package 2 18 Viscosity Assay Percent Distilled ps09 60000 98280 Accessing the Oil Environment The HYSYS Oil Characterization procedure is used to convert the laboratory data into petroleum hypocomponents 1 On the Simulation Basis Manager view click the Oil Manager tab Figure 2 16 Simulation Basis Manager Associated Fluid Package Basis 1 M Associated Flow Sheets Associate FlowSheet Fluid Pkg In Use Case Main TES To Enter the Oil environment There must be a Fluid Package and the associated Property Package must be able to handle Hypo Components a Components Fluid Pkgs Hypotheticals Oil Manager Reactions Component Maps UserProperty Enter Simulation
385. ponents list click in the first cell labeled lt lt Component gt gt then select H2O from the drop down list of available components Figure 3 80 Ni Comp Frac Spec H20 Fraction PSG Ea H20 Fraction tage Reboiler low Basis Mole Fraction hase Liquid Components H20 Target Type C Stream Stage Parameters Summary Spec Type Delete 10 Close this view to return to the Column property view The new specification appears in the Column Specifications list on the Specs page 11 Return to the Monitor page where the new specification appears at the bottom of the Specifications list If you want to view the 12 Click the Group Active button to bring the new specification to the entire Specifications top of the list directly under the other Active specifications table re size the view by clicking and dragging its bottom Figure 3 81 border Column Tower COL1 Fluid Pkg Basis 1 UNIQUAC Ideal Design Optional Checks Profile 3 Input Summary View Initial Estimates Connections Monitor Temp g C Press pecs C Flows Specs Summary Subcooling Notes Specifications Specified Value Current Value Wt Error Active Estimate Current Ovhd Yap Rate 0 0000 Ibmole hr 7 94e 013 0 0000 Vv Iv v Reflux Ratio 1 000 lt empty gt lt empty gt v v v H20 Fraction 5 000e 003 lt empty gt lt empty gt Iv
386. pulated and monitored objects is to see how the monitored objects will respond to the changes you make to the manipulated variable To make the strip chart easier to read do not activate more than six variables per strip chart To change the configuration of each strip chart click the Setup button 1 128 3 Variables to Manipulate 1 128 Dynamic Simulation Select the Flowsheet Object and Variable groups for any of the following suggested variables Variables to Monitor Tower Feed Molar Flow Ovhd Molar Flow Heater Q Utility Outlet Temperature LiquidProd Molar Flow Feed 1 Molar Flow InletSep Liquid Percent Level Feed 2 Molar Flow LTS Liquid Percent Level Click the Add button to add the selected variable to the Variables page Repeat steps 3 and 4 to add any remaining variables to the Databook Click the Strip Charts tab In the Available Strip Charts group click the Add button HYSYS will create a new strip chart with the default name DataLogger1 You may change the default name by editing the Logger Name cell In the table check the Active checkbox for each of the variables that you would like to monitor on this particular strip chart Figure 1 157 10 11 LZ 13 DataBook Biel x Individual Strip Chart Data Selection View 7 000 00 20 00 Stip Chart Logger Name DataLoggerl Sample Int Historical Feed 1 Molar Flow Feed 2 Molar Flow Current
387. quid residence time 1 Double click the Condenser icon on the PFD to open its property view 2 Click the Worksheet tab then select the Conditions page Figure 2 162 Condenser Worksheet Conditions Properties Composition PF Specs Temperature C Pressure kPa Molar Flow kgmole h Mass Flow kg h Std Ideal Lig Yol Flow m3 h 1 953e 005 264 8 0 0000 1 115e 005 152 4 Molar Enthalpy kJ kgmole Molar Entropy kJ kgmole C Heat Flow kh 241 5 3 905e 008 1 592e 005 4197e 005 136 3 Waste Water 1 942e 005 121 8 2 439e 008 Atmos Cond 0 0000 41 47 0 0000 41 47 lt empty gt lt empty gt lt empty gt Molar Flow kgmole h Mass Flow kg h Std Ideal Lig Yol Flow m3 h 106 7 lt empty gt lt empty gt lt empty gt Molar Enthalpy kJ kgmole 1 942e 005 2 841 005 lt empty gt Molar Entropy kJ kgmole C Heat Flow kJ h 121 8 1 708e 008 57 88 3 029e 007 lt empty gt 1 146e 008 2 127 Dynamic Simulation 3 On the Conditions page confirm the following Liquid Volumetric Flow Std Ideal Liq Vol Flow of the following streams Liquid Volumetric Flow Rate m3 h ATIC 152 4 Waste Water 5 736 4 Calculate the vessel volume as follows assuming a 50 liquid level residence volume and a 10 min
388. quire flow specifications since both the Pressure Flow and the Delta P specifications are not set for the pump around coolers e PA 1 Draw e PA 2 Draw e PA 3 Draw The following streams have their flow specifications defined by PID Controller operations e Reflux e Kero SS Draw e Diesel SS Draw e AGO SS Draw 2 137 2438 Dynamic Simulation Dynamic Simulation t Enter Parent Simulation Environment icon y Enter the Main Flowsheet environment Close the column property view if it is still open Switch to dynamic mode by clicking the Dynamic Mode icon When asked if you want to allow dynamics assistant to identify items which are needed to be addressed before proceeding into dynamics click the No button Every material stream in the Main Flowsheet requires either a pressure Dynamic Mode icon or flow specification 3 Double click the Diesel Steam icon to enter its property view 4 Click the Dynamics tab then select the Specs page 5 Inthe Pressure Specification group clear the Active checkbox 6 Inthe Flow Specification group select the Molar radio button then activate the Active checkbox 7 Inthe Molar Flow cell enter 75 54 kgmole h if required Figure 2 172 Diesel Steam Dynamic Specifications Dynamics Pressure Specification Pressure Active Stripchart 344 7 kPa Specs Flow Specification Molar Mass IdealLigyol Std Lig ol Molar Flow Activ
389. quired H N ratio in the synthesis end product The oxygen in the air is consumed in the combustion of methane Any remaining methane in the Combustor is eliminated by this reaction C2 11 Steady State Simulation Reactions of equal ranking can have an overall specified conversion between 0 and 100 C2 12 HYSYS automatically ranks the three reactions in the Combustor Rxn Set Since HO is a reactant in the combustion reaction Rxn 1 and is a product in the two reforming reactions Rxn 2 and Rxn 3 HYSYS provides a lower rank for the combustion reaction An equal rank is given to the reforming reactions With this ranking the combustion reaction proceeds until its specified conversion is met or a limiting reactant is depleted The reforming reactions then proceed based on the remaining methane Install the Combustor and define it as indicated below Conversion Reactor Combustor Tab Page In this cell Enterse Design Inlets Connections Reactions Details Reaction Set Combustor Rxn Set em anift Reactors The three shift reactors are all equilibrium reactors within which the water gas shift reaction occurs In the Combustor Shift reactor the equilibrium shift reaction takes place and would occur with the reactions in the Combustor A separate reactor must be used in the model because equilibrium and conversion reactions cannot be combined within a reaction set Synthesis Gas Production Install th
390. r ower MIx 101 vie Heater PFD of the Column sub flowsheet after controllers are added Figure 1 150 To Condenser CondDuty T Condenser TowerFeed Stageg TC Main TS Reboiler To LiquidExit lt Li idp d Reboiler iquidExi Reboil iquidPro Valve 1 119 Dynamic Simulation Level Control In this section you will add level controllers to both the Main flowsheet and Column sub flowsheet to control the liquid levels of each vessel operation 1 Inthe Main flowsheet ensure the Object Palette is open if it isn t press F4 2 Inthe Object Palette click the Control Ops icon A sub palette appears 3 Inthe sub palette right click and drag the PID Controller icon to Control Ops icon the PFD between InletSep and Sep Valve The controller icon IC 100 appears in the PFD Double click the controller icon to open its property view Q PID Controller icon Figure 1 151 1C 100 Name fic 1 00 Process Yariable Source Object Variable Optional p Output Target Object Select OP Remote Setpoint Source Connections Parameters Monitor Stripchart User Variables Delete Face Plate 5 Click the Connections tab In the Name field change the name of the PID Controller operation to Sep LC 6 Inthe Process Variable Source group click the Select PV button The Select Input PV view appears 1 120 Gas Processing Tutorial 1 121 7 Inthe Obje
391. r to Section 11 7 3 Strip Charts in the User Guide Refining Tutorial Click the OK button The variable now appears in the Databook Add the following variables to the Databook If you select the top variable in the list of Available Data Entries before inserting a new variable the new variable will always be added to the top of the list Object Ela tle Kero SS Reb Liquid Percent Level Vessel Temperature The next task is to create a Strip Chart to monitor the dynamics behaviour of the selected variables 9 Click the Strip Charts tab in the Databook view 10 Click the Add button HYSYS creates a new Strip Chart with the default name DataLoggerl1 11 Click in the blank Active checkbox beside the Condenser Liquid Percent Level variable 12 Repeat step 11 to activate the other variables as shown below Figure 2 177 ioi x Available Strip Charts Individual Strip Chart Data Selection View DataLogger1 Logger Name DataLoagert Sample Int o00 00 20 00 Strip Chart pin j Object Variable Active Historical Condenser Vessel Temperature c Off Gas Main Molar Flow urent Kero_SS_Reb Liq Percent Level Condenser Liquid Percent Level Add Delete Setup aay Variables Process Data Tables Strip Charts Data Recorder Case Studies 13 Select DataLoggerl in the list of Available Strip Charts group then click the Setup button to open the Logger
392. r Fraction Raw Crude 0 2937 PreFlash Wap 1 0000 PreFlash Lig 0 0000 _ Hot Crude 0 4003 Atm Inlet 0 6122 AGO Steam 1 0000 Temperature F 450 0 450 0 450 0 650 0 622 2 300 0 Pressure psia Molar Flow Ibmolehr 75 00 6214 75 00 1825 75 00 4389 65 00 4389 65 00 6214 50 00 138 8 Mass Flow lb hr 1 282e 006 1 602e 005 1 122e 006 1 122e 006 1 282e 006 2500 Liquid Volume Flow barrel day 1 000e 005 1 490e 004 8 510e 004 8 510e 004 1 000e 005 171 5 Heat Flow Btu hr Name Vapour Fraction 9 192e 008 Main Steam 1 0000 1 004e 008 Diesel Steam 1 0000 6 187 e 008 Residue 0 0000 6 447e 008 Dff Gas 1 0000 7 452e 008 Waste Water 0 0000 1 414e 007 Naphtha 0 0000 Temperature F 375 0 300 0 663 1 107 3 107 3 107 3 Pressure psia 150 0 Molar Flow Ibmole hr Mass Flow Ib hr 416 3 50 00 166 5 32 70 1397 19 70 4 473e 005 19 70 700 9 19 70 2822 7500 3000 6 216e 005 2 304e 003 1 263e 004 2 474e 005 Liquid Volume Flow barrel day 514 6 205 8 4 398e 004 2 612e 004 866 4 2 300e 004 Heat Flow Btu hr Vapour Fraction 4 222e 007 Kerosene 0 0000 1 697e 007 Diesel 0 0000 3 647e 008 AGO 0 0000 2296 New
393. r at a controlled flow rate such that the desired ratio of H2 N2 in the synthesis gas is attained C2 3 5 The oxygen from the air is consumed in an exothermic combustion reaction while the inert nitrogen passes through the system The addition of steam serves the dual purpose of maintaining the reactor temperature and ensuring that the excess methane from the natural gas stream is consumed In the last two reactors the water gas shift equilibrium reaction takes place as the temperature of the stream is successively lowered There are two general steps in this process simulation l Setup In this step the Fluid package Reaction sets and Reaction components are selected The Reaction Component list includes CH4 H20 CO CO2 H2 N2 and 02 Steady State Simulation The case will be built in steady state with the following key unit ops e Reformer A conversion reactor in which most of the methane is reacted with steam to produce hydrogen carbon monoxide and carbon dioxide e Combustor A second conversion reactor which takes the product of the Reformer an Air stream and a Comb Steam stream as the feeds to the reactor e Shift Reactors A series of equilibrium reactors in which the water gas shift reaction occurs 2 2 Setup From the Tools menu select Preferences In the Session Preferences view Variables tab Units page select Field units for this application Close the Session Preferences view 2 2 1 Compo
394. r icon a 1 122 12 Click the Face Plate button at the bottom of the property view 13 Change the controller mode to Auto on the face plate by opening the drop down list and selecting Auto Close the face plate view when you are finished Figure 1 154 Sep LC xl Exec Int Sp L PY lt empty gt OP 50 00 14 Using the same procedures add another PID Controller operation that will serve as the LTS level controller Specify the following details Tab Page In this cell Enter Process Variable LTS object Liquid Source Percent Level variable Output Target Object LTS Valve Ke 2 15 Click the Face Plate button Change the controller mode to Auto on the face plate view Next you will enter the Column sub flowsheet environment 16 Instead of entering through the Column property view click the Object Navigator icon in the Toolbar 17 Double click on DePropanizer in the Flowsheets group to enter the Column sub flowsheet environment 18 Ensure the PFD for the column is visible The Column sub flowsheet uses a simplified Object Palette To add a PID Controller operation in the sub flowsheet right click the PID Controller icon in the Object Palette and drag the cursor to the PFD The Flow values shown here do not use the default units Enter the values then select the correct units from the drop down list HYSYS automatically converts the values to the default units Gas
395. r left corner of the PFD view For more information on customizing the PFD refer to Chapter 7 25 PFD in the User Guide 2 95 2 96 Steady State Simulation The customized PFD appears below Figure 2 117 To Condenser Reflux Condenser WasteH20 Naphtha Kero _Retum Kero _Draw Kero 5_Energy hain TS Kero _BoilUp KeroS _Reb Lu KeroSS_ToReb Kerosene DieselSS_Retum DieselS _Draw DieselS PR_3_Cooler q Diesel Steam La Diesel AGOSS_Retum PA_3_Draw Tower Feed Trim Duty Bottom E 2 E 8 zy 10 15 18 19 20 E 22 23 gs D esidue 12 To view the workbook for the column click the Workbook icon Figure 2 118 Workbook Atmos Tower COL1 OF x Reflux To Condenser Naphtha Off Gas Residue Bottom Steam Tower Feed 2 96 apour Fraction emperature F ressure psia iquid Yolume Flow barrel day eat Flow Btu hr apour Fraction emperature F ressure psia iquid Volume Flow barrel day eat Flow Btu hr apour Fraction emperature F ressure psia iquid Volume Flow barrel day eat Flow Btushr apour Fraction emperature F ressure psia iquid Volume Flow barrel day eat Flow Btu hr Doz zIy4 Doz z yaA4 IIC zZz z D H lt IICIzZz zi D H lt fo jo wo wfo e 8 a 2 g in be n n a a ajn olg o 5 i mT i 2 FIF TIF FIF FIF 3 3 3 3 ai EIES Ear EJEN m m om m
396. r ratio in the Synthesis Gas stream calculate the ratio in a Spreadsheet and then use an Adjust operation The Synthesis Gas should have an H N gt molar ratio slightly greater than 3 1 Prior to entering the ammonia plant hydrogen is used to rid the synthesis gas of any remaining CO and COs 1 Create a Spreadsheet and change the Spreadsheet Name to SSRatio Import the following variables e Synthesis Gas Comp Molar Flow Hydrogen e Synthesis Gas Comp Molar Flow Nitrogen 2 Assign the Hydrogen value to cell B1 and the Nitrogen value to cell B2 Synthesis Gas Production 3 Incell B4 calculate the Hy N gt ratio using the following formula B1 cell that contains flow of H2 B2 cell that contains flow of N2 The Spreadsheet tab of the Spreadsheet view should appear similar to the following i Hydrogen Nitrogen H2N2 Ratio 4 Click the Parameters tab and define the Variable name for the B4 cell as Hy N gt Ratio 5 Install the Adjust operation as shown below Adjust ADJ 2 Tab inthis cell Entet Connections Adjusted Variable Air Molar Flow Target Variable SSRatio B4 H2 N2 Ratio Step Size 39 68 lbmole hr 6 Click the Start button to begin the Adjust operation The Secant method is used for both Adjust operations even though each adjusted variable will have an effect on the other operation s target variable The close proximity of the logical operations in the flowsheet increas
397. rac Methane 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Comp Mole Frac H20 0 2518 0 2738 0 2737 0 2171 0 2172 0 2049 0 2051 Comp Mole Frac CO 0 0770 0 0990 0 0990 0 0423 0 0423 0 0301 0 0301 Comp Mole Frac C02 0 0817 0 0598 0 0598 0 1164 0 1165 0 1286 0 1286 Comp Mole Frac Hydrogen 0 5222 0 5003 0 5003 0 5570 0 5568 0 5691 0 5689 Comp Mole Frac Nitrogen 0 0672 0 0672 0 0672 0 0672 0 0672 0 0672 0 0672 Comp Mole Frac Oxygen 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Name New Material Steams Compositions Energy Streams Unit Ops C2 17 RB Results 8 Results C2 18 Case Linking i F H X1 1 Process Descrip onoinene r a a ATE 3 X1 2 Building Flowsheet i nnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnnaninnnnnnnnnnnnnnnne 4 X1 2 1 Setup T o o oo aaaeeeaa 4 X1 2 2 Installing Streams cccccsseeceeseeseeeeseeeeeeesaeeeeeeeaeeeeeeens 5 X1 2 3 Instalbrg Unit Operations NA eneren 5 X1 3 Builditg Flowsheet 2 nnnnnnnnnsriinnnnnnnnn MMMM cccnnseccnnssccnsssecenssecenees 8 See An oilers 8 X1 3 2 Installing Unit Operations cee ceccceeeeeeeeeeeeeeeeeeeeesnaeeees 8 X1 4 Creating a User Unit Operation cccccsssssseeeeeseeeseeeeeeeeeeneeees 10 X1 4 1 Initializing the User Unit Op i eeeeceeeeeeeeeeeeeeeeees 11 X1 4 2 Operation Execution cccccccecceceseeeceesseeessse
398. ream Specify the feed stream as shown below Material Stream SourH2O Feed Presse R2 5 R2 6 Steady State Simulation If messages appear regarding loading an older case or installing property sets click the OK button They will not affect the case R2 6 Operations 1 Install and specify the Heat Exchanger as shown below Heat Exchanger Feed Bottoms TablPage inthis cel teh O OOOO 2 Install a Distillation Column using the Distillation Column icon in the Object Palette This column will have both a reboiler and an overhead condenser 3 Define the Column configuration as shown below Column SW Stripper Page inthis cells Emere O Reboiler Energy Stream 4 Inthe Column property view click the Design tab then select the Monitor page 5 Click the Add Specs button to install new specifications In the present configuration the column has two degrees of freedom For this example the two specifications used will be a quality specification and a reflux ratio Sour Water Stripper RAT Water Stripper R2 7 6 First uncheck the Active checkbox for the Ovhd Vap Rate specification 7 Add a Component Fraction specification and modify the existing Reflux Ratio specification and define as shown below Column SW Stripper Tab Page In this cell Emere O O Design Specs Liquid Mass Frac Active Stage Reboiler Spec Value 0 000010 Component NH3 Reflux Ratio Active Spe
399. ream e 16 Double click the mixer icon MIX 100 Change the name to Mixer then close the view 2 64 Refining Tutorial 2 65 Resizing Icons in the PFD Resize icons in the PFD to make it easier to read 1 Resize the PFD view by clicking and dragging the outside border 2 Click the Zoom All icon to fill the PFD window including any objects that were not visible previously A possible view of the resized PFD Zoom All icon appears in the figure below Figure 2 75 ioixi H A Ta tA RR e A i E Default Colour Scheme x PreFlashVap PreFlash Diesel Steam Preheat Crude 3 Click the Size Mode icon on the PFD toolbar Hf 4 Click the Furnace icon in the PFD A frame with sizing handles appears around the icon Size Mode icon 5 Place the cursor over one of the sizing handles The cursor changes to a double ended sizing arrow Figure 2 76 Double ended sizing arrow 6 With the sizing arrow visible click and drag to resize the icon 7 Click the Size Mode icon again to return to Move mode 2 65 2 66 Steady State Simulation gt Energy Stream icon Save icon If you choose to use the pre built crude column template you still have to customize the column by modifying the various draw and return stages and default specifications Although using the template eliminates the majority of the work over the next few pages it is recommended that you w
400. rial streams a dark blue icon indicates the stream has been flashed and is entirely known A light blue icon indicates the stream cannot be flashed until some additional information is supplied Similarly a dark red icon is for an energy stream with a known duty while a purple icon indicates an unknown duty Installing the Reactor Next you will install a continuously stirred tank reactor operation CSTR You can install streams or operations by dropping them from the Object Palette onto the PFD 1 Ensure that the Object Palette is displayed if it is not press F4 2 You will add the CSTR to the right of the Mixer so if you need to make some empty space available in the PFD scroll to the right using the horizontal scroll bar 3 Inthe Object Palette click the CSTR icon 4 Position the cursor in the PFD to the right of the Mixer Out stream The cursor changes to a special cursor with a plus symbol attached to it The symbol indicates the location of the operation icon Figure 3 59 gt PFD Case Main E iol x EAE x Hi il HI tH Ret p A v i D Default Colour Scheme cP A x 5 Click to drop the Reactor onto the PFD HYSYS creates a new Reactor with a default name CSTR 100 The Reactor has red status colour indicating that it requires feed and product streams Chemicals Tutorial Attaching Streams to the Reactor H 1 Click the Attach Mode icon on the PFD toolbar to enter Attach Atta
401. rksheet Stream Name Feed 2 Vapour Phase Fraction __ lt empty gt Conditions Temperature F 60 000 Properties Pressure psia 600 00 Composition Molar Flow MMSCFD K Value Std Ideal Lig Vol Flow barrel day 4 0000 lt empty gt lt empty gt User Variables Molar Enthalpy Btu Ibmole lt empty gt Molar Entropy Btu lbmole F lt empty gt Notes Heat Flow Btu hr Cost Parameters Lig Vol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 u Worksheet Dynamics Delete Define from Other Stream lt a gt 5 Click the Composition page Figure 1 30 Feed 2 Worksheet Conditions lt empty gt lt empty gt lt empty gt Properties lt empty gt Composition K Value lt empty gt lt empty gt lt empty gt User Variables Notes Cost Parameters lt Worksheet Attachments Dynamics Total 0 00000 Edit Edit Properties Basis a Define from Other Stream con o gt 1 28 Gas Processing Tutorial 1 29 Processing Tutorial 1 29 The current Composition 6 Click the Edit button at the bottom of the Composition page The Basis setting is the Input Composition for Stream view appears Preferences default You must enter the stream composition on a mass basis Figure 1 31 Ni Inpu
402. rmation displayed on any tab Object Palette A floating palette of buttons that can be used to add streams and unit operations Before proceeding any further to install streams or unit operations save your Case 1 Do one of the following e Click the Save icon on the toolbar e From the File menu select Save e Press CTRL S If this is the first time you have saved your case the Save Simulation Case As view appears By default the File Path is the Cases sub directory in your HYSYS directory 2 Inthe File Name cell type a name for the case for example GLYCOL You do not have to enter the hsc extension HYSYS automatically adds it for you 3 Once you have entered a file name press the ENTER key or the OK button HYSYS will now save the case under the name you have given it when you Save in the future The Save As view will not appear again unless you choose to give it a new name using the Save As command 3 27 3 27 3 28 Workbook Icon HYSYS accepts blank spaces within a stream or operation name 3 28 Steady State Simulation 3 2 6 Using the Workbook Installing the Feed Streams In general the first task you perform when you enter the Simulation environment is to install one or more feed streams In this section you will install feed streams using the Workbook 1 Click the Workbook icon on the toolbar to make the Workbook active 2 On the Material Streams tab click in the New cel
403. rop down list select Auto to change the controller mode 14 Double click in the PV value field type 85 then press ENTER 15 Close the Reactor LC face plate view then close the Reactor LC property view Flow Control Next you will add flow controllers to the feed streams in the process 1 The Control Ops sub palette should still be open If it isn t click the Control Ops icon in the Object Palette In the sub palette click the PID Controller icon In the PFD click above the Prop Oxide stream icon The IC 100 icon appears This controller will serve as the Prop Oxide flow controller Double click the IC 100 icon to open its property view Specify the following details Tab Page In this cell Enter Connections PropOxide FC Process Variable Source Prop Oxide Mass Flow Output Target Object VLV Prop Oxide Parameters Configuration 6 Click the Face Plate button Change the controller mode to Auto and input a set point of 8712 lb hr Chemicals Tutorial Close the PropOxide FC face plate view and property view In the Object sub palette click the PID Controller icon In the PFD click below the Water Feed stream icon The controller icon appears This controller will serve as the Water Feed flow controller 10 Double click the controller icon then specify the following details Tab Page In this cell Enter Connections WaterFeed FC Process Variable Source Water Feed Mass Flow Ou
404. rs and three cooled pump around circuits The column sub flowsheet appears below Figure 2 2 Cooler A roan PES PA_1_Retum Pa amp _1_Cooler PA_1_Draw PA_2_0 Cooler PA_2_ Retum PA Cooler PA_2 Draw PA_B_Q Cooler PA_3_Retum PR_3_Cooler PA_3_Draw Tower Feed Trim Duty No h ee ee j a ej Si Sop D am S Bottom Js D To Condenser Reflux Condenser WasteH20 Naphtha Kero _Retum Kero _Energy Kero _BoilUp Kero _Reb Kero _ToReb rr a DieselSS_Retum Diesel _Draw DieselSS q AGOSS_Retum Diesel Steam La Diesel tery esidue The following pages guide you through building a HYSYS case for modeling this process This tutorial illustrates the complete construction of the simulation from selecting a property package and components characterizing the crude oil to installing streams and unit operations through to examining the final results The tools available in HYSYS are utilized to illustrate the flexibility available to you Before proceeding you should have read Chapter A HYSYS Tutorials which precedes the Tutorials in this manual Refining Tutorial 2 2 Steady State Simulation 2 2 1 Process Description This example models a crude oil processing facility consisting of a pre fractionation train used to heat the crude liquids and an atmospheric crude column to fractionate the crude into its straight run products Th
405. rt The first page of the Input Expert should appear as shown in the following figure Figure 3 74 Ni Distillation Column Input Expert Condenser Energy Stream CondDuty Column Name Tower Condenser Ovh Ovhd Outlets RecyProds P Water Draw Inlet Streams Inlet Stage eactor Prods 5 Mair Optional Side Draws lt Stream gt gt Reboiler Energy Stream RebDuty Bottoms Liquid Outlet Glycol v Stage Numbering Top Down Pres Next gt C Bottom Up Connections page 1 of 4 Cancel 12 Click the Next button to advance to the Pressure Profile page 3 58 Steady State Simulation Although HYSYS does not require estimates to produce a converged column you should provide estimates for columns that are difficult to converge 3 58 13 In the Condenser Pressure field enter 15 psia In the Reboiler Pressure field enter 17 psia Leave the Condenser Pressure Drop at its default value of zero Figure 3 75 Ni Distillation Column Input Expert Condenser Pressure f 5 00 psia Condenser Pressure Drop 0 0000 psi Reboiler Pressure lt Prev Pressure Profile page 2 of 4 Cancel 14 Click the Next button to advance to the Optional Estimates page For this example no estimates are required 15 Click the Next button to advance to the fourth and final page of the Input Expert This page allows you to supply values for the default column specifi
406. rties Pressure psia 580 00 LiquidProd Liquid Production l barrel day Molar Flow MMSCFD 8 9765 Eamonn a ee Mass Flow lb hr 23183 K Value Std Ideal Lig Vol Flow barrel day 4342 2 View DataBook User Variables Molar Enthalpy Btu Ibmole S 3 823e 004 Molar Entropy Btu lbmole F 33 423 Notes Heat Flow Btu hr 3 7685e 07 Cost Parameters Lig Yol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 Worksheet Dynamics eee Delete Define from Other Stream gt 1 85 1 86 Steady State Simulation Currently the LTS temperature is 0 E The key variables will be checked at 10 F 6 Inthe ColdGas Temperature cell enter 10 HYSYS automatically recalculates the flowsheet The new results are shown below Figure 1 113 1D ETT moe F Worksheet Stream Name ColdGas prey eae ag IF EIA z Vapour 7 Phase Fraction 0 82007 _SalesDP DewPoint F Conditions Temperature F 10 000 SalesG as Sales Gas Productior MMSCFD Properties Pesona LiquidProd Liquid Production barrel day No Tag E Molar Flow MMSCFD T 8 3765 gt Mass Flow lb hr 23183 K Value Std Ideal Lig Vol Flow barrel day 43M2 View DataBook User Variables Molar Enthalpy Btu Ibmole 3 796e 004 Molar Entropy Btu lbmole F 34 018 Notas Heat Flow Btu hr 3 7413e 07 Cost Parameters Liq Yol Flow Std Cond
407. ry list 1 Click on the first component in the list in this case C1 2 Doone of the following e Hold the SHIFT key and click on the last component required in this case nC4 All components C1 through nC4 will now be selected Release the SHIFT key e Click and hold on C1 drag down to nC4 and release the mouse button C1 through nC4 will be selected 3 Click the Add Pure button The highlighted components are transferred to the Selected Components list The completed component list appears below Figure 1 15 Selected Components A component can be removed from the Current Components List by selecting it and clicking fi PETA the Remove button or the EE DELETE key lt Substitute gt Sort List Viewing Component Properties To view the properties of one or more components select the component s and click the View Component button HYSYS opens the property view s for the component s you selected For example 1 Click on CO2 in the Selected Components list 2 Press and hold the Crrt key 3 Click on n Butane The two components should now be selected Steady State Simulation 4 Release the crrt key Figure 1 16 Selected Components lt Add Pure lt Substitute gt Remove gt Sort List View Component 5 Click the View Component button The property views for the two components appear Figure 1 17 S C02 n Butane Oe x Component
408. s Uninitialized Insert Valves Int Flow Spec Set pressure specifications in these streams LiquidProd M SalesGas M Tell me why lt 7 n General Streams Pressure Flow Specs Unknown Sizes Tray sections ler J Analyze Again i i Cancel 1 114 Gas Processing Tutorial 115 Processing Tutorial 1 115 some of the columns orrows FOT each page in the Streams tab set the following on the pages are not visible recommendations as active or inactive according to the table shown use the scroll bars beside or below under the information area to bring the columns or rows into view Tab Page Recommendation Stream OK Checkbox Streams Pressure Specs Remove Pressure Feed 1 Kiks Specifications Set Pressure LiquidProd Specifications e E Streams Flow Specs Remove Flow An active recommendation will Specifications be implemented by the A Dynamics Assistant Streams Insert Valves Insert Valves Inactive LIK Ovhd Inactive m Streams Int Flow Spec Set Internal Flow Ke E Ei Ee Specification An inactive recommendation will be ignored by the 4 Click the Pressure Flow Specs tab Dynamics Assistant Figure 1 144 Ni Dynamics Assistant Pressure Flow Select pressure flow option instead of pressure drop PF versus DP Name LNG Chiller M Gas Gas WM Heater WM This tab contains a list of unit operations which can use a Press
409. s Compositions Energy Streams Unit Ops Preheat Crude PreFlashLiq PreFlash ap C Include Sub Flowsheets The matrix shows the operation Name its Object Type the attached streams Inlet and Outlet whether it is Ignored and its Calculation Level Optional Methods for Accessing Property Views When you click the View UnitOp button the property view for the operation occupying the active row in the matrix opens Alternatively by double clicking on any cell except Inlet and Outlet associated with the operation you also open its property view You can also open the property view for a stream directly from the Unit Ops tab of the Workbook When any of the Name Object Type Ignored or Calc Level cells are active the display field at the bottom of the view displays all streams attached to the current operation Currently the Name cell for PreFlash is active and the display field displays the three streams attached to this operation To open the property view for one of the streams attached to the separator such as Preheat Crude do one of the following e Double click on Preheat Crude in the display field at the bottom of the view e Double click on the Inlet cell for PreFlash The property view for the first listed feed stream opens In this case Preheat Crude is the only feed stream so its property view also opens 2 52 Steady State Simulation Return to the Material Streams tab of the Workbook Any utilitie
410. s Description naeneneannnnnneoennnsenensnrennnrernnnesenee X1 3 X1 2 Building FIOWSNCCT vis ieedovsiaiivnoresiisne aioe ue X1 4 X1 3 Building Flowsheet 2 cccccccccsssseeeeessserenseseeesseaeeees X1 8 X1 4 Creating a User Unit Operation eee X1 10 All completed Tutorial cases are included with your HYSYS package and are available on HYSYS Samples HYSYS Tutorials A 1 HYSYS Tutorials The Tutorials section of this manual presents you with independent tutorial sessions Each tutorial guides you step by step through the complete construction of a HYSYS simulation The tutorial s you choose to work through will likely depend on the simulation topic that is most closely related to your work your familiarity with HYSYS and the types of simulation cases you anticipate on creating in the future Regardless of which tutorial you work through first you will gain the same basic understanding of the steps and tools used to build a HYSYS simulation After building one of these tutorial cases you might choose to build one or several more or begin creating your own simulations If you are new to HYSYS it is recommended that you begin with the steady state tutorials These tutorials explicitly detail each step required to complete the simulation In steps where more than one method is available to complete a particular action all methods are outlined The dynamic tutorials which are continued after the steady state sec
411. s attached to the stream with the Workbook active are also displayed in and are accessible through this display field 2 52 c c Using Workbook Features Before you install the remaining operations you will examin a number of Workbook features that allow you to access information quickly and change how information appears Accessing Unit Operations from the Workbook There are a number of ways to open the property view for an operation directly from the Workbook besides using the Unit Ops tab When your current location is a Workbook streams tab Material Streams Compositions and Energy Streams tabs the field at the bottom of the Workbook view displays the operations to which the current stream is attached In this display field you can click on any cell associated with the stream For example if you click in any cell for Preheat Crude the field displays the name of the operation PreFlash to which this stream is attached The display field also displays FeederBlock_Preheat Crude because the Preheat Crude stream is a boundary stream To access the property view for the PreFlash operation double click on PreFlash The operation property view appears Figure 2 57 Stream Preheat Crude is the current Workbook location Workbook Case Main Name Preheat Crude Bottom Steam Diesel Steam Vapour Fraction 0 1292 1 0000 1 0000 Temperature F 450 0 375 0 300 0 Pressure psia 75 00 150 0 50 0
412. s belonging to certain families i 4 Property Package Filter P Recommended Only lt none gt ma Family Type Filter fw Use Filter Hydrocarbons Solids Miscellaneous Amines Alcohols Ketones Aldehydes Esters Caboxyplic Acids Halogers D Nitriles Phenols Ethers User Defined All Invert Next you will add Propylene Glycol to the component list using the filter 5 Ensure the Match field is empty by pressing ALT M and then the DELETE key Click the View Filters button The Filters view appears Click the Use Filter checkbox to activate the filter checkboxes Since Propylene Glycol is an alcohol click the Alcohols checkbox 3 12 Chemicals Tutorial 3 13 9 Inthe Match field begin typing propyleneglycol as one word HYSYS filters as you type displaying only the alcohols that match your input Figure 3 14 Component List iew a 10l x Add Component Selected Components Components Available in the Component Library a 12C30xide Match propyle View Filters raditiona Electrolyte Sim Name C Full Name Synonym Formula Hypothetical a oer TriC3 Glycol Propanol 1 Methyl 1 2 Ethanediyl bis oxy Jbis CSHz er lt Add Pure 12 C3diol Propylene_Glycol C3H802 lt Substitute gt Remove gt Sort List View Component J Show Synonyms Cluster u Selected Component by Type
413. s group Figure 2 35 Selected Components Hypoth etical H20 components are Propane SHu Butane indicated by qt rPentene after the HEE lt Add Pure compone nt NBP O 139 name t a a lt Substitute gt NBP O 213 NBP 0 238 NBP 0 261 NBP 0 289 NBP O 313 NBP 0 338 Sort List NBP O 362 NBP 0 388 NBP 0 412 NBP 0 437 NBPIOM62 Viewing Component Properties To view the properties of one or more components select the component s and click the View Component button HYSYS opens the property view s for the component s you selected 1 Inthe Selected Components list select H2Oand NBP 0 113 2 Click the View Component button The property views for these two components appear Figure 2 36 H20 ioixil i xi Component Identification NBP O 113 Family 7 Class Hydrocarbon Chem Formula ID Number 10000 Group Name Blend 1 Hypos CAS Number UNIFAC Structure Structure Builder lt lt lt No Structure Available gt gt gt User ID Tags Tag Number _ i ___ lt empty gt NotSpec d Critical Point TDep UserProp a Estimate Unknown Props Edit Properties Edit Yisc Curve 2 35 2 36 Steady State Simulation See Chapter 3 Hypotheticals in the Simulation Basis manual for more information on cloning library components Basis Manager icon 2 36 The Component property view provid
414. s information is supplied 2 57 The icons for all streams installed to this point are dark blue indicating they have been flashed Heater icon Red Cooler icon Blue Notice the heater has red status colour indicating that it requires feed and product streams 2 58 Steady State Simulation A similar colour scheme is used to indicate the status of streams For material streams a dark blue icon indicates the stream has been flashed and is entirely known A light blue icon indicates the stream cannot be flashed until some additional information is supplied Similarly a dark red icon is for an energy stream with a known duty while a purple icon indicates an unknown duty Installing the Crude Furnace In this section you will install a crude furnace The furnace is modeled as a Heater 1 Ensure the Object Palette is visible if it is not press F4 You will add the furnace to the right of the PreFlash Separator so make some empty space available by scrolling to the right using the horizontal scroll bar 2 Inthe Object Palette click the Heater icon The cursor changes to a special cursor with a black frame and plus symbol attached to it The frame indicates the size and location of the operation icon 3 Position the cursor over the PFD to the right of the separator Figure 2 64 PFD Case Main lolx pana tona Serene mi E H 4 ot 4 Wei p A DefaultColou Scheme Y E SN Pre
415. s to the simulation case e Size the Valve Vessel and Heat Exchanger operations 1 113 1 114 Dynamic Simulation 1 Click the Dynamics Assistant icon Browse through each tab in the Dynamics Assistant view to inspect the recommendations a Dynamics Assistant icon Figure 1 142 Dynamics Assistant Make changes Disable stream pressure specifications Disable stream flow specifications Enable stream pressure specifications Append new valves and streams Enable pressure flow equations not pressure drop Enable internal stream flow specifications Miscellaneous specification changes Volumes not known Pressure flow k values not known Tray section pressure profile needs attention Stream pressures differ from attached stages About Preferences General Pressure Flow Specs Unknown Sizes Tray sections ler J Analyze Again i i Cancel KKI XKS Green checkmarks appear in the Make Changes column beside all recommendations by default You can choose which recommendations will be executed by the Assistant by activating or deactivating the checkboxes beside each recommendation 2 Click the Streams tab The Streams tab contains a Figure 1 143 list of recommendations regarding the setting or I Dynamics Assistant removing of pressure flow specification s in the flowsheet Stream Specs Remove pressure specifications in these streams Pressure Specs Flow Spec
416. say HYSYS provides two default temperatures 100 F and 210 F for entering bulk viscosity but these temperature values are ignored unless corresponding viscosities are provided Since the value for bulk viscosity is not supplied there is no need to delete or change the temperature values Entering Boiling Temperature TBP Data The next task is to enter the TBP distillation data 1 Click the Calculation Defaults tab 2 Inthe Extrapolation Methods group select Lagrange from the Distillation drop down list Return to the Input Data tab Select the Distillation radio button The corresponding TBP data matrix appears HYSYS displays a message under the matrix stating that At least 5 points are required before the assay can be calculated From the Assay Basis drop down list select Liquid Volume Click the Edit Assay button The Assay Input Table view appears Click in the top cell of the Assay Percent column OND oO Type 0 then press the ENTER key You are automatically advanced to the corresponding empty Temperature cell 9 Type 80 then press the ENTER key You are automatically advanced down to the next empty Assay Percent cell Refining Tutorial 2 25 10 Repeat steps 8 and 9 to enter the remaining Assay Percent and Temperature values as shown Figure 2 22 Ni Assay Input Table Fa Assay Input Data a 80 00 __ 258 0 349 0 430 0 527 0 635 0 751 0 915 0 1035 1
417. se button to return to the Gas Gas property view The new specification appears in the Specifications group on the Specs page Figure 1 73 m Gas Gas Design Solver Unknown Variables eee Tolerance 1000 014 ale dl Current Error lt empty gt Temperature of CoolGas Parameters Maximum Iterations 25 Specs Iterations pee Unknown Variables 1 Constraints 1 Notes Degrees of Freedom 0 User Yariables Specifications CSp ecified Value Current Value Relative Error O00Btuh 29e010 B2e0I6 E 100 UA lt empty gt 2 1e 004 lt empty gt Hot Side Approach 10 0 00 Delete Rating Worksheet Performance Dynamics HTFS TASC Delite mmm ie T Iancred 7 Click the Worksheet tab then select the Conditions page to view the calculated stream properties Figure 1 74 m Gas Gas Worksheet Name Sep ap Conditions Properties Composition 2 318e 004 2 318e 004 1 562e 004 1 562e 004 PF Specs lt 4842 BA SG 3 657e 004 3 705e 004 3 536e 004 3 475e 004 36 77 35 86 35 61 36 90 3 605e 007 3 652e 007 2 725e 007 2 678e 007 Tag Design Rating Worksheet Dynamics HTFS TASC Delte mmm Uedate T Ignored 1 60 Gas Processing Tutorial 61 Processing Tutorial 1 61 Using the 10 F approach HYSYS calculates the t
418. sed to split the feed stream into its liquid and vapour phases As with most commands in HYSYS installing an operation can be accomplished in a number of ways One method is through the Unit Ops tab of the Workbook l 2 3 Click the Workbook icon to ensure the Workbook is the active view Move to the Unit Ops tab Click the Add UnitOp button The UnitOps view appears listing all available unit operations In the Categories group select the Vessels radio button HYSYS produces a filtered list of unit operations showing only those in the current category Add the separator by doing one of the following e Select Separator in the list of Available Unit Operations and click the Add button or the ENTER key e Double click on Separator Figure 2 50 gt UnitOps Case Main Categories Available Unit Operations All Unit Ops 3 Phase Separator oa Vessels Cont Stirred Tank Reactor ae Heat Transfer Equipment Conversion Reactor a ae E Equilibrium Reactor SENS oS Gibbs Reactor Piping Equipment Solids Handling Reactors C Prebuilt Columns Short Cut Columns Sub Flowsheets C Logicals Extensions C User Ops C Electrolyte Equipment C Refine Ops Steady State Simulation HYSYS provides the default name V 100 for the separator The default naming scheme for unit operations can be changed in your Session Preferences 2 48 The property view for the separator appears in
419. sel al 2i 3 a E 10 19 20 E 22 23 Bottom Steam Js D esidue The main column consists of 29 trays plus a partial condenser The TowerFeed enters on stage 28 while superheated steam is fed to the bottom stage In addition the trim duty is represented by an energy stream feeding onto stage 28 The Naphtha product as well as the water stream WasteH20 are produced from the three phase condenser Crude atmospheric Residue is yielded from the bottom of the tower Each of the three stage side strippers yields a straight run product Kerosene is produced from the reboiled KeroSS side stripper while Diesel and AGO atmospheric gas oil are produced from the steam stripped DieselSS and AGOSS side strippers respectively The two primary building tools Workbook and PFD are used to install the streams and operations and to examine the results while progressing through the simulation Both of these tools provide you with a large amount of flexibility in building your simulation and in quickly accessing the information you need The default Preference file is named HYSYS prf When you modify any of the preferences you can save the changes in a new Preference file by clicking the Save Preference Set button HYSYS prompts you to provide a name for the new Preference file which you can later use in any simulation case by clicking the Load Preference Set button Refining Tutorial The Workbook is used to
420. sensitivities for flow and composition as indicated below Recycle RCY 1 TRE in this cels Enters Acid Gas Sweetening with DEA O14 Simulation Analysis The incoming sour gas contains 4 1 CO2 and 1 7 H2S For an inlet gas flow rate of 25 MMSCED a circulating solution of approximately 28 wt DEA in water removes virtually all of the H2S and most of the CO2 A typical pipeline specification for the sweet gas is no more than 2 0 vol CO2 and 4 ppm volume H2S If you look at the property view of the Sweet Gas stream you will see the sweet gas produced easily meets these criteria 01 5 Calculating Lean amp Rich Loadings Concentrations of acid gas components in an amine stream are typically expressed in terms of amine loading defined as moles of the particular acid gas divided by moles of the circulating amine The Spreadsheet in HYSYS is well suited for this calculation Not only can the loading be directly calculated and displayed but it can be incorporated into the simulation to provide a control point for optimizing the amine simulation Also for convenience the CO2 and H2S volume compositions for the Sweet Gas stream are calculated The following variables are used for the loading calculations Figure G1 5 88 SPRDSHT 1 5 x Imported ariables cal tie Vasiable Description Edit impot RICH DEA Comp Molar Flow DEAmir RICH DEA Comp Molar Flow H2 RICH DEA Comp Molar Flow CO _Add
421. serVariable LinkStr eam binkSt ream uvtText utcNull 0 LinkCase Variable Value ActiveObject SimulationCase Path amp LinkCase2 hsc lf an error occurs during the execution of this subroutine go to the line designated Catch You are setting the names that will be associated with the energy and material primary and secondary inlet and exit connections Feeds Feed compressed ___ lt empty gt a Unused Feed Products Unused Prod lt empty gt a Unused Prod2 E Unused Energy Feeds E Unused Energy Products Deactivates the secondary inlet and exit connections as well as the energy inlet and exit connections After the initialization subroutine has been successfully implemented the checkboxes associated with the secondary material connections and energy connections should be deactivated as shown in the figure above Creates a text user variables called LinkCase This will appear on the Variables page of the Design tab along with the current values This variable holds the path and name of the linked case Creates a text user variables called LinkStream This will appear on the Variables page of the Design tab along with the current values This variable holds the name of the stream to link to This sets the linked case path to be the same as the current case and sets the name to LinkCase2 hsc Xi Creating a User Unit Operation Explanatio
422. simplified steady state model to be converted to dynamics 2 Implement a tray sizing utility for sizing the column and the side stripper tray sections Install and define the appropriate controllers Add the appropriate pressure flow specifications Set up the Databook Make changes to key variables in the process and observe the dynamic behaviour of the model 2 5 1 Simplifying the Steady State Flowsheet In this section you will The preflash train in the steady state simulation case R 1 hsc is deleted in this section 1 Open the pre built case file R 1 hsc The crude column simulation file R 1 hsc is located in your HYSYS Samples directory 2 Press F4 to make the Object Palette visible For the purpose of this example the Session Preferences are set so that the Dynamic Assistant will not manipulate the dynamic specifications 3 From the Tools menu select Preferences The Session Preference view appears 4 On the Simulation tab select the Dynamics page Deactivate the Set dynamic stream specifications in the background checkbox Figure 2 147 Assistant IV Perform checks when switching to dynamics or starting the integrator Click the Variables tab then select the Units page In the Available Unit Sets group select SI Click the Close icon to close the Session Preferences view Close all other views except for the PFD view 2 115 2416 Dynamic Simulation 16 Dynamic Simulation 9 Add a mater
423. sitions d 1 Click the Cut Blend tab Oil Characterization view and click the Add button The Blend Blend 1 view appears Propane 0 0088 i e 0 0055 2 Click the Data tab then select the Assay you created in the Available aay Assays column NBP_ 0 0403 ____ ora 3 Click the Add button HYSYS will transfer that Assay to the Oil Flow NBP_ 0 0502 Information table 0 0519 0 0504 E ee As a guideline each Outlet stream from the crude column should 3 i contain a minimum of 5 hypocomponents where the composition is NBP_ 0 0396 greater than 1 0 Therefore a total of 30 components should fulfil 0 0444 l 0u this requirement NBP_ 0 0415 i Le aes 4 From the Cut Option Selection drop down list select User Points 0 0267 then specify the Number of Cuts at 30 HYSYS will calculate the ae hypocomponents 0 0181 a 5 Click the Tables tab to view the hypocomponents INRP 971 N NPAR From the Table Type group drop down list select Molar Compositions 7 Close the Blend view Install Qil in the Flowsheet The final step is to install the oil in the flowsheet 1 Click the Install Oil tab of the Oil Characterization view 2 Inthe Stream Name cell type Raw Crude This is the stream name where you would like to install the oil 3 Onthe Oil Characterization view click Return to Basis Environment button 4 Click the Enter Simulation Environment button on the Simulation Basis Manager view to enter the
424. ssay Input Table x Assay Input Data Assay Percent Mass Density API lt empty gt All input curves except distillation are on midpoint basis Dependent curves will be shifted to middle Cancel OK Click the Edit Assay button to access the Assay Input Table Refining Tutorial Entering Viscosity Data 1 Select the Viscosity 1 radio button The corresponding assay matrix appears 2 Inthe Viscosity Type drop down list above the assay matrix ensure Dynamic is selected 3 Inthe Viscosity Curves group select the Use Both radio button The Temperature field is for each of the two viscosity curves 4 Input the Viscosity 1 assay data as shown here This viscosity curve 5 6 corresponds to Temperature 1 100 E Figure 2 25 Input Data C Bulk Props C Light Ends Viscosity Type Dynamic x C Distillation C Molecular Wt Temperature fi 00 0 F C Density o Viscosity Assay Percent C Viscosity2 3 eeg Viscosity Curves C Use Curve 1 C Use Curve 2 Use Both Select the Viscosity 2 radio button Enter the assay data corresponding to Temperature 2 210 E as shown Figure 2 26 Assay Input Data Assay Percent Viscosity eee i ct 10 00 0 1000 30 00 0 3000 50 00 0 8000 70 00 7 500 90 00 122 3 lt empty gt The Assay is now completely defined based on our available data iG Click the Calculate butto
425. ssing Tutorial 16107 Processing Tutorial 1 107 1 3 2 Column Sizing In preparation for Dynamic operation the column and surrounding equipment must be sized In the steady state environment column pressure drop is user specified In dynamics it is calculated using dynamic hydraulic calculations Complications will arise in the transition from steady state to dynamics if the steady state pressure profile across the column is very different from that calculated by the dynamics pressure flow solver Column Tray Sizing 1 To access the Available Utilities property view do one of the following e Press CTRL U e From the Tools menu select Utilities 2 Scroll down the list of available utilities until the Tray Sizing utility is visible Figure 1 134 Available Utilities Ioj x Utility 1 Data Recon Utility Depressuring Dynamics Depressuring Original Derivative Utility Envelope Utility Hydrate Formation Utility Parametric Utility Pipe Sizing Property Balance Utility User Property Vessel Sizing View Utility Add Utility Delete Utility 1 107 1 108 Dynamic Simulation 3 Inthe list select Tray Sizing then click the Add Utility button The Tray Sizing view appears Tray Sizing Tray Sizing 1 OF x Select TS Design Name Tray Section a Tra Sizing 1 Setup ol S Setup Sections pecs Section Name Tray Internals tart Notes ctive tatus esign Limit imiting S
426. sssecccsseecceseeeseeeeeseaeees 8 3 2 4 Defining the Reaction ccccseseccneeeeecseseeceeeeecaeeeeeseeeensaes 17 3 2 5 Entering the Simulation Environment cccceeeeeeeeeeee 26 3 2 6 Using the Workbook aF fp cccccccscssececscsseeessceeeees 28 3 2 7 Installing Equipment on the PFD ccceeeeeeeseeeeeeeeeeeeees 46 3 2 8 Viewing eS _ _ ee se 66 3 3 Dynamic Simulation MN MMe re ccnnssccnnesccnnessccnnssccnnesseanes 76 3 3 1 Simplifying the Steady State Flowsheet ceeeeeeceeeeees 77 3 3 2 Using the Dynamics Assistant eeeeeeneeeeeeeneeeee nner eenn 78 3 3 3 Modeling a CSTR Open to the Atmosphere 000 82 3 3 4 Adding Controller Operations ccccceccseeeeeeeeeeeeeeeeeeeeeeaes 86 3 3 5 Monitoring in DYNAMICS ccccececcseeeeeceeeeeeeeeeecaeeeeesaeeeesaees 92 3 1 The complete case for this tutorial has been pre built and is located in the file TUTORS3 HSC in your HYSYS Samples directory Chemicals Tutorial 3 3 3 1 Introduction In this tutorial a flowsheet for the production of propylene glycol is presented Propylene oxide is combined with water to produce propylene glycol in a continuously stirred tank reactor CSTR The reactor outlet stream is then fed to a distillation tower where essentially all the glycol is recovered in the tower bottoms A flowsheet for this process appears below Ovhd
427. ssssscsssssseeeneccnnsnmeeeeeees R1 1 R2 P1 C1 C2 X1 R1 1 Process Description ccccscceeeseeseeeeeseseeeeenenseeensaaeeess R1 3 RLZ SOU cs eae a hate ett se od ete R1 6 R1 3 Steady State SIMUIAtION cc eesseeeeesseseseeseesnees R1 10 Ris RESUS antenna aria Saas angen a a R1 18 Sour Water Stripper ssccsssesccnsseenenneseenenseeeeeennnneeenns R2 1 R21 Process Descriptions essare R2 3 R22 MMOGUCUON airs ar R2 4 R23 OGU Deora a a a a A R2 4 R2 4 Steady State SiMulation ccccccsssseeceeeeeseeeeeeeeeseeeees R2 5 R2 RESUS nena N E NR R2 8 R26 CaSe Stuy em a a a satan R2 10 Propylene Propane Splitter scesscessssssceeeennnnnneenes P1 1 Pist Process Description teviedcevetineh incr Meta a utes P1 3 Pee OCUP E E NTA N P1 4 P1 3 Steady State SIMUIALION cceeeeeeeeeeeeeesseeeeeeeneeees P1 5 PITA WROSUILS cyiee tae ok ti ech ad aes eta Deen s P1 10 Ethanol Plantsoen aaan a C1 1 Gist Process DESCLIDUCIT ornan a denned C1 3 UGS POC UDe a A N C1 6 C1 3 Steady State SiIMUlAtION cee cceecseeeeeeeeeeseeseeeeeeeees C1 6 Ae RESUS rect Sete sgt A een tacgueete eee C1 13 Synthesis Gas Production csscsseecsseneenseneeeennneenenns C2 1 G2 1 Process DESCrOU ON secsi n C2 3 C22 OED a a ees C2 4 C23 Steady State Simulation senine C2 9 G24 TROSUMS s cetncti sac ie cee hehe sete con hele 5 etree esate a oes C2 16 Case Linkini sssrinin a aa a X1 1 X1 1 Proces
428. ssure psia 75 00 75 00 Std Ideal Lig Vol Flow barrel da h 6282 9 372e 004 Name A Material Steams P T Flow Compositions Energy Streams Unit Ops FeederBlock_Preheat Crude LJ Include Sub Flowsheets PreFlash L Show Name Only Number of Hidden Objects 13 Save your case by doing one of the following e Click the Save icon on the tool bar e Select Save from the File menu 2 55 PFD icon 2 56 Steady State Simulation c e d Using the PFD The PFD is the other main view used in HYSYS The PFD item appears in the HYSYS menu bar whenever the PFD is active To open the PFD click the PFD icon on the tool bar The PFD view should appear similar to the one shown below except some stream icons may overlap each other Figure 2 63 PFD toolbar Stream Operation labels PED Case Main a Material Hi W HI ki Rek D A 2 Default Colour Scheme x siream icon PreFlashap b Diesel Steam PreFlash Preheat Crude AGO Steam i Unit Operation icon for a PreFlashLig Separator z As a graphical representation of your flowsheet the PFD shows the connections among all streams and operations also known as objects Each object is represented by a symbol also known as an icon A stream icon is an arrow pointing in the direction of the flow while an operation icon is a graphic representing the actual physical operation
429. store the view to its original size Modifying the Coldbas Stream In this section you will change the temperature of stream ColdGas which determines the LTS temperature and view the changes in the process data table 1 Click the Navigator icon on the toolbar The Object Navigator view ir appears Navigator icon 2 Inthe Filter group select the Streams radio button Gas Processing Tutorial 85 Processing Tutorial 1 85 3 Inthe Streams list select ColdGas then click the View button The ColdGas property view appears Figure 1 111 Worksheet Conditions Vapour Phase Fraction Temperature F Properties Pressure psia Molar Flow MMSCFD Mass Flow Ib hr Mats Std Ideal Liq Vol Flow barrel day User Variables Molar Enthalpy Btu Ibmole 3 823e 004 Molar Entropy Btu lbmole F 33 423 Holst Heat Flow Btu hr 3e Cost Parameters Lig Yol Flow Std Cond barrel day lt empty gt Fluid Package Basis 1 Composition Worksheet Attachments Dynamics Define from Other Stream gt gt 4 Ensure that you are on the Worksheet tab Conditions page of the property view 5 Arrange the two views as shown below by clicking and dragging on their title bars Variable urine Caldas Vessel Temperature Vapour Phase Fraction 0 78182 SalesDP DewPaint I g Conditions Temperature F T n0000 SalesGas Sales Gas Productior i MMSCFD Prope
430. such as the number of stages The Numb of Stages field contains 10 default number of stages Note the following e These are theoretical stages as the HYSYS default stage efficiency is one e The Condenser and Reboiler are considered separate from the other stages and are not included in the Num of Stages field Chemicals Tutorial 3 For this example 10 theoretical stages are used so leave the Numb of Stages at its default value 4 Inthe Inlet Streams table click in the lt lt Stream gt gt cell From the drop down list of available inlet streams select Reactor Prods as the feed stream to the column HYSYS supplies a default feed location in the middle of the Tray Section TS in this case stage 5 indicated by 5_Main TS 6 Inthe Condenser group ensure the Partial radio button is selected as the column will have both Vapour and Liquid Overhead Outlets In the Column Name field change the name to Tower In the Condenser Energy Stream field type CondDuty then press ENTER 9 Inthe top Ovhd Outlets field type OvhdVap then press ENTER In the bottom Ovhd Outlets field type RecyProds then press ENTER 10 In the Reboiler Energy Stream field type RebDuty then press ENTER 11 In the Bottoms Liquid Outlet field type Glycol then press ENTER When you are finished the Next button becomes active indicating sufficient information has been supplied to advance to the next page of the Input Expe
431. t 10 In the Column Name field enter Atmos Tower 11 In the Bottoms Liquid Outlet field type Residue to create a new stream 12 In the Condenser Energy Stream field type Cond Duty to define a new stream Press ENTER The first page of the Input Expert should appear as shown below Figure 2 82 Ni Refluxed Absorber Column Input Expert Condenser Energy Stream Cond Duty 7 Parca jor Gas v C Total Column Name Atmos Tower Partial Ovhd Outlets C Full Rflg Naphtha r Optional Inlet Streams gt Tower Feed 26_Ma Trim Duty 28_ Ma 7 WasteH20 Bottom Stage Inlet lt lt Stream gt gt Bottom Steam n E A Bottoms Liquid Outlet Stage Numbering Residue E Top Down C Bottom Up Hia Next gt Connections page 1 of 4 Cancel Refining Tutorial Allstream attachments The Next button now becomes available indicating sufficient made on this page result in information has been supplied to advance to the next page of the Input the creation of Column sub Exp ert flowsheet streams with the same names For example when the Main Flowsheet stream BottomSteam was attached as a feed HYSYS on automatically created an Entering the Initial Estimate Values identical stream named BottomSteam to be used in the Column sub flowsheet 1 On the Pressure Profile page specify the following e Condenser Pressure 19 7 psia e Condenser Pressure Drop 9 psi e Bottom Stage Pressure 32
432. t in water is used as the absorbing medium The contactor consists of 20 real stages The rich amine is flashed from the contactor pressure of 1000 psia to 90 psia to release most of the absorbed hydrocarbon gas before it enters the lean rich amine exchanger In the lean rich exchanger the rich amine is heated to a regenerator feed temperature of 200 E The regenerator also consists of 20 real stages Acid gas is rejected from the regenerator at 120 F while the lean amine is produced at approximately 255 E The lean amine is cooled and recycled back to the contactor Figure G1 1 COOLER P 100 qm qm Q DEA TO PUMP zi A BE E 101 fam PUMP Q SVVEET GAS GAS TO CONTACTOR nek re WLIO To 100 CONTACTOR FLAS REGEN E 100FEED SPRDSHT 1 REGENERATOR REGEN BTTMS G4 Process Description Process Description Recommended amine strength ranges Lean Amine Strength in Water Wt MEA 15 20 DEA 29 35 TEA MDEA 35 50 Figure G1 3 To p Condenser ACID GAS COND Q qm Reflux Condenser J MainTS GAS TO CONTACTOR REGEN FEED Boilup Reboiler To Reboiler REGEN BTTMS There are three basic steps used in modeling this process 1 Setup The component list includes C1 through C7 as well as N2 CO2 H2S H20 and DEA 2 Steady State Simulation The case will consist of an absorber scrubbing the inlet gas using a DEA solution which will be regenerated in a distillation column Sweet gas
433. t select the Column T 100 operates in a left to right i manner the selected 4 Inthe Object Filter group select the UnitOps radio button The Flowsheet determines the Object list is filtered to show unit operations only Object list the chosen Object dictates the Variable 5 Inthe Object list select the Condenser The Variable list available for list and the selected the column appears to the right of the Object list variable determines a whether any Variable 6 In the Variable list select Liquid Percent Level Specifics are available Figure 2 176 ariable Navigator Flowsheet Variable Case Main AGO FC Boot height T 100 COL1 Cond LC Condenser Overall U Diesel FC Degree of Subcool Off Gas FC Distillate Mass Flow Object Filter Reb LC Distillate Molar Flow All 4GO_SS on Volume Flow Crests uty E Heavy Liquid Mass FI UnitOps Navigator Scope L Heavy Liquid Molar Fl Logicals Qi Kero_SS_Reb Heavy Liquid Yolume ColumnOps Main TS C Case PA_1_Cooler Liqui Pea s PA_2_Cooler i Custom Utility P _3_Cooler i i Custom Variable Description Liquid Percent Level Cancel 2 142 If you can t find an Object in the Variable Navigator view select the All radio button in the Object Filter group then select Case Main in the Flowsheet group All operations and streams for the design will appear in the Object list For more information about the Strip Chart setup refe
434. t Composition for Stream Feed 2 Composition Basis Mole Fractions C Mass Fractions C Liq Yolume Fractions C Mole Flows lt empty gt ss Mass Flows C Lig Volume Flows Composition Controls Erase Normalize Cancel 7 Change the Composition Basis to Mass Fractions by selecting the appropriate radio button or by pressing ALT N 8 Click on the compositional cell for Nitrogen type 6 for the number of parts of this component then press ENTER 9 Press the Down arrow key to move to the input cell for Methane as this stream has no CO2 10 Input the number of mass parts for the remaining components as shown in the following figure Press ENTER after typing each one Figure 1 32 Ni Input Composition for Stream Feed 2 Composition Basis 6 0000 amp Mole Fractions suet Mass Fractions 6 0000e 01 C Liq Volume Fractions 6 0000e 01 go 30000e 01 C Mass Flows C Lig Volume Flows Composition Controls Erase Normalize Cancel 1 29 Steady State Simulation 11 Click the Normalize button once you have entered the parts and HYSYS will convert your input to component mass fractions For CO2 the component you left lt empty gt the Mass Fraction was automatically forced to zero Figure 1 33 Total f 0000 12 Click the OK button to close the view and return to the stream property
435. t Sets re FieldT3 P Units neg Crone Formats HoverT extUnitSet1 HoverT extUnitS et2 Delete Unit Set Name Field density Mat D2 Display Units rel_to_air Btu lb F Ib ft3 g mL SG_60 60api SG_H2060nbs Simulation WYariables Reports Files All commands accessed via 12 Your new unit set is now defined Close the Session Preference view the toolbar are also available to return to the Simulation Basis Manager view as Menu items Steady State Simulation c e d BUUdINg the simulation Selecting Components Before defining a fluid package in HYSYS you will create a component list for the fluid package In this example the component list contains non oil components Light Ends and hypocomponents You must first add the non oil components and Light Ends from HYSYS pure component library into the component list 1 Click the Components tab then click the Add button The Component List View view appears Figure 2 9 Component List View Add Component Selected Components Components Available in the Component Library Components Match View Filters Traditional Electrolyte Hypothetical Other NRE Methane lt Substitute gt _Femove gt ahere n Hexane n Heptane Sort List n Octane n Nonane n Decane n C11 nCi2 C12 J Show Synonyms Cluster Sim Name C Full Name Synonym Formula a Selected Component by Type Delete Compone
436. t pressure and having HYSYS flash the new stream to calculate its dew point temperature To do this you will install a Balance operation Steady State Simulation F Balance icon Changes made to the vapour fraction temperature or pressure of stream SalesDP will not affect the rest of the flowsheet However changes which affect SalesGas will cause SalesDP to be re calculated because of the molar balance between these two streams 1 62 1 Double click the Balance icon on the Object Palette The property view for the new operation appears Figure 1 76 Name BaL Inlet Streams lt lt Stream gt gt lt lt Stream gt gt Connections l Connections Notes Connections Parameters Worksheet Stripchart User Variables Requires an inlet Steam Delete Ignored 2 Inthe Name field type DewPoint then press ENTER 3 Click in the lt lt Stream gt gt cell in the Inlet Streams table 4 Open the drop down list of available streams and select SalesGas Figure 1 77 DewPoint Connections Name D ewPoint Outlet Streams lt lt Stream gt gt Connections Notes Inlet Streams Connections Parameters Worksheet Stripchart User Variables Delete Ignored 5 Click in the lt lt Stream gt gt cell in the Outlet Streams table 6 Create the outlet stream by typing SalesDP then press ENTER 7 Click the Parameters tab
437. ta Tables Strip Charts a Variables Creating the Data Table In this section you will create a data table to display the variables 1 Click the Process Data Tables tab 2 Inthe Available Process Data Tables group click the Add button HYSYS creates a new table with the default name ProcDatal Figure 1 105 101x Available Process Data Tables _ Individual Process Data Selection ProcDatal View Process Data Table ProcDatal Variable __Lis Vessel Temperature D mee SalesDP DewPoint SalesGas Sales Gas Production Setup i _LiquidProd __ Liquid Production Add All Vatiables Invert All Yariables Remove All Variables o Variables Process Data Tables Strip Charts Data Recorder Case Studies 1 81 1 82 Steady State Simulation 3 Inthe Process Data Table field change the name to Key Variables The four variables that were added to the Databook appear in the table on this tab 4 Activate each variable by clicking on the corresponding Show checkbox Figure 1 106 Variable Show LTS Vessel Temperature v SalesDP DewPoint Vv _SalesGas _ Sales Gas Production IV LiquidProd Liquid Production M 5 Click the View button to view the Key Variables Data table which appears below Figure 1 107 Ni Key Yariables Data Variable Vessel Temperature SalesDP DewPoint SalesGas Sales Gas Productior MMS
438. tage a Liquid Draw 10 00 Use Tray Vapour to Size Ask Each Time x z Design Dynamics Delte TTT orori In the Name field change the name to DEPROP TS Click the Select TS button The Select Tray Section view appears In the Flowsheet group select DePropanizer In the Object group select Main TS Click the OK button Figure 1 136 Select Tray Section x Flowsheet Case Main DePropanizer COL1 Object Fiter All C Streams C UnitOps C Loagicals ColumnOps C Custom Uisconnest Cancel 1 108 Gas Processing Tutorial 1 109 Processing Tutorial 1 109 7 Inthe Setup Sections group click the Auto Section button The Auto Section Information view appears The default tray internal types appear as follows Auto Section Information Internal Type C Sieve Valve C BubbleCap Packed Area Tolerance When the ratio between the curent calc d area and either of min max previous areas for the 0 6000 section exceeds this tolerance a new diameter section is started Higher more sections lower fewer sections NFP Diam Factor When a new number of flow paths will result in a diameter diff gt diam fact old diameter a new 0 1 500 NFP section is started Not required for packed columns Lower more sections higher fewer sections Cancel 8 Keep the default values click Next The next view dis
439. tall a column using a pre built template HYSYS supplies certain default information such as the number of stages The current active field is Stages Number of Stages indicated by the thick border inside this field There are some other points worth noting e These are theoretical stages as the HYSYS default stage efficiency is one e If present the Condenser and Reboiler are considered separate from the other stages and are not included in the Stages field Entering Inlet Streams and Number of Trays For this example the main column has 29 theoretical stages 1 Enter 29 in the Stages field 2 Advance to the Optional Inlet Streams table by clicking on the lt lt Stream gt gt cell or by pressing TAB 2 67 Steady State Simulation 3 Click the down arrow J to open the drop down list of available feeds Figure 2 78 Condenser Energy Stream z Condenser r 4 C Total Column Name T 00 F K Partial Ovhd Outlets AR AT C Full Afls 1 Optional Inlet Streams eee ale Water Draw Stream T Inlet Stage vr 5 Optional Side Draws Stages r AGO Steam Stream Type Draw Stage Diesel Steam lt Stream gt gt Tower Feed Trim Dut i Bottoms Liquid Outlet Stage Numbering oo Top Down C BottomUp Pre hier Connections page 1 of 4 Cancel 4 Select Tower Feed as the feed stream to the column HYSYS supplies a default feed location in the middle of the Tray Section
440. te each variable by clicking on the corresponding Include checkbox Figure 1 109 ioi x Available Scenarios gt Data Recorder Data Selection Scenario 1 Record Current Scenario Scenario 1 j Variable Add _ Vessel Temperature M TEE __SalesDP DewPoint v SalesGas Sales Gas Production v LiquidProd Liquid Production y Variables Process Data T ables Strip Charts Data Recorder Case Studies 5 Click the Record button to record the variables in their current state ee The New Solved State view appears prompting you for the name of the new state OK 1 83 Steady State Simulation 6 Enter the new name Base Case then click OK You return to the Databook In the Available Display group select the Table radio button Click the View button The Data Recorder appears displaying the values of the key variables in their current state Figure 1 110 Data Recorder Main tate Base Case TS Temp F 0 0000 ew Point F 5 269 ales Gas Productio 7 018 iquid Production ba 479 7 a Scenario 1 Delete Table C Graph Re Number Now you can make the necessary flowsheet changes and these current values remain as a permanent record in the Data Recorder unless you choose to erase them 9 Click the Minimize button to reduce the Data Recorder to an icon 10 Click the Restore Up icon on the Key Variables Data view to re
441. tegrator view and change the Step Size to 0 2 sec on the General tab 7 Click the Options tab and make sure that the Singularity analysis before running checkbox is selected 8 Run the integrator for 2 minutes to ensure that the degrees of freedom for pressure flow specification is zero and all the vessels are sized Select Non Equilibrium Vapour when asked how you want to initialize V 101 Acid Gas Sweetening with DEA 01 6 2 Adding a Control Scheme The following Controllers will be used in the Dynamics model e Level e Temperature e Pressure e Flow Level Controllers Level Controller Name V100 LC Tab Page Liquid Percent Level Connections Process Object Process Variable Output Variable VLV FWKO Parameters Configuration PVmin 0 PVmax 100 Action Direct Mode Auto 50 V 100 O T Ti Tab Page Connections Process Object FLASH TK Process Variable Liquid Percent Level Output Variable VLV 101 G1 27 2B Dynamic Simulation Dynamic Simulation Level Controller Name LIC 100 Tab Page Connections V 101 Liquid Percent Level Output Variable MAKEUP H20 To size the Control Valve for the MAKEUPHZ2O stream select the Control Valve button Process Object Process Variable FCV for MAKEUP H20 Flow Type Mass Flow Min Available 0 0 lb hr Max Available 1200 lb hr PVmax 100 Action Reverse Mode Auto Ao A Oj U Ti Reb LC COL2 Tab Page Reboiler COL2 Liquid
442. the separator no Optional Heat Design Delta P Transfer information is Connections Yapour outlet psi 0 0000 requl red Parameters User Variables Notes Liquid Yolume Separator C 3Phase Sep C Tank Design Reactions Worksheet Dynamics Delete NS crore 14 To view the calculated outlet streams click the Worksheet tab This is a condensed Workbook displaying only those streams attached to the operation Figure 2 55 Worksheet Conditions Vapour Temperature F Properties Pressure psia Molar Flow Ibmole hr Mass Flow Ib hr 1 144e 006 1 080e 006 PF Specs Std Ideal Liq Vol Flow barel day 1 000e 005 9 372e 004 6282 Molar Enthalpy Btu Ibmole 1 998e 005 2 175e 005 8 049e 004 Molar Entropy Btu Ibmole F 266 0 288 8 112 4 Heat Flow Btu hr 7 619e 008 7 222e 008 3 967e 007 Composition lt ee Design Reactions Rating Worksheet Delte M iooi 2 50 Refining Tutorial 2 51 15 Now that the separator is completely known close the PreFlash view and the UnitOps view and return to the Workbook view The new separator appears on the Unit Ops tab Figure 2 56 Workbook Case Main Iof Xx Name Object Type inlet Outlet Ignored Calc Level PreFlashLig PreFlash Separator Preheat Crude E PreFlash ap View Unit0p Add Unit0p Delete Unit0p Material Stream
443. the LiquidProd than the Object Palette in the stream icon Move the LiquidProd stream to make room if required Parent Environment gt 46 Open the valve property view and specify the following connections Tab Page In this cell Enter Design Connections Reboil Valve 47 Close the valve property view 48 Click the Attach Mode icon then connect the LiquidExit stream to the liquid exit connection point of the Reboiler Exit the attach mode when you are done 49 Click the Run Column Solver icon in the tool bar The column will solve with the existing column specifications and the added valve To Ovhd Condenser a CondDuty Condenser Figure 1 132 TowerFeed Main TS Boilup Reboiler LiquidExit gt lt LiquidProd IQUIGEX qui ro To 4 Reboil Reboiler Valve 1 105 tT Enter Parent Simulation Environment icon When you delete a stream unit or logical operation from the flowsheet HYSYS will ask you to confirm the deletion Ensure that the Standard Windows file picker radio button is selected on the File tab in the Session Preferences view For more information on Session Preferences refer to Chapter 12 5 Files Tab in the User Guide 1 106 Dynamic Simulation Next you will delete unit operations that have no impact on the Dynamic solver 50 Return to the Main Flowsheet environment by clicking the Enter Parent Simulation Environm
444. the following e Access commands and features from the PFD tool bar e Open the property view for an object by double clicking on its icon e Move an object by clicking and dragging it to the new location e Access fly by summary information for an object by placing the cursor over it e Change an icon s size by clicking the Size Mode icon clicking on the icon you want to resize then clicking and dragging the sizing handles that appear Keep in mind that these are the HYSYS default colours you may change the colours in the Session Preferences The icons for all streams installed to this point are dark blue except for the Heat Exchanger shell side streams LTSVap and SalesGas and tube side outlet CoolGas Gas Processing Tutorial e Display the Object Inspection menu for an object by placing the cursor over it and right clicking This menu provides access to a number of commands associated with that particular object e Zoom in and out or display the entire flowsheet in the PFD window by clicking the zoom buttons at the bottom left of the PFD view Some of these functions will be illustrated here for more information refer to the User Guide Calculation Status Before proceeding you will examine a feature of the PFD which allows you to trace the calculation status of the objects in your flowsheet If you recall the status indicator at the bottom of the property view for a stream or operation displayed thr
445. the right of the SalesDP stream icon 4 Click to drop the Adjust icon onto the PFD A new ADJUST object appears with the default name ADJ 1 5 Click the Attach Mode icon on the PFD toolbar to enter Attach mode 6 Position the cursor over the left end of the ADJ 1 icon The connection point and pop up Adjusted Object appears 7 With the pop up visible left click and drag toward the ColdGas stream icon 1 94 Steady State Simulation 8 When the solid white box appears on the ColdGas stream release the mouse button The Select Adjusted Variable view appears Figure 1 121 Select Adjusted Variable ForADJ 1 Variable Cancel aS Std Ideal Lig Vol Flow Std Lig Yol Flow Spec User Variables Description Taoro cuca E At this point HYSYS knows that the ColdGas should be adjusted in some way to meet the required target An adjustable variable for the ColdGas must now be selected from the Select Adjusted Variable view 3 10 11 12 13 From the Variable list select Temperature Click the OK button Position the cursor over the right corner of the ADJ 1 icon The connection point and pop up Target Object appears With the pop up visible left click and drag toward the SalesDP stream icon When the solid white box appears at the cursor tip release the mouse button The Select Target Variable view appears Figure 1 122 Select Target Variable ForADJ 1 x Variable Dynamic P F
446. the variable selecting the Heating Value operation as the Object and NHV as the variable The Adjust operation performs automatic trial and error calculations until a target value is reached Adjust icon The current heating value of the sales gas is 1080 Btu scf Whenever flowsheet changes are made that result in the re calculation of the stream SalesGas the compositional changes will be automatically transferred to the Spreadsheet and the heating value updated accordingly 8 Click the Close button to continue with the study Installing an Adjust for Calculating the LTS Temperature Suppose the market price of your liquid product is currently unfavourable and you want to raise the LTS temperature to leave more of the heavier components in the gas phase This will increase the sales gas heating value resulting in a bonus from the transmission company The sales gas must however still comply with the dew point specification An Adjust operation can be used to adjust the temperature of the LTS ColdGas stream until the sales gas dew point is within a few degrees of the pipeline specification In effect this increases the gas heating value while still satisfying the dew point criteria Installing Connecting and Defining the Adjust 1 Click the PFD icon to display the PFD The Object Palette should also be visible if not press F4 Click the Adjust icon on the Object Palette Position the cursor on the PFD to
447. then click the View button The PFD menu option appears in the HYSYS menu bar whenever the PFD is active 1 49 SepVap 60 00 F 600 0 psia 8 976 MMSCFD Fly by Information ra Zoom Out 25 EJ Display Entire mi PFD Zoom In 25 Size Mode Icon Steady State Simulation Your PFD view should appear as shown in the figure below with all streams and unit operations visible If they are not all visible choose Auto Position All from the PFD menu HYSYS now displays all streams and operations arranging them in a logical manner Figure 1 62 PFD Case Main of X Hi il HI 4 neil p A p Default Colour Scheme x gt LTSVap epvap CoolGas PFD toolbar Gas Gas gt Feed InletSep SalesGas 1am MixerOut jE Material MIx 100 Stream Feed 2 Unit Operation icon for a Separator Stream Operation labels As a graphic representation of your flowsheet the PFD shows the connections among all streams and operations also known as objects Each object is represented by a symbol or icon A stream icon is an arrow pointing in the direction of flow while an operation icon is a graphic representation of the actual physical operation The object name or label appears near each icon Like any other non modal view the PFD view can be re sized by clicking and dragging anywhere on the outside border Other functions you can perform while the PFD is active include
448. ting Options Edit Assay Atleast 5 points are requied a Input Data Calculation Defaults Working Curves Corelations User Curves Delete Name Assay 1 Assay Was Not Calculated Calculate The next task is to enter the composition of the Light Ends in the Assay 3 From the Light Ends drop down list select Input Composition 4 Inthe Input Data group select the Light Ends radio button 5 Ensure that Liquid Volume is selected in the Light Ends Basis drop down list Click in the Composition cell for i Butane Type 0 19 then press the ENTER key You are automatically advanced down one cell to n Butane 2 21 2 22 Input Data C Bulk Props Light Ends C Distillation C Molecular Wt C Density C Viscosity1 C iscosity2 2 22 Steady State Simulation 8 Type the remaining compositions as shown The total Percent of Light Ends in Assay is calculated and displayed at the bottom of the table Figure 2 20 Ni Assay Assay 1 Pile ES Assay Definition Bulk Properties NotUsed Assay Data Type TBP v Light Ends Input Composition Molecular Wt Curve NotUsed ss J Density Curve NotUsed Viscosity Curves NotUsed ss J gt Distillation Conditions Atmospheric C Vacuum Light Ends Handling amp Bulk Fitting Options Input Data Light Ends Light Ends Basis Liquid Yolume 7 C Distillation T H20 Propane i Butane n Butane Pentane Pentane 0 460
449. tion are also presented in a step by step manner but are less detailed in their explanations They assume a rudimentary knowledge of the HYSYS interface and methods The three tutorials are grouped in three general areas of interest l Gas Processing 2 Refining 3 Chemicals Each area has an associated steady state and dynamic tutorial The dynamic tutorials use the steady state cases and add control schemes and dynamic specifications required to run the case in Dynamic mode If you are interested only in steady state simulation go through the steady state tutorial s that most interest you and stop at the dynamics section If you are interested only in learning to apply dynamic simulation methods use the pre built steady state base case included with HYSYS as the starting point for your dynamic tutorial case A 1 There are also several HYSYS training courses available Contact your Hyprotech agent for more information or visit the training page of our web site www hyprotech com The solved steady state cases are saved in the HYSYS Samples folder as TUTOR1 hsc TUTOR2 hsc and TUTOR3 hsc files For the dynamics tutorials you can use the pre built steady state cases as your starting point The solved dynamics cases are also included as dyntut1 hsc dyntut2 hsc and dyntut3 hsc A 2 a Introduction In the chapters that follow example problems are used to illustrate some of the basic concepts of building
450. tion case to run effectively Activate the following recommendations if required Page Recommendation Unit Operation OK Checkbox Misc Specs Set Equalize Option Mixers MIX 100 9 Click the Make Changes button once only All the active suggestions in the Dynamics Assistant are implemented Close the Dynamics Assistant view 10 Switch to Dynamic mode by pressing the Dynamic Mode icon When asked if you want to let the dynamics assistant evaluate your process before moving into dynamics click the No button Since the suggestion to insert a valve on the Reactor Vent stream was deactivated you must set a pressure specification on this stream 11 Double click the Reactor Vent stream icon in the PFD The property view appears 12 Click the Dynamics tab then select the Specs page 13 In the Pressure Specification group click in the Active checkbox to activate the specification 14 Close the Reactor Vent stream property view In order for the CSTR to operate in steady state and dynamic mode the vessel must be specified with a volume Since the Dynamic Assistant detected that a volume was already specified for the CSTR reactor it did not attempt to size it 15 The PFD for the dynamic tutorial before the addition of the controllers should look like the following figure Figure 3 108 Reactor P Oxid P it rop Oxide rop VL Prop Oxide 1 Oxide R t R al eactor eactor Reactor Prods VLY
451. tions Enter the Simulation Environment and enter the following unit operations Add Compressors Compressor Name K 100 Tab Page Inthis cell tern a K 101 TabtPag inthis cell tern Case Linking XG Linking X1 9 Add Heat Exchangers Heat Exchanger Name E 100 Tab Page inthis cele tern Design Parameters Heat Exchanger Model Exchanger Design End Point Tube Side Delta P 15 kPa Tab Pagel inthis els Design Connections hot100atm Shell Side Inlet wtr2 Shell Side Outlet wtr2b Design Parameters Heat Exchanger Model Exchanger Design End Point Tube Side Delta P 15 kPa Shell Side Delta P 15 kPa Worksheet Temperature 20 C Temperature 25 C renmen O X1 9 Creating a User Unit Operation Add a Tee Tee T 100 TaD Page inthis cels Me 4 Once you have completed specifying this flowsheet save the case as LinkCase2 hsc and close it X14 Creating a User Unit Operation Now that both cases have been created you can create the link between them 1 Open LinkCasel hsc 2 Adda User Unit Op to the flowsheet When you add a Unit Op HYSYS asks you for the type Click the Create Type button then type Case Linking in the input field and click the OK button Next you will define the User Unit Op Defining the User Unit Op involves writing two different subroutines e Initialize Defines material and energy feed product streams and creates user variables e Execute Opens
452. tions Target Object Source Object Natural Gas Parameters Multiplier Post Set SET 3 Teb inThisCell Enter Parameters Multiplier pofeet o E C2 10 This reactor is adiabatic so there is no energy stream and you do not have to specify the outlet temperature Synthesis Gas Production Installing the Reformer The Reformer is a conversion reactor in which most of the methane is reacted with steam to produce hydrogen carbon monoxide and carbon dioxide The outlet gas will also contain the unreacted methane and excess water vapour from the steam The overall conversion of the two reactions in the Reformer is 70 Rxn 1 which produces carbon monoxide and hydrogen has a conversion of 40 while Rxn 2 has a conversion rate of 30 The two reforming reactions are endothermic so heat must be supplied to the reactor to maintain the reactor temperature Specify the temperature of the outlet stream Combustor Feed at 1700 E so that HYSYS will calculate the required duty Install the reactor and define it as indicated below Conversion Reactor Reformer Tab Page inthis cell Enters Design Connections Inlets Liquid Outlet Reformer Liq CH 2H 5O gt CO 4H Installing the Combustor The Combustor is the second conversion reactor The feed streams for the Combustor include the Reformer product Air stream and Comb Steam streams The air stream is the source of the nitrogen for the re
453. tom of the Cut Input Information group the Straight Run radio button is selected and HYSYS provides default TBP cut point temperatures for each Straight Run product The Cut Distributions table shows the Fraction of each product in the Blend Since Liquid Vol is the current Basis in the Table Control group the products are listed according to liquid volume fraction These fractions can be used to estimate the product flow rates for the fractionation column For example the Kerosene liquid volume fraction is 0 129 With 100 000 bbl day of crude feeding the tower the Kerosene production is expected at 100 000 0 129 12 900 or roughly 13 000 bbl day If you want you can investigate other reporting and plotting options by selecting another Table Type or by viewing information on the other tabs in the Blend property view 2 When you are finished close the Blend view to return to the Oil Characterization view Now that the Blend has been calculated the next task is to install the oil Installing the Oil The last step in the oil characterization procedure is to install the oil which accomplishes the following e The petroleum hypocomponents are added to the fluid package e The calculated Light Ends and Oil composition are transferred to a material stream for use in the simulation 1 On the Oil Characterization view click the Install Oil tab 2 Inthe Stream Name column click in the top blank cell 2 33 2 33 a L
454. tor Prods which determines the Reactor temperature then view the changes in the process data table aA 28 Click the Navigator icon in the toolbar 29 In the Filter group select the Streams radio button pavieien ican 30 In the Streams list select Reactor Prods then click the View button The Reactor Prods property view appears 31 Ensure you are on the Worksheet tab Conditions page of the property view 3 73 Steady State Simulation 32 Arrange the Reactor Prods and Key Variables Data views so you can see them both Figure 3 100 ioi iol Worksheet Reactor Prods iat Reactor emp 140 0 F aa Vapour Phase Fraction 0 00000 Coolant CoolingDuty 4 520e 006 Btuhr iz Conditions Tem aa perature F 140 00 Glycol GlycolProduction 713 4 barrel day Properties Pee asl 16 166 4 f G eee Molar Flow lbmole hr 618 55 position ee eee Mass Flow lb hr 19712 ___ View DataBook K Value Std Ideal Lig Vol Flow USGPM 38 749 User Variables Molar Enthalpy Btu Ibmole 1 409e 005 Molar Entropy Btu lbmole F 3 8453 Notes Heat Flow Btu hr B 7137e 07 Cost Parameters Liq Vol Flow Std Cond barel day 1415 5 Fluid Package Basis 1 gt Worksheet eee 5 oe Define from Other Stream e Dynamics Currently the Reactor temperature is 140 E The key variables will be checked at 180 E 33 In th
455. torial 6 Specify the following e Vapour Rate 0 e Reflux Ratio 1 0 Figure 2 85 Ni Refluxed Absorber Column Input Expert Vapour Rate 0 0000 Liguid Rate Reflux Ratio Flow Basis lt Prev Done Side Ops gt Specifications page 4 of 4 Cancel 7 Click the Done button The Column property view appears Figure 2 86 Column Atmos Tower COL1 Fluid Pkg Basis 1 Peng Robinson Desian Column Name Atmos Tower Sub Flowsheet Tag COL Condenser 2 E Total Partial Full Reflux Connections RAS Condenser Energy Stream Cond Duty Delta P Dff Gas Specs 9 000 psi Overhead Outlets Specs Summary Napra gt Subcooling Notes Optional Inlet Streams 5 x Optional Side Draws Tower Feed por A Type Draw Stage Trim Duty 28_Ma WasteH20 W ndenser lt Stream gt gt Bottom Stage Inlet Bottom Steam 32 70 psia Stage Numbering TopDown Bottom Up Bottoms Liguid Outlet R esidue z Edit Trays m E Design Parameters Side Ops Rating Worksheet Performance Flowsheet Reactions Dynamics Delete Column Environment Run Reset Unconverged J Update Outlets Ignored 2 3 The basic column has three available degrees of freedom Currently two Specifications are Active so the overall Degrees of Freedom is one The number of available degrees of freedom increases with the addition of side equipment T
456. tput Target Object VLV Water Feed Parameters Configuration 11 Click the Face Plate button Change the controller mode to Auto and input a set point of 11 000 lb hr 12 Close the WaterFeed FC face plate view and property view Temperature Control Next you will install temperature controller to control the temperature of the CSTR reactor The control will be implemented using an energy utility stream 1 Inthe Object sub palette click the PID Controller icon then click in the PFD above and to the left of the Reactor icon The controller icon appears This controller will serve as the Reactor temperature controller 3 89 3 90 3 90 Dynamic Simulation 2 Double click the controller icon then specify the following details Tab Page In this cell Enter Connections Reactor TC Process Variable Source Reactor Vessel Temperature Parameters Configuration eoo s wooo o e 3 Click the Control Valve button The FCV for Coolant view appears Figure 3 117 Nil FCV For Coolant Eel x Control Attachments ines sepa tes Attached Stream Reactor f Attached Controller Reactor TC Direct O Attached Operations Reactor lt empty gt Min Available lt empty gt Max Available lt Infinite gt Duty Source Direct 0 C From Utility Fluid Iv Available to Controller 4 Inthe Duty Source group select the Direct Q radio button 5 Inthe Direct Q group table enter the following
457. tropic ethanol products Ce Synthesis Gas Production Steady State Modeling Reaction Manager Reactors Synthesis gas H N on a 3 1 basis is the necessary feedstock for an ammonia plant The traditional process for creating synthesis gas is explored in this example Air steam and natural gas are fed to a series of reactors which produces a stoichiomtrically correct product Extensive use of HYSYS s Reaction Manager is illustrated as four individual reactions are grouped into three reaction sets that are used in five different reactors This example also demonstrates the use of an Adjust operation to control a reactor outlet temperature The case is then converted to a dynamics simulation by adding valves and assigning pressure flow specifications on the boundary streams Reactors are sized using the actual gas flow and the residence time A spreadsheet operation imports the H N molar ratio to a ratio controller controlling the Air flowrate Temperature controllers are used to achieve the reactors setpoint by manipulating the duty streams B 3 aa B 4 HYSYS Extensibility XI Case Linking Steady State Modeling This case explores the use of the User Unit Operation to link two HYSYS simulation cases such that the changes made to the first case are automatically and transparently propagated to the second case Within each User Unit Op two Visual Basic macros are used The Initialize macro sets the field names for the various
458. tus As String Dim LinkCase As Object Set LinkCase ActiveObject GetUserVariable LinkCase Dim LinkStream As Object This UV will hold the Linked stream name Set LinkStream ActiveObject GetUserVariable LinkStream Dim myFeeds As Object Set myFeeds ActiveObject Feedsl if myFeeds Count lt gt 1 Then Exit Sub end if Dim Case2 As Object Set Case2 GetObject LinkCase Variable Value Dim Case2FS As Object Set Case2FS Case2 Flowsheet Dim CaselFS As Object Set CaselFS ActiveObject Flowsheet Dim Case2Strm As Object Set Case2Strm Case2FS MaterialStreams Item CStr LinkSt ream Variable Value Dim CaselStrm As Object Set CaselStrm myFeeds Item 0 Case2Strm TemperatureValue CaselStrm TemperatureValue Case2Strm PressureValue CaselStrm PressureValue Explanation Signifies the Start of the operation execution subroutine You do not have to add this line as it should already be there If an error occurs during the execution of this subroutine go to the line of code designated EarlyGrave Connects the variables LinkCase and LinkStream to their corresponding user variables If the number of streams specified in the Feed list is not 1 then exit the subroutine Creates a reference to the LinkCase user variable called Case2 Creates a reference to the flowsheet inside Case2 LinkCase called Case2FS Creates a reference to the current flowsheet called Case1FS Cre
459. u hr B Material Streams Energy Streams Unit Ops ProductBlock_Preheat C C Include Sub Flowsheets FeederBlock_Preheat Cr L Show Name Only Number of Hidden Objects 0 Optional Info Preheat Crude Unknown Compositions Optional Info Preheat Crude Unknown Temperature 2 37 2 38 You can toggle the palette open or closed by pressing F4 or by selecting Open Close Object Palette from the Flowsheet menu 2 38 Steady State Simulation There are several things to note about the Main Simulation Environment In the upper right corner the Environment has changed from Basis to Case Main A number of new items are now available on the menu and toolbar and the Workbook and Object Palette are open on the Desktop These latter two objects are described below Objects Description Workbook A multiple tab view containing information regarding the objects streams and unit operations in the simulation case By default the Workbook has four tabs namely Material Streams Compositions Energy Streams and Unit Ops You can edit the Workbook by adding or deleting tabs and changing the information displayed on any tab Object Palette A floating palette of buttons which can be used to add streams and unit operations Also notice that the name of the stream Preheat Crude you created during the Oil characterization procedure appears in the Workbook and the white Object Status window at the very botto
460. ue Specification Description Heat Balance The tube side and shell side duties must be equal so the heat balance must be zero 0 This is the product of the overall heat transfer coefficient U and the area available for heat exchange A HYSYS does not provide a default UA value so it is unknown at this point It will be calculated by HYSYS when another constraint is provided Adding a Heat Exchanger Specification To exhaust the remaining degree of freedom a 10 F minimum temperature approach to the hot side inlet of the exchanger will be specified 1 Inthe Specifications group click the Add button The ExchSpec Exchanger Specification view appears 2 Inthe Name cell change the name to Hot Side Approach The default specification in the Type cell is Delta Temp which allows you to specify a temperature difference between two streams The Stream and Stream cells correspond to the warmer and cooler streams respectively 3 Inthe Stream cell select SepVap from the drop down list 4 Inthe Stream cell select SalesGas from the drop down list In the Spec Value cell enter 10 F The view should appear as shown in the following figure Figure 1 72 Si Hot Side Approach Bi E3 Hot Side Approach Delta Temp Sevap SalesGas B Parameters Summary Delete Steady State Simulation HYSYS will converge on both specifications and the unknown streams will be flashed 6 Click the Clo
461. um vapour phase slightly warmer than the vessel Alternatively the liquid level can be set to 100 but this can cause difficulties starting simulation RECOMMENDATION Increase temperature Non E quilibrium Yapour 100 Liquid HYSYS recommends that you increase the temperature setting to create a vapour phase You can also create a non equilibrium vapour phase or set the liquid level to be 100 For the sake of this example select the default recommendation 19 Click the Increase Temperature button 20 Let the integrator run for few minutes so all the values can propagate through the column Observe the value changes on the face plate view 21 To stop the integrator click the Stop Integrator icon 2 141 Dynamic Simulation 2 5 5 Monitoring in Dunamics Now that the model is ready to run in dynamic mode the next step is to install a strip chart to monitor the general trends of key variables The following is a general procedure for installing strip charts in HYSYS 1 Open the Databook by using the hot key combination CTRL D Figure 2 175 DataBook Available Data Entries Object Variable Insert o Variables Process Data Tables Strip Charts Data Recorder Case Studies The Variable Navigator is 2 On the Variables tab click the Insert button The Variable Navigator used extensively in HYSYS for locating and selecting VIEW appears variables The Navigator 3 In the Flowsheet lis
462. umn Reboil Ratio Spec lt empty gt Column Recovery Components lt lt Component gt gt Column Reflux Feed Ratio Spec i p Column Reflux Fraction Spec Column Reflux Ratio Column Tee Split Spec Column Temperature Target Type Stream Stage Column Transport Properties Spec p s Column User Property Spec Parameters Spec Type Column Vapour Flow Column Yapour Fraction Spec Column Yapour Pressure Spec Add Spec s 6 Inthe Name cell change the specification name to Propane Fraction 1 70 Gas Processing Tutorial 1 71 7 Inthe Stage cell choose Reboiler from the drop down list of available stages Figure 1 89 X Comp Frac Spec Propane Fract Fill Eg Propane Fraction Components Target Type Stream Stage Parameters Spec Type Delete 8 Inthe Spec Value cell enter 0 02 as the liquid mole fraction specification value 9 Click in the first cell lt lt Component gt gt in the Components table and select Propane from the drop down list of available components Figure 1 90 Ni Comp Frac Spec Propane Fract BG EG Propane Fraction tage Reboiler Flow Basis hase _ Liquid 2 000e 002 Components Propane Target Type C Stream Stage Parameters Summary 10 Close this view to return to the Column property view HYSYS automatically made The new specification appears in the Column Specifications list on the the new specific
463. ure Flow or Pressure Drop DeltaP specification Tell me why Typically all unit operations in E Dynamic mode should use the etei izes J Tray sections Jer J Pressure Flow specification A mE Cancel 5 Ensure that all the recommendations in this page are active Tab Page Recommendation Unit Operation OK Checkbox Pressure Flow Pressure Flow Spec Chiller Specs instead of Delta P PF versus DP 1 115 1 116 Dynamic Simulation 6 Click the Unknown Sizes tab The Unknown Sizes tab Figure 1 145 contains a list of the unit operations in the flowsheet O Denamics Assistant that require sizing e The Valve operati ons Sizing These items have unknown volumes Use the volumes listed below are sized based on the Valves Gas Gas Gas Gas current flow rate and Volumes Cooler Heat Exchanc Heat Exchanc pressure drop across k values 5 0 7 1 5 2 the valve The valves are Volume Ra TSE TT GT k i sized with a 50 valve Flow berrel day 2876e 004 3060e 004 2232e 004 opening Residence time 000 00 10 00 000 00 10 00 000 00 10 00 e The Vessel operation volumes are determined based on the liquid exit volumetric flow rate and a 10 second residence time e The Heat Exchanger operations are sized Quick size Teme wh based on the current flow rate and pressure drop across the Serre i l Cancel equipment General Streams Pressure Flow Specs Unknown Sizes Tray sections
464. ure profile across the column Figure 2 159 Profiles Optional Estimates C Molar C Mass Volume Pressure Temp Net Liquid Net Vapour a L Stagg kP C 3 h m 3 m Pressure ws Tray Number 107 6 3 154e 00 Flow Basis M w Fa aa ag J co ae t t 26 Record the top stage pressure 1_Main TS Calculate the theoretical bottom stage pressure as follows Bottom Stage Pressure Top Stage Pressure Total Section Pressure Drop 2 1 Variable Value Top Stage Pressure 197 9 kPa Total Section pressure drop 23 66 kPa Bottom Stage Pressure 221 56 kPa 27 In the Pressure column of the Profiles group specify a bottom stage pressure 29_Main TS of 221 56 kPa Figure 2 160 Pressure Temp ee eee 27 26__Main TS 219 0 7_MainTS 28 2199 8 _ManTS 29 220 7 3 M nTS 30 221 6 r A NAL 2 124 Run Column Solver icon Refining Tutorial 28 Converge the Column sub flowsheet by clicking the Run Column Solver icon in the tool bar 29 Close the Column property view Side Stripper Tray Sizing In this section you will size the following side stripper operations using the tray sizing utility as described in the Column Tray Sizing section e Kero SS e Diesel SS e AGO SS 1 From the Tools menu select Utilities The Utilities property view appears Double click on the Tray Sizing utility The Tray Sizing vie
465. utton The UnitOps view appears listing all available unit operations When you click the Add Figure 1 40 button or press the ENTER key inside this view HYSYS adds the operation that is UnitOps Case Main currently selected araa ppan All Unit Ops j Vessels l Cancel b You can also double click an operation to install it Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling Reactors Prebuilt Columns Short Cut Columns Sub Flowsheets Logicals Extensions User Ops Electrolyte Equipment Refinery Ops EEEE EEEE EEE Column Sub Flowsheet 4 Select Mixer by doing one of the following e Start typing mixer e Press the Down arrow key to scroll down the list of available operations to Mixer e Scroll down the list using the vertical scroll bar and click on Mixer 5 With Mixer selected click the Add button or press the ENTER key You can also use the filters to find and add an operation e For the Mixer operation select the Piping Equipment radio button under Categories A filtered list appears in the Available Unit Operations group e Double click the Mixer operation to install it The Mixer property view appears Figure 1 41 gt MIX 100 Design Name Mix 1 00 Connections Parameters User Variables Notes Inlets Outlet lt lt Stream gt gt Fluid Package i Basis 1 Design Rating Worksheet Dynamics 1 35 1
466. utton and the bulk property table appears to the right of the radio buttons 2 Clickin the Molecular Weight cell in the table Type 300 and press ENTER You are automatically advanced down one cell to the Standard Density cell 3 In the Standard Density cell enter 48 75 and press SPACE BAR To the right of the cell a field containing the current default unit associated with the cell appears When you defined the new unit set you specified the default unit for standard density as API_60 which appears in the field Figure 2 21 Ni Assay Assay 1 Assay Definition Input Data Molecular Weight 3000 Bulk Properties Used x f Bulk Props Standard Density 4875 API 60 Light Ends Watson UOPK Gda o E Bal TI C Distiation Dynamic Light Ends Input Composition x Molecular Wt 100 0 F C Density lt empty gt Molecular Wt Curve Dependent z E Viscosiyt 210 0 F Viscosity2 lt empty gt Density Curve Independent v Viscosity Curves Independent bd TBP Distillation Conditions Atmospheric C Vacuum Light Ends Handling amp Bulk Fitting Options a Input Data Calculation Defaults Working Curves Correlations User Curves Delete Name Assay 1 Assay Was Not Calculated Calculate 4 Since this is the correct unit press ENTER and HYSYS accepts the density value 2 23 2 24 2 24 Steady State Simulation No bulk Watson UOPK or Viscosity data is available for this as
467. view HYSYS has performed a flash calculation to determine the unknown properties of Feed 2 as shown by the status indicator displaying OK Figure 1 34 Feed 2 Worksheet action 0 020000 Conditions 0 000000 0 400000 Properties aod Composition 0 200000 K Value 0 080000 User Variables Notes gt Cost Parameters Tota 1 00000 i Edit Properties Basis a Worksheet Attachments Dynamics KR Delete Define from Other Stream lt a gt To view the properties of each phase use the horizontal scroll bar in the table on the property view or drag and expand the window to view all property columns 1 30 r Sizing Arrow Cursor Stream Feed 2 Fa Compositional Basis Mole Fractions Liquid YVolume Fractions C Mole Flows Mass Flows C Liquid Volume Flows To expand the property view move your cursor over the right border of the view The cursor becomes a sizing arrow With the arrow visible click and drag to the right until the horizontal scroll bar disappears leaving the entire table visible The compositions currently appear in Mass Fraction To change this click the Basis button then select another Compositional Basis radio button in the view that appears To view the calculated stream properties click the Conditions page New or updated information is automatically and instantly transferred among all locations in HYSYS
468. w Yapour Fraction 0 0000 0 0000 0 0000 0 0000 0 0000 0 0000 Temperature F 315 9 142 5 612 1 367 4 615 4 485 0 Pressure psia 28 84 28 84 30 99 30 99 31 70 31 70 Molar Flow Ibmole hr 4716 4716 1790 1790 1414 1414 Mass Flow lb hr 5 740e 005 5 740e 005 3 765e 005 3 765e 005 3 928e 005 3 928e 005 Liquid Yolume Flow barrel day 5 000e 004 5 000e 004 3 000e 004 3 000e 004 3 000e 004 3 000e 004 Heat Flow Btu hr 4 697e 008 5 247e 008 2 596e 008 2 946e 008 2 433e 008 2 783e 008 l R1 19 RAD Rests 20 Results R1 20 Sour Water Stripper R2 1 He Sour Water Stripper 2 1 Process Description si oecstiecs cadeedesiceceai aaa aaa ean 3 2 2 INTPOGUCTION sneu aaa winters decd 4 R2 3 Setup 1 cccccnnsssees anette AI eee ennageicennssssecennssssnensssssess 4 R2 4 Steady State Simulation cccceseeeseeeeeeesseeeeeeeseeseceeseeeseenseeeses 5 R2 4 1 Installing the SW Stripper cc eeeccesseeeeeeseeeeeeeeeeeeeeeeaees 5 R25 BRPSUITS cinccccntecennne ds E 8 R256 Case Study iii a an MMM ensssssccnnssscccnssssscensssssees 10 R2 6 1 Resule aaaeeeaa 12 R2 1 R2 2 Sour Water R2 2 To see this case completely solved see your HYSYS Samples directory and open the R 2 hsc file Sour Water Stripper R2 3 Re Process Description Figure R2 1 Stripper Face Bottoms oW Stripper Stripper Bottoms The sour water
469. w appears In the Name field change the name to Kero_SS TS Click the Select TS button The Select Tray Section view appears From the Flowsheet list select T 100 then select Kero_SS from the Object list Click the OK button Click the AutoSection button The AutoSection view appears Click the Next button Click the Complete AutoSection button to calculate the Kero_SS TS tray sizing parameters oS 2S 9 Record the following tray section parameters available on the Performance tab in the Results page Variable Kero SS Section Diameter 1 676 m Weir Height 0 0508 m 10 Close the Kero_SS TS tray sizing utility 11 Repeat steps 2 8 to size the Diesel_SS and AGO_SS side strippers 2 125 2 126 Dynamic Simulation 12 Click the Performance tab select the Results page then confirm that the following tray section parameters match the table below Variable Diesel SS AGO SS 1 AGO SS2 Section Diameter 1 676 m 0 9144 m 0 6096 m Weir Height 0 0508 m 0 0508 m 0 0508 m The pressure drop rating information found in the side stripper tray sizing utilities is not used to specify the pressure profile of the Side Stripper unit operations Since there are only three trays in each side stripper the pressure drop across the respective tray sections is small Keeping the pressure profile across the side strippers constant does not greatly impact the transition from steady state mode to dynamics 13 Close the Availa
470. w appears in the Databook Figure 3 91 DataBook Available Data Entries Object Variable Reactor Temp EF Variables Process Data Tables Strip Charts Data Recorder Case Studies 8 To add the next variable click the Insert button The Variable Navigator appears 9 In the Object Filter group select the Streams radio button The Object list is filtered to show streams only 10 In the Object list select Coolant in the Object list The variables available for this stream appear in the Variable list 3 69 Steady State Simulation 11 In the Variable list select Heat Flow Figure 3 92 Yariable Navigator Flowsheet Case Main Tower COL1 Object Filter C All Streams C UnitOps Navigator Scope ili C Logicals Utility maximum flow ral C ColumnO Flowsheet litu mini eee F Cass Water Feed Utility minimum flow rate Custom Utility Qutlet Temp Basis Custom Utility Esm Variable Description Cooling Duty Cancel 12 In the Variable Description field change the description to Cooling Duty then click the OK button The variable now appears in the Databook 13 Click the Insert button again In the Object list select Glycol In the Variable list select Liq Vol Flow Std Cond Change the Variable Description for this variable to Glycol Production then click the OK button The completed Variables tab of the Databook appears below Figure 3 93 DataB
471. will add the following components N2 CO2 Cl C2 C3 iC4 and nC4 First you will add nitrogen using the match feature 3 Ensure the FullName Synonym radio button is selected and the Show Synonyms checkbox is checked Move to the Match field by clicking on the field or by pressing ALT M Type NITROGEN HYSYS will filter as you type displaying only those components that match your input Figure 1 13 Components Available in the Component Library Match Nitrogen View Filters C Sim Name C Formula Nitrogen Nitrogen Nitrogen 2 V Show Synonyms Cluster 6 With Nitrogen selected add it to the Current Composition List by doing one of the following e Press the ENTER key e Click the Add Pure button e Double click on Nitrogen note that Nitrogen need not be highlighted for this option In addition to the Match criteria radio buttons you can also use the Filters view to display only those components belonging to certain families Next you will add CO2 to the component list using the filter feature 7 Ensure the Match cell is empty by pressing ALT M and DELETE 1 14 Steady State Simulation 8 Click the View Filters button The Filters view appears as shown in the following Figure 1 14 Component List View 7 Property Package Filter Selected Components Components Available in the Component Librar Add Component P P z _ Recommended Only E Components Match fo 0 View Filters Tra
472. wsheet streams when external streams are deleted Property Correlations Trace Window V Confirm Before Adding if Active Correlations are Present Simulation Variables Reports Resources Extensions Oillnput Tray Sizing Save Preference Set Load Preference Set x 7 Close the Session Preferences view along with all the open views on the HYSYS desktop except for the PFD view by clicking the Close Close icon icon in the top right corner of each view 1 100 Gas Processing Tutorial 1 401 Processing Tutorial 1 101 In the PFD the stream pressure for Feed 2 will be deleted so that it will be calculated by the MIX 100 in dynamic mode 8 Double click the Feed 2 stream icon to open its property view 9 On the Conditions page of the Worksheet tab click in the Pressure cell then press DELETE to remove the stream pressure 10 Close the stream property view Next you will change the pressure setting for the MIX 100 so that the whole PFD can be simulated 11 Double click the MIX 100 icon to open its property view 12 On the Design tab select the Parameters page 13 In the Automatic Pressure Assignment group click the Equalize All radio button 14 Close the MIX 100 property view Next you will insert a valve operation between the SepLigq stream and the MIX 101 unit operation T H i l 16 Break the SepLiq stream by doing the following Break Connection icon 15 Click the Break Conn
473. y 10 Activate the following recommendations Tab Page Recommendation Unit Operation OK Checkbox Equalize Option Mixer 101 Active Mixers 11 Click the Make Changes button once All the active suggestions in the Dynamics Assistant are implemented 12 Close the Dynamics Assistant view 13 Switch to Dynamic mode by clicking the Dynamic mode icon When asked Are you sure you want to switch to dynamics click the Yes Dynamic Mode icon button Since you deactivated the suggestion to insert a valve on the Ovhd stream you must set a pressure flow specification on this stream You can enter the Ovhd stream pressure specification in either the Main Flowsheet environment or the Column Sub Flowsheet 14 In the PFD double click the Ovhd stream icon to open stream property view 15 Click the Dynamics tab then select the Specs page 1 117 1 118 Dynamic Simulation 16 Activate the Pressure specification The Pressure specification should be the only specification active Ensure that the Ovhd Molar Flow specification is inactive Figure 1 147 Dynamic Specifications Dynamics Pressure Specification Stich tripchart 202 6 psiaf M Specs Flow Specification Molar Mass IdealLigvol Std Lig ol Molar Flow 244 3 Ibmole hr E Product block Worksheet Attachments Dynamics Delete Define from Other Stream lt a
474. y as a Cooler enough heavier hydrocarbons condense such that the eventual sales gas meets a pipeline dew point specification The cold stream is then separated in a low temperature separator LTS The dry cold gas is fed to the gas gas exchanger and then to sales while the condensed liquids are mixed with free liquids from the inlet separator These liquids are processed in a depropanizer column to produce a low propane content bottoms product Gas Processing Tutorial 1 5 Once the results for the simulation have been obtained you will have a good understanding of the basic tools used to build a HYSYS simulation case At that point you can either proceed with the Optional Study presented at the end of the tutorial or begin building your own simulations In this tutorial three logical operations will be installed in order to perform certain functions that cannot be handled by standard physical unit operations Logical Flowsheet Function Balance To duplicate the composition of the SalesGas stream in order to calculate its dew point temperature at pipeline specification pressure To determine the required LTS temperature which gives a specified SalesGas dew point HYSYS Spreadsheet To calculate the SalesGas net heating value The Balance operation will be installed in the main example In the Optional Study section the Adjust and Spreadsheet operations will be installed to investigate the effect of the LTS temperature on the sa
475. y gt gt Main TS Return Temp lt empty gt Flow Rate lt empty gt 5 500e 007 Bt Delete PA_1 The remainder of the information on the above view is calculated by the Column solver 11 Click the Close icon on the main Pump Around view to return to the Column property view 12 Repeat the previous steps to install the two remaining pump arounds Enter Rate specifications of 3e4 barrel day and Duty specifications of 3 5e7 Btu hr for both of these pump arounds Specify the Return Stage and Draw Stage Click the Install button The second view The completed Pump Around views and Liquid Pump Around Summary appears l table appear in the following figures Specify the 1st Active spec Double click the empty Figure 2 99 cell in the 2nd Active spec Pump Around PA_2 ox See Pel ES Select Duty from the Spec Type drop down list st Active 2nd Active Spec P _ 2 Rate Pa P 2 Duty Pa 3 500e 007 Btu hr Return Stage Ist Active 2nd Active Spec PA amp _3 Rate Pal PA 3 Duty Pa 3 500e 00 Btushr Enter the Spec Value Retum Stage 8 Close the view 16_ Main TS Draw Stage 17_Main i Delete PA 2 Calculated Information lt empty gt Return Temp lt empty gt Flow Rate lt empty gt 3 500e 007 Bt vw valve 21_ Main TS Draw Stage 22_Main T x Delete PA_3 Calculated Information lt empty gt Return
476. y section types are necessary Figure 2 157 Setup Sections Section Name Section_1 Section_2 1_ Main TS 28_ Main TS 27_ Main TS 29__Main TS Valve Valve Design Design Complete Complete DC Backup Weir Loading 1_ Main TS 28 Main TS 11 Click the Design tab then select the Specs page 12 Inthe Number of Flow Paths cell enter 3 for both Section_1 and Section_2 13 Click the Performance tab then select the Results page to see the dimensions and configuration of the trays for Section_1 and Section_2 Since Section_1 is sized as having the largest tray diameter its tray section parameters should be recorded 14 Confirm the following tray section parameters for Section_1 Variable Value Section Diameter 5 639 m Weir Height 0 0508 m Tray Spacing 0 6096 m Total Weir Length 13 31 m The number of flow paths for the vapour is 3 The Actual Weir length is therefore the Total Weir Length recorded 3 15 Calculate the Actual Weir length Variable Value Actual Weir Length Total Weir Length 3 Refining Tutorial 16 Confirm the Maximum Pressure Drop Tray and check the number of trays in the Main TS column The Total Section Pressure drop is calculated by multiplying the number of trays by the Maximum Pressure Drop Tray VEUF Lol Value Maximum Pressure Drop Tray 0 831 kPa Number of Trays 29 Section DeltaP 24 10 kPa 17 Close the Tray Sizing Main TS and Available Utilities
477. you want to delete the object click the Yes button If not click the No button Items to be deleted Material Streams Energy Streams Unit Operations Hot Crude Crude Duty Pre Flash Separator Pre Fish Liq Crude Heater Pre Flsh Vap Mixer Raw Crude After you delete the above items stream Atm Feed is not fully specified 16 Double click the Atm Feed stream icon to open its property view 17 Click the Define from other Stream button The Spec Stream As property view appears 18 In the Available Streams group select Store then click OK Figure 2 151 Atm Feed q Make sure that the Standard Windows file picker radio button is selected on the File page in the Session Preferences view For more information on Session Preferences please refer to Chapter 12 5 Files Tab in the User Manual 2 118 Worksheet Conditions Properties Composition K Value User Variables Notes Cost Parameters a Worksheet 19 Close the Atm Feed stream view then delete the stream Store This steady state case now contains the crude column without the preflash train Since the identical stream information was copied to stream Atm Feed the crude column operates the same as before the deletion of the 20 Save the case as DynTUT2 1 hsc Attachments Vapour Phase Fraction Temperature F Pressure psia Molar Flow lbmole hr Mass Flow lb hr Std Ideal Lig Vol Flow barrel day Molar Enthalpy Btu Ibmole

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