Home

User's Guide Version 1.13

Contents

1. 8 Press the Stop button and enter the flow rates from the above table into the stream data for the wells Specify the a value of 10 8 MMSCEFED for the Molar Flow of Well A Similarly enter the flow rates for Well B and Well C 9 Press the Go button and let PIPESYS complete the iterations 12 7 Optimization Application When the program is finished solving the network the new well pressures calculated by PIPESYS should be A 868 5 B 838 0 C 783 0 10 Find the flow rates that correspond to these pressures from the wellhead curves These values should be A 10 3 B 9 0 C 11 9 11 Once again press the Stop button and enter the flow rates from Step 11 into the well stream data as you did in Step 9 12 Press the Go button When the program is finished the well pressures should read A 842 5 B 810 9 C 763 8 You will find that the flow rate and pressure for Wells B and C are close enough to the curves and can consider these to be a valid solution However the point 10 3 MMSCFD and 844 5 psia on the Well A Wellhead Performance curve is still some distance from the graph You will need to do one or two more iterations to find the solution 13 Find the flow rate on the Well A curve that corresponds to 844 5 psia this should be 10 5 MMSCFD Press the Stop button and enter 10 5 into the flow rate parameter for the Well A stream 12 8 PIPESYS Ap
2. 5 Use the following information to complete the Compressor Property view On the Parameters page Brake Power Specified 1000 hp Max Discharge Temp 100 F Max Interstage Temp 100 F Number of Stages 2 Adiabatic Efficiency 0 73 Interstage delta P 10 psi On the Mechanical Losses Page Overall Efficiency 0 95 Once again the solution process will require several minutes to perform the iterative calculation for the PIPESYS network and converge When the process is complete the well pressures should be as follows 12 6 Well Pressure psia A 686 7 B 655 5 C 619 5 To compare the performance between two compressors the same calculations are repeated using a 750 hp compressor 6 Change the 1000 hp parameter in the Specified cell of the Brake Power group box to 750 hp When the HYSYS completes the iteration the new pressures are Well Pressure psia A 753 2 B 726 3 C 693 5 PIPESYS Application mr Application 2 12 7 The PIPESYS calculations indicate that when a 1000 hp compressor is used the wellhead pressure is lower than when a 750 hp compressor is used However this may not result in an economically significant higher production rate especially if these pressures are located on the steeper region of the wellhead performance curve Figures 12 4 12 5 and 12 6 at the end of this application show the wellhead performance curves for Well A Well B an
3. eecssseceseesseseeeseeseeeseesseeseeseeseneseeseeeseeneeseneneetes 13 9 7 1 C nhections Tab EE 15 ra 9 lt T HI TAD DEE 15 9 1 9 1 a 9 8 Erosion Velocity Check ccsccsseseerseseessseeeseesseesesseseeeseeseeeseeseeesesentes 16 9 81 SGCOMMECHONS TAD EE 17 9 8 2 E WEN 18 9 9 Side Stre E 18 9 9 1 Connection TAD 0 c ccenncevescesesencesessvnesuncrerscosnestneennezseecceatennezsuecueneds 19 9 9 2 Parameters lab TT 19 9 2 In line Facility Options 9 3 9 1 In line Heater The In Line Heater can be used with any fluid system but its effects are only considered for systems on which simultaneous pressure and temperature profile calculations are being performed For example the heater is ignored by the program if a user specified temperature profile is entered because to have both a heater and a user specified temperature profile over specifies the system PIPESYS copes with this situation by ignoring the effects of the heater E Neotec In line Heater Branch 1 ll x Klee Name Heater 1 imbibe Heater Location Unit Displacement 2900 m 280 0 m 3012m S Connections Parameters Delete 9 1 1 Connections Tab Figure 9 1 shows the Connections tab for the In line Heater As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab 9 1 2 Para
4. Recomended Procedures Gas based with liquid Liquid based with gas C User selected m Selections for Horizontal and Inclined Flow Selections for Yertical How Vertical Upflow Overall Selection JL Gas based default Overall Selection Gas based default Flow Regime Prediction Taitel and Dukler Flow Regime Prediction Govier and Aziz Liquid Holdup Eaion etal Liquid Holdup Aziz Govier and Fi Frictional Pressure Loss __Oliemans_ Frictional Pressure Loss Aziz Govier and Fc Uphill Correction No Correction Downhill Recovery Recovery Based ot Vertical Downflow o Overall Selection Gas based default Fluid Temperature Options Flow Regime Prediction Beggs and Brill Res Calculate Profile Liquid Holdup Beggs and Brill Res EE Frictional Pressure Loss Beggs and Brill Connections Worksheet Methods Elevation Profile Cooldown Aperature Profile Delete In the Fluid Temperature Options group box select either Calculate Profile or Specify Temperature If the former is selected the program will perform simultaneous pressure and temperature calculations if the latter the temperature of the fluid will be fixed according to values which you enter on the Temperature Profile tab and only pressure calculations will be performed Define the sequence of pipeline units that make up your system on the Elevation Profile tab You should start by entering values into the Dista
5. following table Methane mole frac 0 623 Ethane mole frac 0 280 Propane mole frac 0 0163 i Butane mole frac 0 00433 n Butane mole frac 0 00821 i Pentane mole frac 0 00416 n Pentane mole frac 0 00405 n Hexane mole frac 0 00659 C7 mole frac 0 00992 Nitrogen mole frac 0 00554 Carbon Dioxide mole frac 0 0225 Hydrogen Sulfide mole frac 0 0154 Because the stream composition is identical over the entire system the composition of stream specified for Well A may be copied to streams Well B and Well C 5 Use the Define from Other Stream button on Well B s stream view to define its composition by copying the stream specs from Well A Repeat for Well C 6 Now open the Energy Streams page on the Workbook view Enter the names of five energy streams Energy Streams ES1 ES2 ES3 ES4 ES5 For this case each of the five branches of the pipeline will be represented by a separate PIPESYS extension mn Setting Up the Case Setting Up the Case 11 3 Setting Up the Case 11 3 1 Adding the First PIPESYS Extension 1 Adda PIPESYS Extension to the flowsheet 2 Complete the Connections page as shown in Figure 11 3 SM PIPESYS Extension Branch 1 BIS See the PIPESYS Reference Manual Chapter 3 The Name Branch PIPESYS View for a Dutlet description of all pages in the PS main PIPESYS view Inlet well E Energy Solving Beh
6. sccssscseseceeeseeseeeseesenesseseeeseesseeseesseesenseneeeneeneae 9 6 1 Global Change Feature 6 3 The Global Change feature is a convenient way to change the parameters of multiple Pipe Units in the elevation profile A Global Change operation makes a simultaneous access to any or all of the Pipe Units in the elevation profile and changes a selection of parameters to your specifications The Global Change feature has been implemented in PIPESYS as a time saving mechanism so that you are not required to open the property views for each individual Pipe Unit in order to make a change common to all units The Global Change button is accessed through the Elevation Profile tab of the Main PIPESYS view SPIPESYS Extension Branch 1 Sisi Pipeline Dom Distance 0 00 Elevation E 00 Distance Pipeline Unit m 100 0 Pipe L Pipe Pipe B lt empty gt T ES Copy Paste Global Change View AAA Methods Elevation Profile Stepsize Temperature Profile Delete It can be used to edit the property view parameters for a single Pipe Unit and to subsequently duplicate the edits for none some or all of the other Pipe Units in the pipeline in a single sequence of operations This saves time when implementing changes to many Pipe Units at once Of greater importance is that this feature reduces the potential for errors during the edit pr
7. 4 10 To add a table to a PFD right click on the PFD and choose Add Workbook Table from the drop down list Figure 4 8 W PIPESYS Extension Branch 1 iol x Ee E E rEluid Temperature Pipeline Origirr Calculate profile E 4 Ambient Temperature C Specify temperatures Distance Elevation Cum Length Ambient T Surroundings Type Buried Buried Buried 13 Save your completed case as Pipesys1 hsc The PFD generated for the completed case plus a material stream table is shown below Figure 4 9 Branch 1 RE o Inlet Outlet been PIPSYS Q Material Streams Inlet Outlet Vapour Fraction 1 0000 1 0000 Temperature C 45 00 27 06 Pressure kPa 8000 7183 Molar Flow kgmole h 300 0 300 0 Mass Flow kg h 6504 6504 Liquid Volume Flow m3 h 17 78 17 78 Heat Flow kl 2 775e 007 2 799e 007 Pipe Unit View 5 1 d Pipe Unit View Sit Connections Tabi eessen gebuere CARE SEEREE EEN 3 5 1 1 IDIMENSIONS lab DEE 3 521 2 Heat Transter Tab stees ehy tin ENEE 5 5 13 Pipe Coatings Tabs ainen re annan a ae aa iai 8 5 2 Adding a Pipe Unit A aapne nann anneren annnnn annann ananman ennan nanana 9 5 1 Pipe Unit View 5 3 This view is used to enter all parameters associated with the specification of a Pipe Unit in PIPESYS All data settings related to physical characteristics such as dimensions roughness an
8. Outside Diameter all Thickness Inside Diameter Default Roughnesses bsolute Roughness Relative Roughness Ke Connections Dimensions Heat Transfer e 88 900 mm Default Steel bare wl T Change 5 486 mm 77 927 mm TT Change 0 04572 mm 0 000587 f Pipe Coatings The check beside a Pipe Unit parameter indicates that it has been changed and that this change can subsequently be applied to other Pipe Units Global Change Feature 6 11 Now change the Pipe Unit diameter to 4 Select 4 Inches from the Nominal Diameter drop down cell and you will see that a check appears in the Change check box beside it You will also have to re select Schedule 40 from the Pipe Schedule drop down cell Figure 6 13 shows the changed view Hl Neotec Pipe Unit Branch 1 o x 2 Pipe Dimensions el lM Change A Nominal Diameter Pipe Schedule 40 SE Outside Diameter Mall Thickness Inside Diameter __ 114 300 mm 6 020 mm 102 260 mm Default Roughnesses Change bsolute Roughness Relative Roughness Default Steel bare 0 04572 mm 0 000447 Connections Dimensions Heat Transfer Pipe Coatings Now press the Apply button at the bottom of the Global Change View The Global Change Dialog Box will appear Here you must specify which Pipe Units in the pipeline will be subjected to the Global C
9. 3 24 The PIPESYS View 3 4 8 Results Tab Calculation results at the endpoint of each pipeline unit are summarized on the screen in columns of Pressure Temperature Pressure Change and Temperature Change The length and label as entered in the Elevation Profile tab are also displayed PIPESYS Extension Branch 1 ojx Pressure kPa Cum Length Temperature DeltaP DeltaT m Cc kPa Label Pipeline Unit Pipe lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt Pipe H Pipe lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt Pipe 2 Pipe lt empty gt lt empty gt lt empty gt lt empty gt lt empty gt Pipe 3 Detail Report Worksheet Methods Z Elevation Profile L Cooldown The Results tab also features the Detail button the Report button and the Plot button These buttons give you the capability to view your data and results in a number of formats If you want to see results in greater detail than are displayed on the Results tab matrix press the Detail button This will bring up the Pipe Segment Results dialogue box that displays detailed results for each calculation step The pipe segment for each step is controlled according to the parameters on the Step Size tab For each of these the Pipe Segment Results dialogue box displays e Sum Length Horizontal distance of the Segment from the Pipel
10. Case Main Mi x Categories p Available Unit Operations All Unit Ops PIPESYS Ewtension Vessels Saturate Extension Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling Reactors Prebuilt Columns Short Cut Columns Sub Flowsheets Logicals Extensions User Ops Add Cancel on a a 66966666 To create a new PIPESYS Extension highlight PIPESYS Extension in the list of Available Unit Operations as shown above Click the Add button and a new PIPESYS Extension will become appear on the screen The initial PIPESYS view is the Connections Page and it is shown in Figure 2 4 SPIPESYS Extension Branch 1 ojx Name Branch 1 Outlet Outlet K Inlet BEN Inlet be Energy Solving Behaviour PIPE sys Q z I Ignore this UnitOp During Calculations e p m Connections Worksheet Elevation Profile Temperature Profile Delete To view any other pages of the PIPESYS view simply click on the tab of the desired page and the view will switch to the selected page The PIPESYS View 3 1 3 The PIPESYS View 3 1 PIPESYVS Features i Ao cect oes cence veces a etek eevee 3 3 2 Adding PIPESYVS cciccsscissstcescccsscssectsessseatensvacesecsvaseessecssseresicesecnsencvecteranvesves 4 3 3 PIPESYS User Interface sssini daaraan aapea iaa aa asaini nahaeun akadan da 8 3 4 The Main PIPESYS View ccsssscssssseessssseessseeeessseee
11. the vertical position of the compressor using the Pipeline Origin as the reference point e Unit Displacement the length of the true flow path from the pipeline origin to the compressor The data displayed in the Compressor Location group box may not be edited You must go to the Elevation Profile tab in the Main PIPESYS View if you need to change the compressor location data 7 3 The Compressor View Figure 7 1 Hl Neotec In line Compressor Branch 1 5 x Compressor Location Distance Elevation Unit Displacement 2900 m 280 0 m 3012 m Connections Parameters L Fuel Requirements 7 1 2 Parameters Tab This tab is used to define the basic operating characteristics of the compressor In the Compressor Type group box there is a drop down cell from which you can select one of five possible models for performing compressor calculations Figure 7 2 Neotec In line Compressor Branch 1 ioj xj 2 Type arameters P Brake Power Specified 37 3 kW Calculated 35 6 kw Discharge Pressure gt Specified lt empty gt Calculated 8963 2 kF Constraints Optional Number of Stages diabatic Efficiency lt empty gt Delete In line Compressor 7 5 The five types of compressor models available in PIPESYS are e Isentropic H S Diagram A compressor that follows an adiabatic compression path
12. Once you enter a value here PIPESYS will calculate the corresponding discharge pressure and display it in the Discharge Pressure group box e Calculated PIPESYS will display the brake power calculated from the specified Discharge Pressure in this input cell Discharge Pressure e Specified This value is the pressure at the outlet of a single or multistage compressor You need to specify only one of Brake Power or Discharge Pressure and PIPESYS will calculate the other Once you enter a value here PIPESYS will calculate the corresponding brake power and display it in the Brake Power group box 7 5 The Compressor View Calculated PIPESYS will display the discharge pressure calculated from the specified Brake Power in this input cell Optional Constraints Max Power If the compressor discharge pressure has been specified you can enter a value here to constrain the computed power requirement If no value is entered here PIPESYS will make its calculations with the assumption that the compressor is capable of supplying as much power as is needed to attain the specified discharge pressure However this can be an unrealistic assumption The compressor may be incapable of such performance in which case you can find the greatest discharge pressure that it can deliver without exceeding its rated maximum power To do so enter values for Discharge Pressure and Max Power If PIPESYS finds that the compressor must exceed the M
13. calculations using a specific value for the heat transfer coefficient rather than have PIPESYS calculate it for you choose this setting and enter a value in the Overall Heat Transfer Coefficient input cell e Buried If the pipe unit is completely below ground choose this setting e Submerged Used for pipe units that are completely immersed in water e Above Ground Choose this setting if the pipe unit is completely above ground and surrounded by air e Buried Submerged Used for pipe units that are partly below ground and partly underwater 5 6 5 6 Connections Tab e Buried Exposed Choose this setting if the pipe unit is partly below ground and partly exposed to air Hl Neotec Pipe Unit Branch 1 ioj x Heat Transfer Environment C User Specified Default Conductivities Default Steel Pipe Conductivity 48 461 Wim Centre Line Depth 0 914 m Submerged Soil Type Default Above Ground Soil Conductivity 0 865 Wimk C Buried Submerged Inside Film Coefficient lt empty gt C Buried Exposed Inside Film Coefficient Calculated C Specified Default Connections Dimensions Heat Transfer Pipe Coatings Delete The Inside Film Coefficient group box has a setting that allows you to control how PIPESYS accounts for the effects of the inside film on heat transfer The term inside film refers to the laminar sublayer that exists adjacen
14. i Pentane 0 00416 Hydrogen Sulfide 0 0154 Pipe diameters for each of the branches are Branch 1 3 Branch 2 3 Branch 3 3 Branch 4 4 Branch 5 6 Schedule 40 steel pipe is used throughout and all branches are buried at a depth of 3 feet All pipes are uninsulated Elevation data for each of the branches are provided in the following table The elevation given for the pipe units is for the endpoint of the pipe i e the downstream end Branches that traverse undulating terrain have been subdivided into a number of segments with elevation points assigned at locations where there is a significant slope change Such locations in the network are labelled on the schematic diagram with the elevation value in italics The following table summarizes the elevation data For each of the branches the resulting distance and elevation data as obtained from the topographic map is listed With these data you can simulate the performance of the given system using PIPESYS extension and thereby calculate important parameters such as pressure losses temperature changes and liquid holdup amounts as well as predicting the flow regimes Length ft Elevation ft Branch 1 Well A n a 2095 Pipe Unit 1 945 2110 Pipe Unit 2 1110 2089 Pipe Unit 3 1056 2090 PIPESYS Application ns Application 1 11 5 Branch 2 Well B n a 2015 Pipe Unit 1 282
15. into the Name cell The following table summarizes the required input for the Condensate stream Name Condensate Vapour Fraction 0 9576 Temperature F 110 Pressure psia 1150 Molar Flow lbmole hr 8235 signifies required input Mass Flow lb hr 1 905e 05 Liq Volume Flow barrel day 3 399e 04 Heat Flow Btu hr 3 307e 08 Std Gas Flow MMSCFD 75 00 Comp Mass Frac Methane 0 76110 Comp Mass Frac Ethane 0 07860 Comp Mass Frac Propane 0 02820 Comp Mass Frac i Butane 0 0075 Comp Mass Frac n Butane 0 0142 Comp Mass Frac i Pentane 0 0072 Comp Mass Frac n Pentane 0 0070 Comp Mass Fac n Hexane 0 0114 Comp Mass Frac Nitrogen 0 0096 Comp Mass Frac CO2 0 0390 Comp Mass Frac H2S 0 0268 Comp Mass Frac C7 0 0094 10 7 13 ee 0 8 Adding a PIPESYS Extension 10 8 10 2 Adding a PIPESYS Extension 1 Add the PIPESYS Operation to the HYSYS case by selecting Flowsheet and then Add Operation from the Menu Bar 2 Select PIPESYS Extension from the Available Unit Operations list in the UnitOps dialog as shown in Figure 10 6 and press the Add button Figure 10 6 12 UnitOps Case Main Categories All Unit Ops C Vessels Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling Reactors Y Prebuilt Columns Short Cut Columns Sub Flowsheets Logicals Extensions C User
16. parameters common to the PIPESYS operation as a whole 3 9 mu The Main PIPESYS View The Main PIPESYS View 3 10 Figure 3 8 SY PIPESYS Extension Branch 1 oj xj EECH Name Branch il Outlet Outlet Inlet EE leie SS Energy Solving Behaviour IS PESYS Q L T Ignore this UnitOp During Calculations perature Profile 77 Connections Worksheet Methods Z Elevation Profile L Cooldown The Main PIPESYS View is the starting point for the definition of any PIPESYS operation When you select Flowsheet Add Operation from the Menu Bar and then choose PIPESYS extension the Main PIPESYS View will appear and be ready to accept input You must then select each of the tabs on the Main PIPESYS View and complete them as required 3 4 1 Connections Tab This tab is used to define the connections between the HYSYS simulation case and the PIPESYS operation The inlet outlet and energy streams are specified here using the Inlet Outlet and Energy drop down input cells You may also choose a name for the operation and enter this in the Name input cell The Ignore this UnitOp During Calculations check box can be selected if you wish to disable the concurrent calculation of intermediate results during data entry This setting is recommended if you have a slow computer and data processing is slowing down the entry process or if you wish to delay the calculations until you have entered all of
17. profile the temperature or vapour mole fraction of the stream can be optionally specified If the flowing fluid temperature profile is being specified or the temperature or vapour mole fraction are left empty then the inflow stream s temperature and vapour mole fraction are obtained from main line stream conditions The Before Side Stream main line stream s data is used when calculations are done in the 9 19 9 20 Side Stream direction of flow For calculations done against the direction of flow the After Side Stream main line stream s data is used The outflow stream always obtains its temperature and vapour mole fraction data from the main line streams Similarly as when the inflow stream s temperature and vapour mole fraction data are left empty the Before Side Stream main line stream s data is used when calculations are done in the direction of flow For calculations done against the direction of flow the After Side Stream main line stream s data is used 9 20 Gas Condensate Tutorial 10 1 10 Gas Condensate Tutorial 10 1 Setting Up the Flowsheet cccssseseeeseseeeseeseeeseesseeseesseeseesseeseensentes 3 10 2 Adding a PIPESYS Extension ssscecsseeseesseeseesseeseesseeseeseeeseesseeseeneeeees 8 10 3 Applying a Global Change ssscsssssseseersesseeesesneeeseeseesseeseeeseeseenseeseees 16 10 1 10 2 To change the unit set to Field go to Tools in the menu bar and choose Preference
18. 1 has endpoint coordinates of 1200 360 To complete the profile data entry enter 1200 into the Distance cell and 360 into the Elevation cell PIPESYS automatically calculates all the other parameters as shown below SM PIPESYS Extension Branch 1 Jol x Pipeline Dom Distance 0 00 Elevation bm Length Run Rise Distance Elevation Angle Label 16 699 Pipeline Unit 1200 Pipe 360 0 1253 lt empty gt View Copy Paste Global Change Connections Worksheet Methods Elevation Profile Stepsize 7 perature Profile 77 Tr sufficient information on the Temperature Profile screen Delete Cooldown 7 Now add the second pipe unit to the matrix Fill in the pipe unit view with the same specifications as were used for Pipe Unit 1 You may either re enter all this information or use the Copy and Paste buttons on the Elevation Profile tab 8 This time specify the second pipe unit endpoint using the Run and Length parameters instead of Elevation and Distance Figure 4 1 shows that the second pipe unit has a Run of 1200 and a Length of 1227 84 Enter these values into the Elevation Profile tab You may have noticed that the data on the Elevation Profile tab does not correctly represent the actual geometry of the pipeline This is because PIPESYS always assumes a positive angle for the pipe unit when the Run and Length parameters are used
19. Change Connections J Worksheet Methods Elevation Profile Stepsize perature Profile 77 Close L Cooldown Using the Copy and Paste buttons on the Elevation Profile you are able to copy existing Pipeline Units from the Elevation Profile tab and create a new Pipeline Unit with identical properties This saves time when creating a pipeline consisting of several identical pipe units 16 Select the Pipe Unit that you want to copy in this case it is Pipe 1 and press the Copy button You will notice that the Paste button previously greyed out becomes active 17 Select the cell in the Pipeline Unit column with the lt empty gt label and press the Paste button A new Pipe Unit will be added to the profile Repeat this procedure twice so that the elevation profile matrix has a total of four Pipe Units 10 12 Gas Condensate Tutorial wm Tutorial 10 13 18 Since the Copy and Paste procedure copies only the property view data for the Pipe Units you are required to enter the elevation profile data for the remaining three units Use the data values shown in Figure 10 14 to fill in the Distance and Elevation parameters SM PIPESYS Extension Gas Condensate Pipeline ll xj Pipeline Origirr Distance pee Elevation puw Distance Elevation Pipeline Unit 3400 2550 230 am 3500 5162 3 888 Pipe 2 1 530e 004 2600 6750 um 6750 0 594 Pipe 3 2230 004 2290 7000 50
20. Change feature can be used to edit the Property View parameters for a single Pipe Unit and to subsequently duplicate the edits for some or all of the other Pipe Units in the pipeline Any Pipe Unit can be used as a data template for changing the other Pipe Units in the pipeline This short example uses the case Pipesys1 hsc that you created in Chapter 4 Elevation Profile Quick Start This case consists of a single PIPESYS extension comprised of 3 segments of steel pipe and a pig launcher situated between the second and the third pipe units The pipe is buried has a 3 diameter and is schedule 40 If you have not yet completed this case you must do so before proceeding with this example In this example the Global Change feature will be used to change the diameter of all the pipe units from 3 to 4 Figure 6 11 shows an 610 Makinga Global Change Making a Global Change 6 10 elevation profile diagram of the pipeline that is to be modified Figure 6 11 Elevation Pig R d Launcher 1200 300 2900 280 300 200 100 2400 100 Pipeline a oe Origin 0 1000 2000 3000 Distance 1 Highlight the Pipe Unit 1 in the Pipeline Unit column on the Elevation Profile tab and press the Global Change button 2 When the Global Change Pipe Unit View appears open the Dimensions tab as shown in Figure 6 12 Hl Neotec Pipe Unit Branch 1 Pipe Dimensions Nominal Diameter Pipe Schedule 40
21. Flow regimes liquid holdup and friction losses can also be determined There is considerable flexibility in the way calculations are performed You can compute the pressure profile using an arbitrarily defined temperature profile or compute the pressure and temperature profiles simultaneously e given the conditions at one end perform pressure profile calculations either with or against the direction of flow to determine either upstream or downstream conditions e perform iterative calculations to determine the required upstream pressure and the downstream temperature for a specified downstream pressure and upstream temperature compute the flow rate corresponding to specified upstream and downstream conditions Users familiar with HYSYS will recognise a similar logical worksheet and data entry format in the PIPESYS extension Those not familiar with HYSYS will quickly acquire the skills to run HYSYS and PIPESYS using the tools available such as the user manuals online help and status bar indicators It is recommended that all users read this manual in order to fully understand the functioning and principles involved when constructing a PIPESYS simulation S 1 2 How This Manual Is Organized This user manual is a comprehensive guide that details all the procedures you need to work with the PIPESYS extension To help you learn how to use PIPESYS efficiently this manual thoroughly describes the views and capabilities of PIPES
22. Institute Subsurface Controlled Subsurface Safety Valve Sizing Computer Program API Manual 14BM Second Ed p 38 API Jan 1978 American Petroleum Institute Technical Data Book Petroleum Refining API New York 1982 Aziz K Govier G W and Fogarasi M Pressure Drop in Wells Producing Oil and Gas J Can Petrol Technol Vol 11 p 38 July 1972 Baker O Simultaneous Flow of Oil and Gas Oil Gas J Vol 54 No 12 p 185 Jul 1954 Baker O Experience with Two Phase Pipelines Can Oil Gas Ind Vol 14 No 3 p 43 Mar 1961 Beggs H D and Brill J P A Study of Two Phase Flow in Inclined Pipes J Petrol Technol p 607 May 1973 Bendiksen K H Maines D Moe R and Nuland S The Dynamic Two Fluid Model OLGA Theory and Application SPE Paper No 19451 SPE Prod Eng May 1991 Burke N E and Kashou SE History Matching of a North Sea Flowline Startup Using OLGA Transient Multiphase Flow Simulator SPE Paper No 24789 Presented at the 67th Annual SPE Technical Conference and Exhibition Washington DC October 1992 Chen N H An Explicit Equation for Friction Factor in Pipe Ind Eng Chem Fund Vol 18 No 3 p 296 1979 Dukler A E Wicks M and Cleveland R Frictional Pressure Drop in Two Phase Flow B An Approach Through Similarity Analysis AIChE J Vol 10 No 1 p 44 Jan 1964 Dukler A E Gas Liquid
23. Line Depth T Submerged C Above Ground C Buried Submerged C Buried Exposed 0 550 Suhe lt empty gt Inside Film Coefficient Calculated C Specified Default l Connections 7 Dimensions Heat Transfer Delete Pipe Coatings 14 Go to the Pipe Coatings tab of the Pipe Property View Add a single layer of insulation consisting of PVC Foam with a thickness of 2 inches See Figure 10 12 to verify the correctness of your data entries before pressing the Close button on the Pipe Property View Neotec Pipe Unit Gas Condensate Pipeline Pi e x Po in lt Pipe Coatings Thickness in Conductivity Btuzhr ft F 0 023 l Insert Layer Coating Remove PC Foam lt empty gt Im Remove All Connections 7 Dimensions 7 Heat Transfer_ Pipe Coatings Delete 10 11 1042 Adding a PIPESYS Extension 0 12 Adding a PIPESYS Extension 15 Complete the specification for the first Pipe Unit by entering 3400 ft into the Distance column and 2880 ft into the Elevation column of the elevation profile matrix Figure 10 13 shows the data entry completed for the first Pipe Unit K PIPESYS Extension Gas Condensate Pipeline iol x Pipeline Dom Distance 0 00 Elevation 2800 00 Distance Elevation Run Rise Pipeline Unit Pipe 3400 2880 3400 80 00 3401 1 348 lt empty gt View Cut Copy Paste Global
24. Next button HYSYS will then begin installing files to your computer 10 Once the all the files have been transfered to their proper locations the installtion program will register the PIPESYS extension with HYSYS Once the extension is successfully registered click OK to continue HYSYS Extension Registration MHE regextn Version of Jan 18 1999 16 43 45 a Registered E PIPESYS PIPESYS dll Scanning E PIPESYS PIPESYS edf Adding keys Software Hyprotech HYSYS 1 1 Extensions BD 7274E0 9DE4 1 1CF 9344 004400BB 0078 CLSID 8D 7274E0 9DE4 11CF 9344 004400BB0078 ExtensionDefinitionFile E PIPESYS PIPESYS ed lt default gt PIPESYS Extension ExtensionT ype UnitO peration Piping Successfully registered 1 objects OK 11 Click FInish to complete the installation 2 3 2 Starting PIPESYS You can work with PIPESYS only as it exists as part of a HYSYS case Extensions that are part of an existing case may be accessed upon entering HYSYS Main Simulation Environment Here you can view and manipulate them as you would any HYSYS unit operation Before creating a new PIPESYS Extension you are required to be working within a HYSYS case that has as a minimum a Fluid Package consisting of a property package and components New PIPESYS Extensions are added within the Main Simulation Environment from the UnitOps view which lists all the available Unit Operations 2 5 2 6 Installing PIPESYS H UnitOps
25. Ops Available Unit Operations Hydrocyclone Liquid Liquid Extractor LNG Mixer MPC Controller Parametric Unit Operation PID Controller Pipe Segment PIPES Plug Flow Reactor Pump Reboiled Absorber Recycle Refluxed Absorber Relief valve Rotary Vacuum Filter E lol x Add Cancel The Main PIPESYS View should now be on your screen displaying the Connections tab 9 ee e Name the PIPESYS extension Gas Condensate Pipeline From the Inlet drop down list select the Condensate stream Select the Outlet stream from the Outlet drop down list Select Pipeline Energy Transfer from the Energy drop down list Click on the Ignore this UnitOp During Calculations check box The Ignore the UnitOp During Calculations allows you to disable the concurrent calculation of intermediate results while you are specifying data to the PIPESYS extension Figure 10 7 shows the completed view Gas Condensate Tutorial ma Tutorial 10 9 Figure 10 7 K PIPESYS Extension Gas Condensate Pipeline ioj x Name Gas Condensate Pipeline Inlet a Condensate KZ Energy Solving Behaviour 7 Pipeline Energy Transf z perature Profile 77 Connections Worksheet Elevation Profile Stepsize Z Cooldown Insufficient information on the Elevation Profile screen Delete 8 Open the Methods tab Make sure the Gas based with Liquid and the Calculate Profile radio
26. Pipe Unit and to subsequently duplicate the edits for none some or all of the other Pipe Units in the pipeline in a single sequence of operations Any Pipe Unit can be used as a data template for changing the other Pipe Units in the pipeline To implement a global parameter change for some or all of the Pipe Units in the elevation profile select any one of the Pipe Units in the elevation profile matrix and press the Global Change button The Global Change Property View will appear This Property View is identical to the Pipe Unit Property View except that it has check boxes beside each of the major data types on each of its tabs Hl Neotec Pipe Unit Branch 1 o xj Pipe Dimensions Nominal Diameter 3 Inches Pipe Schedule 40 bal Outside Diameter all Thickness Inside Diameter 88 900 mm 5 486 mm 77 927 mm Default Roughnesses ibsolute Roughness Relative Roughness Default Steel bare 0 04572 mm 0 000587 Connections Dimensions Heat Transfer_ Pipe Coatings Delete 3 17 8 The Main PIPESYS View The Main PIPESYS View For more information on making global changes see Chapter 6 Global Change Feature These check boxes have two functions 1 they become checked automatically when you change a parameter to remind you that a particular parameter has been selected for a global change and 2 you can check them manually to indicate to th
27. as occurs with wells under gas lift Erosion losses are seldom a problem in a straight run of pipe but can be significant anywhere the flow abruptly changes direction e g manifolds elbows tees etc It is usual to perform this check at the downstream end of the pipeline where not only do such direction changes typically occur but generally also the highest gas velocities prevail For liquid droplet erosion caused by a sand free fluid the limiting velocity is defined by the following empirical equation v E u VP y where C a constant pm mixture density lb ft Vy maximum allowable mixture velocity The PIPESYS erosion velocity check makes this calculation for two values of the constant C so that you may choose a more conservative or less conservative maximum velocity depending on your need to limit erosion To eliminate erosion losses it is suggested that the value recommended by the API RP14E C 100 be used For situations in which a small amount less than 10 mils per year of erosion can be tolerated Salama and Venkatesh recommend a higher value C 300 It is important to realize that the minimum erosion velocity is a function of the gas density Much higher velocities can be tolerated at low pressure than at high pressure In line Facility Options 9 17 A different relation is used for fluids bearing sand The maximum allowable velocity is obtained using where d pipe inside diameter inches W r
28. cesses cease deed Tagos 3 3 3 2 Adding PIPESYS tte eege det 3 4 23 PIPESYS User Interface nose eaae 3 8 3 4 The Main PIPESYS View 3 9 Elevation Profile Quick Start ssssssssssssssssssssss 4 1 4 1 Flow Sheet Set Up ec ee eee ee 4 3 4 2 Adding the PIPESYS Extension 4 4 4 3 Defining the Elevation Profile AAA 4 5 Pipe Unit View sssssssssssssssssssssssssssssssssssssssssssssss B 1 DI Connections Tab enaere iis Bes 5 3 5 2 Adding a Pipe Uniti ccann aii deed gen 5 9 Global Change Feature sssssssesssessssesssesssesees Del 6 1 Global Change View 6 4 6 2 Global Change Procecdure sss sese eee eee 6 7 6 3 Making a Global Change 6 9 7 10 11 12 13 In line COMPFeSSOF sssssssssssssssssss sss sss EE Ek nek enen 7 1 7 4 The Compressor View 7 3 7 2 Adding a Compreseor sese ee eee ee eee 7 13 In line Pump ssssssssssssssssssssssssssssssssssssssssssssssssssss OF 1 8 1 In line PUMP View sese eee eee eee eee eee 8 3 In line Facility Options sssssssssssssssssssssssssssssssssss 9 1 9 1 In line Heater onc Ze eer CEET 9 3 92 In line Coolers Aessen ege ZER eg 9 4 Bem IE e be vows eek eg ee ee E EEE 9 6 9 4 An line Regulators ed scenes nein inated 9 8 9 5 In line ulas een lind eee 9 9 9 6 Pigging Slug Check 9 11 9 7 Severe Slugging Check 9 13 9 8 Erosion Velocity Check 9 16 G WT EE 9 18 Gas Condensate Tutorial sssssssssssssssssssssssssss 10 1 10 1 Setting Up
29. coefficient If you want PIPESYS to supply a default value for any of the Parameters data highlight the input cell and press the Default button in the lower 5 7 5 8 5 8 Connections Tab right corner of the group box PIPESYS will supply a default value to the input cell 5 1 3 Pipe Coatings Tab If the pipe has insulating and protective coatings the relevant data can be entered into the matrix on this tab You should begin with the innermost coating for Layer 1 and proceed outwards To enter the data for a coating layer select the cell in the Coating column containing lt empty gt From the drop down input cell at the top of the tab see Figure 5 5 you can then choose from a number of coating types Cl Neotec Pipe Unit Branch 1 5 x z User Specified Ee Pipe Co Asphalt Cement Concrete insulating Concrete weight Glass Fibre e Once a coating type has been selected the corresponding conductivity value for that material will appear in the Conductivity column Complete the layer description by entering a value for the thickness If you want to add a new entry at an intermediate point on the list select a cell in the row that will follow the position of the new entry Press the Insert button and an empty row will be created for you to enter data The Remove and Remove All buttons are used respectively to delete a particular row and to delete the entire matrix K Neotec Pipe Unit Bran
30. for the selected Pipe Unit has not changed but will be copied to other Pipe Units in the elevation profile 6 1 Global Change View 6 1 1 Connections Tab Displayed in the Name cell on this tab is the name of the Pipe Unit that was selected for the Global Change appended to the words Copy of This serves as a reminder that you are only working with a copy of the Pipe Unit data No changes will be made to the original data until you first press the Apply button select some Pipe Units to change and then finally press the Close button to close the Global Change View This will then initiate the recalculation of the PIPESYS extension Global Change Feature 6 5 Figure 6 4 Hl Neotec Pipe Unit Branch 1 BIS z Name Copy of Pipe 4 Global Change o Either select the data to apply in the global change or make changes to the pipe data and have those changes applied E Connections Dimensions Z Heat Transfer_ Pipe Coatings 6 1 2 Dimensions Tab This tab is identical to the Dimensions tab of the Pipe Unit Property View except for the Change check boxes beside the Nominal Diameter cell and the Roughness Data matrix K Neotec Pipe Unit Branch 1 xi Pipe Dimensions v M Change Nominal Diameter Pipe Schedule 40 Outside Diameter vall Thickness Inside Diameter 88 900 mm 5 486 mm 77 927 mm Default Roughnesses T Change bsolute Roughness 0
31. make any representations or warranties of any kind whatsoever with respect to the contents hereof and specifically disclaims without limitation any and all implied warranties of merchantability of fitness for any particular purpose Neither Neotec nor Hyprotech will have any liability for any errors contained herein or for any losses or damages whether direct indirect or consequential arising from the use of the software or resulting from the results 1 5 1 6 obtained through the use of the software or any disks documentation or other means of utilisation supplied by Neotec or Hyprotech Neotec and Hyprotech reserve the right to revise this publication at any time to make changes in the content hereof without notification to any person of any such revision or changes 1 4 Copyright The software and accompanying material are copyrighted with all rights reserved Under copyright laws neither the manual nor the software may be duplicated without prior consent from Hyprotech or Neotec This includes translating either item into another language or format This program is protected by a hardware security device Security Key The authors will not be held responsible for any damage to or loss of data from the user s computer if any attempts at unauthorised copying are made PIPESYS and PIPEFLO are trademarks of Neotechnology Consultants Ltd 1 5 Acknowledgements The authors recognise all trademarks used in the manual T
32. more than one individual Pipe Unit hold down lt shift gt while selecting the desired units The check box also allows you to specify that the data of a particular unit as it appears will be duplicated to other Pipe Units in the elevation profile To do this just click on the check box beside each parameter that you want copied to other Pipe Units but leave the data unchanged 3 Once all the changes that you want to make have been specified press the Apply button and the Global Change Dialogue Box will appear with a list of all the Pipe Units in the profile Figure 6 10 Select the pipeline objects to apply the global changes to UnSelect All Select the Pipe Units in the list that will be subjected to the Global Change and press the OK button 4 To complete the Global Change you must close the view by pressing the Close button PIPESYS will then make the requested parameter changes to all Pipe Units selected for the Global Change procedure Global Change Feature 6 9 6 3 Making a Global Change Example The Global Change feature has been implemented in PIPESYS as a time saving mechanism so that when making a change common to more than one pipe unit you do not need to open each Property View and change the data manually A Global Change operation makes a simultaneous access to any or all of the Pipe Units in the elevation profile and changes a selection of parameters to the desired values The Global
33. option to do cooldown calculations can be enabled on the Cooldown tab of the PIPESYS Extensions Main View when the flowing fluid temperature profile is calculated There are two fluid temperature cooldown options that you may choose from e Temperature profiles computed at specified times after shutdown e Profile of time to reach a specified temperature after shutdown For both of the above options the calculations can be based on one of two options e Heat content of the pipeline fluid only Computed or specified inside film heat transfer coefficient e Heat content of both the fluid and pipe material Ignoring the inside film heat transfer coefficient For calculations are based on the heat content of the pipeline fluid only computed or specified inside film heat transfer coefficient the fluid thermal conductivity inside film coefficient or overall heat transfer coefficient can either be specified or computed by the program If the 3 21 3 22 The Main PIPESYS View overall heat transfer coefficient is specified the option to specify the inside film heat transfer coefficient no longer exists For calculations based on the heat content of both the fluid and pipe material ignoring the inside film heat transfer coefficient the overall heat transfer coefficient can either be specified or computed by the program Both the heat capacity of the pipe material and the density of the pipe material must be specified and defaults are
34. remaining liquid in the riser will be energetically blown downstream and the gas pressure will drop to its minimum value Then the liquid buildup begins anew and the process repeats Severe slugging can be a problem for pipeline engineers and operators because of the irregular flow pattern that develops The resultant variations in pressure and flow rate make for an ill behaved system that is difficult to control and operate according to requirements If possible severe slugging should be prevented It is less likely to occur at higher pressures and can be inhibited by choking the flow at the top of the riser although at the cost of reducing production rates Other prevention methods include installing an active flow control device at the top of the riser or injecting gas into the riser just above the base This ensures that the riser can never completely fill with liquid In line Facility Options 9 7 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab Figure 9 8 Neotec Severe Slugging Check Branch 1 m oj x Name SevereSlugCheck 1 Severe Slugging Check Location Unit Displacement 2900 m 280 0 m 3012m Connections Results 9 7 2 Results Tab There are no data entry requirements for this calculation Parameters are taken from the calculated
35. the Flowsheet A 10 3 10 2 Adding a PIPESYS Extension 10 8 10 3 Applying a Global Change 10 16 PIPESYS Application 1 s sssssssescseessessseesssees 11 11 1 Gas Condensate Gathering Gvsiem see eee eee 11 3 11 2 Setting up the Floweheet AA 11 6 11 3 Setting Up the Case E 11 8 If Results2 wcncicie teachin e ees 11 18 PIPESYS Application 2 ssssssssssssssssssssssssssssssss 12 1 12 1 Optimization Appiicaion sss sese ee eee eee 12 3 Glossary Of Terms sssssss sss sss sss sss sss ssssssssssssssss 13 1 3 15 PIPESYS b ZT 13 3 13 2 FRETEFENCES 12 ee R ea aiti 13 6 13 3 PIPESYS Methods and CGorrelatons sss sse esse eee 13 9 Inde 1 ENN S 1 Overview h N N ssi Le 1 2 1 2 How This Manual Is Organized sececssseeeeeseeeeeeneeeeeeseeeseesseeseeseesneeneeeees 5 1 3 DISCIAIMER wvvcaiiictetsdicaies tices ececcecsutersacceccesviersacvedeevensieguesssssnenpeioedestsvetudvebersesed 5 1 4 Copyright EE Ae vse ve esse ees eesyeeveeesveereresrereeene 6 1 5 Acknowledgementts cccsssssessseesscesseesenessseesseessseeseeesenesssneesnenseenennes 6 BAG TU a E E 7 17 Technical Support eg eseu eeEEEEEEEEEEEEEEEESEEEEEEESEeNen 8 1 7 1 Technical Support Centres sees eree ereer e eee eee eee 9 1 7 2 Glen nn ce eneeeeeeeeaeeeneeaceseeseeeeeesneeeerees 10 URS RAIS ETRE aere scccssccccencseesste MMMM cusceconsensecuseusossesesesonsenosseonsensoes 11 1 1 Ce 1 1 Introduction A pipeline must tran
36. the flowing temperature to be isothermal and will fill in the cells with a constant temperature equal to the last entered temperature You can easily overwrite a cell with your own value anywhere the software has filled in a temperature for you Figure 3 18 SMPIPESYS Extension Branch 1 15 x E rEluid Temperature Pipeline Origin Calculate profile Ea 2 Fluid Temperature 0 00 Ze Specify temperatures Distance Elevation Cum Length Fluid Temperature m 300 0 10 00 3002 Pipe 1 49 50 550 0 15 00 551 4 Pipe 2 47 00 872 0 25 00 875 9 Pipe 3 40 00 Connect Worksheet Elevation Profile Delete PIPESYS calculates the fluid temperature when the Calculate Profile button in the Fluid Temperature group box is selected Much like the specified temperatures you must enter at least one temperature value of the surroundings into the Ambient Temperature input cell in the Pipeline Origin group box Any other values can be entered in the Ambient T column corresponding to the surroundings temperature at the end of a pipe segment For any empty cells between the origin and a Pipe unit with a surroundings temperature PIPESYS will interpolate linearly and fill them in with calculated values Any other cells that are empty will be filled with the last entered temperature As with the specified temperatures you can overwrite any of the filled in ambient temperature cells
37. to specify the coordinates of the endpoint 9 To correct the matrix data make a note of the Angle value which is 12 23 and then delete the value in the Length cell Now enter 12 23 into the Angle cell Or alternately you could enter the value for the Rise as 260 m 4 7 4 7 4 8 Defining the Elevation Profile 10 To add the Pig Launcher select the lt empty gt cell and choose Pig Launcher from the Edit Bar W PIPESYS Extension Branch 1 5 x Polane sl Pipeline Origirr Distance 0 00 Elevation bm Elevation Run Rise mi Jm 1200 360 0 1200 360 0 1253 16 699 Pipe 1 2400 100 0 1200 260 0 1228 _ 12 225 Pipe 2 2000 100 0 6 0000 0 0000 0 0000 0000 PigLauncher 1 Distance Pipeline Unit Pi j lt empty gt View Cut Copy Paste Global Change Connections Worksheet Methods H Elevation Profile Stepsize perature Profile 77 L Cooldown Delete You are not required to specify any additional data to incorporate the Pig Launcher into the matrix Figure 4 6 shows the Elevation Profile tab after the Pig Launcher has been added Position data for the launcher or any other in line facility does not have to be specified because this information is obtained automatically from the preceding component Elevation Profile Quick Start 4 9 11 Finally add a third pipe unit with the same parameters as the previous
38. view select Pipe from the drop down list as in Figure 10 9 A Pipe Unit will be added to the elevation profile matrix and the Pipe Property View will open Figure 10 9 H PIPESYS Extension Gas Condensate Pipeline BIS Ka S E Awe T ahel 11 Open the Dimensions tab of the Pipe Property View Select 12 Inches from the Nominal Diameter drop down list Select 40 from the Pipe Schedule drop down list When you are finished these steps the Dimensions tab will appear as in Figure10 10 Figure 10 10 Hl Neotec Pipe Unit Gas Condensate Pipeline iol xj zl Pipe Dimensions Nominal Diameter L Pipe Schedule 40 L Outside Diameter 12 750 in all Thickness 0 406 in Inside Diameter 11 938 in Default Roughnesses Default Steel bare bsolute Roughness 0 00180 in Relative Roughness 0 000151 s Connections _ Dimensions Heat Transfer Delete Pipe Coatings 12 Open the Heat Transfer tab of the Pipe Property View Enter 4 ft for the Centre Line Depth parameter 10 10 Gas Condensate Tutorial wn Tutorial 10 11 13 Choose Sandy Soil Moist from the drop down list for Soil Type eotec Pipe Unit Gas Condensate Pipeline sell x N Pipe Unit Gas Cond Pipeli Sandy Soil Moist e Heat Transfer Environment Buried Pipe Parameters C User Specified Default Conductivities Default Steel Buried Pipe Conductivity j 28 000 Btu h Centre
39. 0 Wellhead Pressure psia N Q E LD oa ki N WoO a A Q y Q o GB PIPESYS Application 2 Wellhead Performance Curve for Well B Gas Flow Rate MMSCFD 11 12 11 Optimization Application Wellhead Performance Curve for Well C Wellhead Pressure psia N E A O Ny wo Gas Flow Rate MMSCFD 12 12 GlossaryofTerms mr of Terms 13 1 13 Glossary of Terms 13 1 PIPESYS Terms E D 3 13 2 Referen S E 6 13 3 PIPESYS Methods and Correlations cccscccssssessseetessseeeesssesensseeees 9 13 3 1 For Horizontal and Inclined Elow 13 3 2 For Vertical and Near Vertical Upflow and Downflow 13 1 13 2 Glossary of Terms 13 3 13 1 PIPESYS Terms absolute roughness The effective roughness of a pipe used in calculating the frictional pressure loss caused by fluid flow shear with the pipe wall This quantity is assigned a value derived from a sand particle size such that a perfectly smooth pipe internally coated with sand particles of that size experiences a frictional pressure loss per unit length identical to that in the actual pipe all other parameters being equal actual gas velocity The velocity that is obtained when the in situ volumetric gas flow rate is divided by the cross sectional area of the pipe that is occupied by the gas brake power The power
40. 0 68 kPa 68 95 kPa 0 069 kPa Te Program Defaults C User Specified Enthalpy Convergence Minimum dH step 1 396 kJ kc Maximum dH stepy 4 652 kJ ke 0 023 kJ kg IT Eorce Enthalpy Convergence IV Optimize Stepsize Overall Pipeline Pressure Convergence Minimum allowed pressure l 101 008 k Downstream pressure convergence tolerance 0 069 KP perature Profile ff if Connections Z Worksheet Z Methods Z Elevation Profile Stepsize To safeguard against a step size that is too large PIPESYS has input cells containing the Maximum dP per step or Maximum dT per step If this pressure change dP or temperature change dT is exceeded on any calculation the step size is halved and the calculations repeated An arbitrarily small step size could perhaps be chosen by the software to meet these criteria but this could result in greatly increased run time with no corresponding increase in accuracy Defaults are provided for these parameters and you will rarely be required to change them There may be cases where you wish to enter your own stepsize values For this reason you will find cells on this tab where you can not only specify an initial step size but where you can also enter maximum and minimum allowed pressure and temperature changes Checking the Stepsize Optimizer check box then requests that PIPESYS determine the stepsize such that the pressure
41. 00 7000 0 409 Pipe H View Cut Copy Paste Global Change Connections Worksheet Methods sy Delete Close 19 Open the Stepsize tab of the Main PIPESYS View Make sure the For most cases the PIPESYS Program Defaults radio button is selected as in Figure 10 15 default Stepsize and tolerance peice Figure 10 15 extension calculations K PIPESYS Extension Gas Condensate Pipeline ioj xj Stepsize and Tolerances Pipe Lengths _ Pressure Convergence 10 00 psi Ge Program Defaults ee 3 000 Ge C User Specified Senn 10 00 psi Go empl 0 010 psi r Iemperature Convergence Enthalpy Convergence T Force Enthalpy Initial dT Guess Minimum dH step 0 6000 Btu Convergence er Maximum dH step 2 000 Btu lt fe Res Tolerance 0 010 Bud Overall Pipeline Pressure Convergence Minimum allowed pressure 14 650 ps Downstream pressure convergence tolerance 0 010 psi Connections Z Worksheet Methods Z Elevation Profile Stepsize perature Profile 7777 10 13 1044 Adding a PIPESYS Extension 0 14 Adding a PIPESYS Extension 20 Open the Temperature Profile tab of the Main PIPESYS View 21 Enter 40 F into the Ambient Temperature cell in the Pipeline Origin group box as shown in Figure 10 16 Figure 10 16 SA PIPESYS Extension Gas Condensate Pipeline Biel E 40 E 7 Fluid Temperature Pipeline Origin Calculate prof
42. 04572 mm Relative Roughness 0 000587 Connections Dimensions Apply Heat Transfer_ Pipe Coatings 6 5 6 6 Global Change View 6 1 3 Heat Transfer Tab On this tab you can change any of the parameters that affect the heat transfer from the fluid system The type of environment method of inside film coefficient derivation and the parameters associated with the environment can all be altered during a Global Change operation Figure 6 6 Hl Neotec Pipe Unit Branch 1 i x Heat Transfer Environment Buried Pipe Parameters c Default Conductivities Pipe Conductivity Specified 2 48 461 W m R Centre Line Depth 0 914 m Submerged Soil Type Default C Above Ground Soil Conductivity 0 865 W mK C Buried Submerged Inside Film Coefficient lt empty gt C Buried Exposed Inside Film Coefficient Calculated C Specified T Change Connections Dimensions Heat Transfer Apply Default Pipe Coatings 6 1 4 Pipe Coatings The Pipe Coatings tab lists in matrix form the insulating coatings applied to the Pipe Unit Figure 6 7 K Neotec Pipe Unit Branch 1 ioj xj 2 000 mm z Pipe Coatings Thickness mm Conductivity Insert W mK 0 040 Layer Coating Remove PVC Foam Remove All lt empty gt Hu IZ Change Connections Dimensions Heat Transfer Pipe Coati
43. 13 11 3 3 Adding a Mixer For this pipeline configuration a HYSYS Mixer is used to merge streams Other HYSYS operations can be used to merge streams but the Mixer is the simplest to use and the most suitable for the this example 12 Adda Mixer to your simulation Named Junction 1 it is used to merge streams PS1 and PS2 Figure 11 9 shows the completed Connections page I gt Junction 1 5 x More information regarding EM S HYSYS unite operations is Design ie located in the HYSYS Reference Manual 2 Chapter 13 Physical Operations Connections Parameters User Variables Notes Inlets Outlet lt lt Stream gt gt uge Rating Z Worksheet Ware Co 13 On the Parameters page of the Mixer select the Equalize All radio button in the Automatic Pressure Assignment group box Automatic Pressure Assignment Equalize All C Set Outlet to Lowest Inlet 11 13 114 Setting Up the Case Setting Up the Case 11 3 4 The Third PIPESYS Extension The third PIPESYS extension you add is used to represent Branch 4 It consists of a single pipe unit 14 Enter the data for the third PIPESYS extension as defined in the following table Connections Page Name Branch 4 Inlet Stream FS4 Outlet Stream PS4 Energy Stream ES4 Elevation Profile Distance ft 0 Page Elevation ft 2090 Pipeline Unit Pipe 1 Pipe 1 Elevation ft 2077 Pip
44. 2 0033 Overview 1 9 Technical Support Centres support hyprotech com e mail 403 520 6181 local technical support 1 888 757 7836 toll free technical support 403 520 6601 fax technical support 1 800 661 8696 information and sales support hyprotech com e mail 34 93 724 424 technical support 900 161 900 toll free technical support Spain only 34 93 154 256 fax technical support 34 93 156 884 information and sales support hyprotech com e mail 0800 731 7643 freephone technical support 44 1235 43 4351 fax technical support 44 1235 43 4852 information and sales support hyprotech com e mail 60 3 4270 3880 technical support 60 3 4271 3811 fax technical support 60 3 4270 3880 information and sales support hyprotech com e mail 81 45 476 5051 technical support 81 45 476 5051 information and sales 1 9 1 10 Technical Support 1 7 2 Offices Calgary Canada Tel 403 520 6000 Fax 403 520 6040 60 Toll Free 1 800 661 8696 Newark DE USA Tel 302 369 0773 Fax 302 369 0877 Toll Free 1 800 688 3430 Oxford UK Tel 44 1235 43 5555 Fax 44 1235 43 4294 Oudenaarde Belgium Tel 32 55 310 299 Fax 32 55 302 030 Hovik Norway Tel 47 67 10 6464 Fax 47 67 10 6465 Kuala Lumpur Malaysia Tel 60 3 4270 3880 Fax 60 3 4270 3811 Yokohama Japan Tel 81 45 476 5051 Fax 81 45 476 3055 Houston TX USA Tel 713
45. 2 2090 Branch 3 Well C n a 2085 Pipe Unit 1 528 2125 Pipe Unit 2 334 2080 Pipe Unit 3 670 2077 Branch 4 Pipe Unit 1 1167 2077 Branch 5 Pipe Unit 1 2110 1980 In this simple example the flow rate at each well is specified and is independent of the flow rate at each of the other wells In cases such as this the system can be modelled with only one pressure drop determination per branch Simultaneous pressure and temperature calculations can be performed if the temperature at each wellhead is also known Figure 11 2 shows the PFD generated by HYSYS for the completed case Branch 1 Well A Branch Branch 5 ES pranch PSs Junction 1 Well B ES2 Branch 3 Well C E53 Since pressures are continuous throughout the network the pressure can be specified at only one point For instance the pressure can be fixed at any one well or at the final delivery point and PIPESYS will compute the pressure everywhere else For this application example a pressure of 1060 psia will be specified for Well A PIPESYS will then determine the pressures elsewhere in the network that are consistent with this specification 1 Setting up the Flowsheet Setting up the Flowsheet Heat transfer calculations should be performed in the direction of flow whenever possible Furthermore wellhead temperatures are generally known For this example the fluid temperatures at wells A B and C are known and must be entered
46. 339 9600 Fax 713 339 9601 Toll Free 1 800 475 0011 Barcelona Spain Tel 34 932 724 424 Fax 34 932 154 256 D sseldorf Germany Tel 49 211 577933 0 Fax 49 211 577933 11 Cairo Egypt Tel 20 2 720 0824 Fax 20 2 702 0289 Seoul Korea Tel 82 2 3453 31445 Fax 82 2 3453 9772 1 7 3 International Innotech Inc Katy USA International Innotech Inc Beijing China International Innotech Taipei Taiwan KBTECH Ltda Bogota Colombia KLG Systel New Delhi ndia Logichem Process Johannesburg South Africa Process Solutions Pty Ltd Peregian Australia Protech Engineering Bratislava Slovak Republic PT Danan Wingus Sakti Jakarta ndonesia Ranchero Services Thailand Co Ltd Bangkok Thailand S C Chempetrol Service srl Bucharest Romania Soteica De Mexico Mexico D F Mexico Soteica Do Brasil Sao Paulo Brazil Soteica S R L Buenos Aires Argentina Soteiven C A Caracas Venezuela ZAO Techneftechim Moscow Russia Agents Overview 1 11 Tel 281 492 2774 Fax 281 492 8144 Tel 86 10 6499 3956 Fax 86 10 6499 3957 Tel 886 2 809 6704 Fax 886 2 809 3095 Tel 57 1 258 44 50 Fax 57 1 258 44 50 Tel 91 124 346962 Fax 91 124 346355 Tel 27 11 465 3800 Fax 27 11 465 4548 Tel 61 7 544 81 355 Fax 61 7 544 81 644 Tel 421 7 4488 8286 Fax 421 7 4488 8286 Tel 62 21 567 4573 75 62 21 567 4508 10 Fax 62 21 567 4507 62 21 568 3081 Te
47. 8 900 mm _ Wall Thickness 5 486 mm Inside Diameter 77 927 mm Default Roughnesses Default Steel bare bsolute Roughness 0 04572 mm Relative Roughness 0 000587 _ A Connections Dimensions Heat Transfer Delete Pipe Coatings The Pipe Dimensions group box contains the following parameter input cells e Nominal Diameter The commercial sizing descriptor for a given pipe size e Pipe Schedule This drop down box allows you to select from the American Standard B36 10 pipe wall thickness schedule or use the traditional standard weight S extra strong XS and double extra strong XXS specification method for entering the pipe nominal wall thickness value e Outside Diameter A value will be automatically generated and entered here once a nominal diameter is selected If you are dealing with a non standard pipe size you can enter this value manually e Wall Thickness The actual thickness of the pipe wall Can be set manually e Inside Diameter The actual inside diameter of the pipe Can be set manually e Default Roughness Wall roughness can be set by PIPESYS according to the pipe material entered in this input cell If you have a specific value for roughness that you want to use instead choose the User specified setting for Default Roughness You will now be able to enter any value into the Absolute Roughness input cell Specify the Default Roughness by selecting from th
48. Control tool allows you to change the Data Axes Title Legend and Plot Area For example you can change the scaling on the plot axes by opening the Axes tab selecting the variable to be re scaled in the list of axes and removing the check from the Use Auto Scale check boxes in the Bounds group box Then change the values in Minimum and Maximum input boxes When the Close button is pressed the plot will be redrawn with the new scales 3 4 9 Messages Tab The text window of this tab is used to display messages or warnings that may have arisen during the PIPESYS extension calculations Elevation Profile Quick Start 4 1 4 Elevation Profile Duich Start 4 1 Flow Sheet Set Up A eege eegen 3 4 2 Adding the PIPESYS Extension scecssseeseseneseeseeseesenesenseeeseeseneneensenes 4 4 3 Defining the Elevation Profile ccscsssssseessteessesssnessneeesseesseeesneeseneeeees 5 4 1 Ifyou would like to follow a more detailed step by step procedure for creating a PIPESYS case see Chapter 10 Gas Condensate Pipeline Elevation Profile Quick Start 4 3 One of the first and most important steps in adding a PIPESYS operation to a HYSYS Flowsheet is the construction of the elevation profile The purpose of this procedure is to create a representation of the pipeline as a connected series of components with the corresponding position data In this example you will go through the steps to enter an elevation profil
49. DJUST operation The adjust will be used to maintain a constant pressure of 1000 psia at the Gas Plant with the pressure at Well A being the adjusted variable 12 3 12 4 12 4 Optimization Application See the PIPESYS Manual Chapter 7 In line Compressor for more information on adding and defining compressor parameters 2 Add an ADJUST operation with the following specifications Name Adjust Adjusted Variable Object Well A Adjusted Variable Variable Pressure Target Variable Object PS5 Target Variable Variable Pressure Specified Target Variable 1000 psia Method Secant Tolerance 0 10 psi Step Size 100 psi Max Iter 25 3 Press the Start button at the bottom of the Adjust property view to begin the adjust calculations HYSYS will require several minutes to reach a solution This is because the entire PIPESYS network must be recalculated for each iteration Upon convergence the well pressures should be Well Pressure psia A 1093 B 1077 C 1052 The next step will be to add an in line compressor at the upstream end of PIPESYS Branch 5 If this addition reduces the pressure at the wells to an extent that production can be significantly increased then the additional cost of the compressor is justifiable It is also useful to look at the incremental performance increase of a larger compressor in order to get a feel for sizing the compressor The performan
50. Dimensions tab of the Pipe Unit view by specifying a Nominal Diameter of 3 Inches and a Pipe Schedule of 40 Figure 4 3 shows the completed tab Hl Neotec Pipe Unit Branch 1 Sie Pipe Dimensions Nominal Diameter Pipe Schedule 40 na Outside Diameter Mall Thickness _ Inside Diameter Best Foughnesses bsolute Roughness 0 04572 mm Relative Roughness 0 000587 Default Steel bare Connections Dimensions Heat Transfer Delete Pipe Coatings 4 Go to the Heat Transfer tab of the Pipe Unit view Select the cell that reads lt empty gt for the Centre Line Depth and the click the Default button Figure 4 4 shows the completed tab Figure 4 4 Cl Neotec Pipe Unit Branch 1 i l x Heat Transfer Environment Buried Pipe Parameters C User Specified Default Conductivities Default Steel Buried Pipe Conductivity _ 48 461 win Centre Line Depth 0 914 m Submerged Soil Type Default C Above Ground Soil Conductivity 0 865 W mK C Buried Submerged Inside Film Coefficient lt empty gt C Buried Exposed Inside Film Coefficient Calculated C Specified Connections Dimensions Heat Transfer Delete Pipe Coatings 5 Close the complete Pipe Unit view Elevation Profile Quick Start 6 The pipe unit will now appear as an entry in the matrix with lt empty gt in all parameter cells Pipe
51. ESYS enables you to e rigorously model single phase and multiphase flows compute detailed pressure and temperature profiles for pipelines that traverse irregular terrain both on shore and offshore e perform forward and reverse pressure calculations e model the effects of in line equipment such as compressors pumps heaters coolers regulators and fittings including valves and elbows e perform special analyses including pigging slug prediction erosion velocity prediction severe slugging checks e model single pipelines or networks of pipelines in isolation or as part of a HYSYS process simulation e perform sensitivity calculations to determine the dependency of system behaviour on any parameter e quickly and efficiently perform calculations with the internal calculation optimizer which significantly increases calculation speed without loss of accuracy 1 3 Introduction e determine the possibility of increasing capacity in existing pipelines based on compositional effects pipeline effects and environmental effects A PIPESYS network ES2 ch RS ES Junction PIPESYS bm Branch E DG PIPESYS Branch PS5 PIPESYS Branch L T res 5 PIPESYS keng PIPES Get em 4 Es3 PIPESYS Branch 3 a ESCH Ji Ri A wide variety of correlations and mechanistic models are used in computing the PIPESYS extension Horizontal inclined and vertical flows may all be modelled
52. Flow in Pipelines Monograph Project NX 28 AGA API May 1969 Duns H Jr and Ros N Vertical Flow of Gas and Liquid Mixtures in Wells Paper No 22 Section II World Petrol Conf Frankfurt Germany 1963 13 6 Glossary of Terms 18 of Terms 13 7 Eaton B A Andrews D E Knowles C R Silberberg I H and Brown K E The Prediction of Flow Patterns Liquid Holdup and Pressure Losses Occurring During Continuous Two Phase Flow in Horizontal Pipelines J Petrol Technol p 815 Jun 1967 Flanking O Effect of Uphill Flow on Pressure Drop in Design of Two Phase Gathering Systems Oil Gas J p 132 Mar 10 1958 Fuchs P The Pressure Limit for Terrain Slugging Paper BA Proc of the 3rd Int Conf on Multiphase Flow BHRA The Hague Netherlands 1987 Govier G W and Aziz K The Flow of Complex Mixtures in Pipes Van Nostrand Reinhold 1972 reprinted by Robert E Krieger Publishing Co Huntingdon New York 1977 Govier G W and Fogarasi M Pressure Drop in Wells Producing Gas and Condensate J Can Petrol Technol Oct 1975 Gregory G A Estimation of the Overall Heat Transfer Coefficient for Calculating Heat Loss Gain in Flowing Wells Technical Note No 4 Neotechnology Consultants Ltd Calgary Canada Mar 1991 Gregory G A Mandhane J and Aziz K Some Design Considerations for Two Phase Flow in Pipes J Can Petrol Technol Jan Ma
53. May 1983 Oliemans R V A Two Phase Flow in Gas Transmission Pipelines Paper No 76 Pet 25 Joint Petrol Mech Eng amp Pressure Vessels and Piping Conf Mexico City Mexico Sept 1976 Oliemans R V A Modelling of Gas Condensate Flow in Horizontal and Inclined Pipes Proc ASME Pipeline Eng Symp ETCE p 73 Dallas Texas Feb 1987 Pots B EM Bromilow I G and Konijn M J W E Severe Slug Flow in Offshore Flowline Riser Systems SPE Prod Eng p 319 Nov 1987 Salama M M and Venkatesh E S Evaluation of API RP 14E Erosional Velocity Limitations for Offshore Gas Wells Paper No OTC 4485 presented at the 15 Annual Offshore Technology Conference Houston May 1983 Singh B and Gregory G A unpublished work 1983 Taitel Y and Dukler A A Model for Predicting Flow Regime Transitions in Horizontal and Near Horizontal Gas Liquid Flow AIChE J Vol 22 No 1 p 47 Jan 1976 Tennessee Gas Pipeline Co private communication 1979 13 8 Glossary of Terms 13 9 13 3 PIPESYS Methods and Correlations 13 3 1 For Horizontal and Inclined Flow Flow Regime Prediction Methods e Beggs and Brill 1973 e Beggs and Brill Revised 1977 e Mandhane Gregory and Aziz 1974 e Mandhane Gregory and Aziz Alternate 1974 e Govier and Aziz 1972 e Baker 1954 e Taitel and Dukler 1976 e OLGAS 1994 Liquid Holdup Prediction Methods e Olieman s Mech
54. PIPES Yo n a L SE Copyright Notice The copyright in this manual and its associated computer program are the property of Hyprotech Ltd All rights reserved Both this manual and the computer program have been provided pursuant to a License Agreement containing restrictions on use Hyprotech reserves the right to make changes to this manual 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 No part of this manual may be reproduced transmitted transcribed stored in a retrieval system or translated into any other language in any form or by any means electronic mechanical magnetic optical chemical manual or otherwise or disclosed to third parties without the prior written consent of Hyprotech Ltd Suite 800 707 8th Avenue SW Calgary AB T2P 1H5 Canada 2001 Hyprotech Ltd All rights reserved HYSYS HYSYS Plant HYSYS Process HYSYS Refinery HYSYS Concept HYSYS OTS HYSYS RTO HYSIM and PIPESYS are registered trademarks of Hyprotech Ltd Microsoft Windows Windows 95 98 Windows NT and Windows 2000 are registered trademarks of the Microsoft Corporation This product uses WinWrap Basic Copyright 1993 1998 Polar Engineering and Consulting Documentation Credits Authors of the current release listed in order of historical start on project Rolf C Fox B Sc E
55. SYS Application 2 Optimization Application le PIPESYS Application c 12 1 Optimization Application cceecsseeeseesseeseeesensseeneesseeneeeseeteeeseeneeseenes A 12 2 PIPESYS Application 2 12 3 12 1 Optimization Application Optimizing the Gas Condensate Gathering System This application is a continuation of the Application 1 Gas Condensate Gathering System in which you modelled the performance of a small gas condensate gathering system given fixed wellhead rates and plant delivery requirements As the next step you will attempt to increase production from the wells by adding a compressor to the fifth PIPESYS extension Using supplied wellhead performance curves the effect of lowering the pressure at the wellheads will be gauged in terms of the resulting increased flow rates Figure 12 1 shows the completed PFD for the completed Application Branch 1 Adjust Branch 4 Branch gt gt E F54 PS4 PIPES JL Junction gt Re mes PS5 Junction Ess Well A PS1 mb ES Branch 2 up Ga l 3 EG Branch 3 ua n S E ES3 PS3 You must complete the Gas Condensate Gathering System Application before you are able to begin work on this application 1 Start HYSYS and load the case file network hsc that you saved upon completion of the Gas Condensate Gathering System of the first part of this application exercise The first modification you make will be to add an A
56. The surroundings type for each Pipe Unit is displayed here as an overview of the system for verification purposes If you choose to switch from a specified temperature profile to a calculated profile note that the Pipe Units will have to be updated with data for heat transfer calculations not previously required In this case PIPESYS will warn you of missing data when calculations are attempted Reasonable default values will be made available for unknown data 3 23 3 24 The Main PIPESYS View To enter temperatures directly select the Specify Temperatures radio button The matrix will display the profile previously entered on the Elevation Profile tab In the Fluid Temperature column you can enter the flowing temperature at the end of each Pipe Unit You must enter at least one flowing temperature at the start of the pipeline and this value is entered in the Fluid Temperature input cell in the Pipeline Origin To enter the pipeline fluid group box All other temperatures are entered in the Fluid Temperature temperatures directly select column of the appropriate Pipe Unit For any cells that are empty the Specify Temperatures between specified temperatures PIPESYS will interpolate linearly the radio button in the Fluid flowing temperatures enter only one more fluid temperature in the last EE cell of the profile to automatically create a linear profile For any cells that are empty after the last entered temperature PIPESYS will assume
57. YS as well as outlining the procedural steps needed for running the extension The basics of building a simple PIPESYS pipeline are outlined in the Quick Start see Chapter 4 Elevation Profile Quick Start A more complex system is then explored in the tutorial problem see Chapter 10 Gas Condensate Tutorial Both cases are presented as a logical sequence of steps that outline the basic procedures needed to build a PIPESYS case More advanced examples of PIPESYS applications are available in the Applications binder This manual also outlines the relevant parameters for defining the entire extension and its environment as well as the smaller components such as the pipe units and in line facilities Each view is defined on a page by page basis to give you a complete understanding of the data requirements for the components and the capabilities of the extension The PIPESYS Users Guide does not detail HYSYS procedures and assumes that you are familiar with the HYSYS environment and conventions If you require more information on working with HYSYS please see Volumes 1 and 2 of the HYSYS Reference Manual Here you will find all the information you require to set up a case and work efficiently within the simulation environment 1 3 Disclaimer PIPESYS is the proprietary software developed jointly by Neotechnology Consultants Ltd hereafter known as Neotec and Hyprotech Ltd hereafter known as Hyprotech Neither Neotec nor Hyprotech
58. ab In the Fitting Selection group box you may select one of five methods for specifying the pressure loss across a fitting by specifying values for the following parameters e Pressure Drop A constant value of pressure loss independent of the flow rate 9 10 In line Fittings e Velocity Heads This method requires a value of the resistance coefficient or number of velocity heads which you enter here to calculate the pressure loss associated with the mixture velocity and density of the fluids e Number of Diameters Characterizes the pressure loss as an equivalent length of pipe measured in terms of pipe diameters or the L D ratio The pressure loss across the fitting is calculated to be equal to that for a horizontal section of pipe having diameter D and length L e Valve Coefficient This method uses the valve coefficient which is defined as the flow rate of water expressed in U S gallons per minute at 60 F that results in a pressure loss of 1 0 pounds per square inch across the valve when it is fully open This coefficient is used in an expression for pressure loss that accounts for a variety of flow conditions and fluid properties Although this expression was derived using water flow it is still a useful guide for valves used in compressible flow i e gas service e Hooper K1 amp Hooper K2 These constants are used in the Hooper procedure to calculate the resistance coefficient which is in turn used to ca
59. and positive for upward sloping Pipe Units Adding an in line facility to the pipeline is simpler because a single point is sufficient to fix its location In most cases you will not have to supply any location data because the position of the in line facility will be determined by the endpoint of the previous Pipeline Unit Entering the Elevation Profile The elevation profile matrix on this tab provides a place for you to enter the sequence of Pipeline Units and the data that defines the geometry of the profile You must enter the Pipeline Units in the order in which they appear in the flow stream so that the first entry is the unit connected to the inlet stream and the last entry is the unit connected to the outlet stream A Pipeline Unit can be entered as follows 1 Select the cell with lt empty gt in it to place the new unit at the end of the sequence To place the new unit at some other point in the sequence select the unit that you want the new unit to precede From the drop down list on the Edit Bar select the Pipeline Unit of the type that you want to add to the sequence A new unit will be immediately added to or inserted in the matrix Now complete the location data if you have entered a Pipe Unit You will have to define at most two of the Distance Elevation Run Rise Length or Angle quantities The remaining cells will be filled in automatically once PIPESYS has enough information to complete the specification For in
60. anistic Model 1987 e Hughmark 1962 e Beggs and Brill 1973 e Beggs and Brill Revised 1977 e Dukler 1969 e Eaton et al 1967 e Lockhart and Martinelli 1949 e OLGAS 1994 Frictional Loss Prediction Methods e Olieman s Mechanistic Model 1987 e Beggs and Brill 1973 e Beggs and Brill Rough Pipe 1973 e Olieman s 1976 e Lockhart and Martinelli 1949 e Dukler et al 1964 e Dukler et al Rough Pipe 1964 e OLGAS 1994 13 9 1340 PIPESYS Methods and Correlations 3 10 PIPESYS Methods and Correlations 13 10 Uphill Corrections e Beggs and Brill Liquid Holdup Correction e Flanigan Head Correction Factor e Tennessee Gas Head Factor e Singh and Gregory Head Factor 13 3 2 For Vertical and Near Vertical Upflow and Downflow Flow Regime Prediction Methods e Govier and Aziz 1972 e Beggs and Brill 1973 e Beggs and Brill Revised 1977 e OLGAS 1994 e Gregory et al 1989 Liquid Holdup Prediction Methods e Aziz Govier and Fogarasi 1972 e Beggs and Brill 1973 e Beggs and Brill Revised 1977 e OLGAS 1994 e Gregory et al 1989 Frictional Loss Prediction Methods e Aziz Govier and Fogarasi 1972 e Beggs and Brill 1973 e Beggs and Brill Rough Pipe 1973 e OLGAS 1994 e Gregory et al 1989 A Above Ground Pipe 5 5 Absolute Roughness 5 5 Activate Curve 8 5 Adiabatic Efficiency 7 6 Air Parameters 5 7 Angle 3 15 Attached Streams 3 10 Brake Powe
61. anscenerssenens 18 PIPESYS Application 1 11 3 11 1 Gas Condensate Gathering System In this PIPESYS Application the performance of a small gas condensate gathering system is modelled Figure 11 1 shows the physical configuration of this system superimposed on a topographic map The system consists of three wells distributed over an area of approximately 1 0 square mile connected to a gas plant via a network of pipelines RN Cen d yq Wels Pipeline elevation a BE ag x Pea Well D 24632 Branch 2 wettc 4 EI Zhe f lt 634 4 Branch 6 Junction 1 Es amp Branch 4 633 Junction 2 Branch 5 617 645 ae Plant Branch 7 639 xr Branch 1 ki Elevation in meters Well A gil Field data shows that the wells are delivering the following rates Well C 10 1 MMSCFD All three wells have the same composition A residual of all the heavier components in the condensate has a molecular weight of 122 anda density of 760 keim The characteristics of this component will be accounted for by using the hypothetical component facility in HYSYS 11 4 Gas Condensate Gathering System The compositional analysis of the gas condensate resulted in the following information Methane 0 623 n Pentane 0 00405 Ethane 0 280 n Hexane 0 00659 Propane 0 0163 C7 0 00992 i Butane 0 00433 Nitrogen 0 00554 n Butane 0 00821 Carbon Dioxide 0 0225
62. as defined on an Enthalpy Entropy diagram e Polytropic Internal Curve The performance of this type is defined by a set of generalized curves contained within PIPESYS These curves describe the relationship between the required brake horsepower per unit of volumetric flow referenced to one atmosphere and the suction temperature and the compression ratio for gases with various specific heat capacity ratios e Polytropic User Curve This compressor is identical to the Polytropic Internal Curve type except that the performance is defined by data which you must enter on the Curve tab e lIsentropic GPSA This compressor follows an adiabatic cycle such that PV constant where P is pressure V is specific volume and k is the heat capacity ratio Cp Cv e Polytropic GPSA This compressor follows an polytropic path such that PV constant where n is called the polytropic exponent Selection of one of these types should be based on your knowledge of the specific compressor that you are modelling Once a particular compressor type is selected the tab will change accordingly and display input cells in which you can enter the values used to characterize the compressor Each compressor type has some or all of the following parameters that must be entered Brake Power e Specified The Brake Power is the total power for all stages You need to specify only one of Brake Power or Discharge Pressure and PIPESYS will calculate the other
63. as fixed conditions PIPESYS will then perform an iterative pipeline calculation in branches where the upstream temperature and downstream pressure are known Temperatures of the blended fluids will be computed on a mass basis downstream of the junctions of two or more streams 11 2 Setting up the Flowsheet Carry out the following steps to model the gathering system with PIPESYS 1 Start HYSYS and create a New case In the Simulation Basis EE Manager create a fluid package using the Peng Robinson equation HYSYS views and conventions see the HYSYS Reference of state and consisting of the pure components methane ethane Manual 1 Chapter 1 propane i butane n butane i pentane n pentane hexane Interface nitrogen carbon dioxide and hydrogen sulfide Property Package Pure Components Peng Robinson C1 C2 C3 i C4 n C4 i C5 n C5 C6 Nitrogen CO2 H2S 2 Create a hypothetical component C7 with the following user defined properties Add it to the fluid package before entering the Main Simulation Environment Name C7 signifies required input Molecular Weight 122 Ideal Liquid Density Ib ft3 47 45 3 Open the Workbook and add the 10 Material Streams listed below Material Streams Well A Well B Well C PS1 PS2 PS3 PS4 PS5 FS4 FS5 PIPESYS Application 1 11 7 4 Enter the compositional data for Well A as specified in the
64. aste functions These buttons will copy the contents of the current Pipeline Unit to memory so that all the data they contain i e pipe diameter for the Pipe Unit can then be copied to a new Pipeline Unit The Cut operation will copy data to memory before removing the unit whereas the copy function will make a copy and preserve the original unit The Paste operation will create a new Pipeline Unit at the cursor position As explained above if this is a Pipe Unit it will then be necessary to enter any two of distance elevation run rise length or angle 3 16 The PIPESYS View 3 17 The Global Change button allows you to change the parameters for several or all of the Pipe Units in the Elevation Profile This feature has been implemented in PIPESYS as a time saving mechanism so that if the same information is required for several Pipe Units you do not need to open the Property Views for each individual Pipe Unit and to change the data A global change operation simultaneously accesses any or all of the Pipe Units in the elevation profile and can change a selection of parameters For example having made a pressure drop calculation for a 4 pipeline you may want to repeat the calculation for the same pipeline using 6 pipe Using the Global Change feature you could in a single procedure change the pipe diameters from 4 to 6 for all Pipe Units The Global Change feature can be used to edit the Property View parameters for a single
65. ate of sand production bbl month where 1 bbl sand 945 lb 429 kg Vu maximum allowable mixture velocity The maximum velocity as Ws approaches zero is assumed to be constrained by the previous equation Even relatively small amounts of sand production have a strong influence on the maximum velocity that should be permitted For example with 4 I D tubing and a typical gas density of 4 0 lb ft the effect of sand production dominates the allowable velocity at any sand production rate above about 100 lb month 9 8 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab Figure 9 9 K Neotec Erosion Velocity Check Branch 1 o x Name Erosion elocityCheck 1 Erosion Velocity Check Location Distance Elevation Unit Displacement 2900 m 280 0 m 3012 m o Connections Results 9 17 9 18 9 18 9 8 2 Results Tab The Fluid Conditions group box displays the Actual Gas Velocity Mixture Velocity Mixture Density and Effective C Value at the erosion velocity check location The mixture velocity data is provided so that you may compare this value against the allowable velocities that appear in the matrix in the Allowable Velocity group box The actual gas velocity and mixture density values are provided for your information To analyse the data p
66. ation in a Pipeline uE Delete Finse If you have added a Pipe Unit to the pipeline you will need to define the position of the downstream end of the pipe using the Distance Elevation Run Rise Length and Angle parameters Any two of these parameters are sufficient to fix the position of the end of the pipe However if you use Length and one of Run or Distance to define the pipe end position the program is unable to resolve the resulting ambiguity associated with the Angle parameter and assumes that this value should be positive If in fact the Angle is negative make a note of the Angle magnitude delete one of the Length Distance or Run values and enter the negative of the Angle magnitude into the Angle input cell 6 The Stepsize tab displays optimizing parameters used in PIPESYS algorithms For a first time solution of your system it is recommended that the Program Defaults radio button be selected For most systems the default values will provide near optimal convergence and solution times 3 7 3 8 3 8 PIPESYS User Interface This group box is also available on the Methods tab 7 Open the Temperature Profile tab Here you can choose to specify a predetermined set of fluid temperatures for your system as might be available from field data or if the system s sensitivity to temperature is being examined Alternatively you can request that the program calculate the heat transfer from the fluid to the su
67. available for these parameters Both of the calculations based on either the heat content of the pipeline fluid only or the heat content of both the fluid and pipe material allow the fluid thermal conductivity to be specified or calculated at all times unless the overall heat transfer coefficient is specified The fluid thermal conductivity can be calculated based on the liquid gas or blended thermal conductivities By default the calculations use the liquid thermal conductivity as this presents the most conservative results for both calculated times and temperatures As a note the fluid thermal conductivity is not used by the calculations when the inside film heat transfer coefficient is specified unless a Pipe Unit has its overall heat transfer coefficient specified The option to compute temperature profiles at specified times after shutdown requires that the e maximum e first second e and third intermediate times since shutdown be entered The intermediate times must be in increasing order and less than the maximum time Defaults are available for these times whereby the first second and third intermediate times are set to be one quarter one half and three quarters of the maximum time since shutdown respectively The profile of time required to reach a specified temperature after shutdown requires that the minimum cooldown temperature be entered Both of the options available for the cooldown calculations require the
68. aviour e ES L T Ignore this UnitOp During Calculations Cooldown Connections Worksheet A Methods Elevation Profile Delete 3 On the Elevation Profile page and enter 0 ft into the Distance cell and 2095 ft into the Elevation cell 4 Add the first of three pipe units for this extension on the Elevation Profile Page The Pipe Unit view will appear PIPESYS Application na Application 1 11 9 5 On the Dimensions Page of the Pipe Unit view specify the pipe as being 3 inches in diameter schedule 40 The completed page is shown in Figure 11 4 Hl Neotec Pipe Unit Branch 1 il x Pipe Dimensions Nominal Diameter Pipe Schedule 40 Outside Diameter 3 500 in all Thickness 0 216 in Inside Diameter 3 068 in Default Roughnesses Default Steel bare bsolute Roughness 0 00180 in Relative Roughness 0 000587 Connections Dimensions Heat Transfer Pipe Coatings 6 On the Heat Transfer page click on the Centre Line Depth cell and press the Default button All other parameters may be left at their default values See Figure 11 5 for the completed form K Neotec Pipe Unit Branch 1 ell xi Heat Transfer Environment r Buried Pipe Parameters C User Specified Default Conductivities Default Steel KE Geen Pipe Conductivity 1 28 000 un Centre Line Depth 3 000 ft Submerged Soil Type Default C Above Ground Soil C
69. ax Power setting to match the discharge pressure it will recalculate and find the greatest discharge pressure that it can deliver at the maximum power setting Max Discharge Pressure If the compressor power has been specified in the Brake Power cell you can constrain the compressor discharge pressure by entering a value in this cell In this way you can ensure that you do not exceed the maximum operating pressure for your pipeline If the specified power will cause the compressor to exceed the maximum discharge pressure then the compressor discharge will be set to this value and a new lower brake power will be computed Parameters Max Discharge Temperature The temperature of the compressor discharge is limited to this value by cooling the gas The theoretical duty for the cooler is reported on the Requirements tab Max Interstage Temperature This parameter is applicable only to multi stage compressors If the temperature of the gas at any of the intermediate discharges exceeds this value PIPESYS will automatically install an interstage cooler to lower the temperature of the gas to this value This duty is also reported on the Requirements tab Number of Stages You may specify any number of stages for a multi stage compressor in this input cell If you leave this empty PIPESYS will compute the number of stages based on a maximum compression ratio of 4 1 Polytropic Efficiency PIPESYS uses a default value of 0 73 unless you s
70. behind the pig would become quite substantial In hilly terrain with moderate to large liquid to gas ratios the pig may well travel at somewhere around 60 of the average steady state gas velocity Unless the pipeline is quite long with relatively high liquid loading the differences in slug size due to pig velocity are not excessive For most cases this check can provide a useful guide for sizing the liquid receiving facilities The insertion of a Pigging Slug Check in a pipeline profile indicates the termination point of the test or the location of the pig slug catcher Therefore the length of the pipeline through which the pig travels 9 11 Pigging Slug Check spans the distance between its insertion point at a Pig Launcher and the Pigging Slug Check The Pig Launcher is available on the drop down list of in line facilities options on the Elevation Profile tab It is added to the Elevation Profile tab in the same manner as any other in line facility Because the Pig Launcher serves only as a marker for the beginning of a Pigging Slug Check it does not have any physical properties and therefore does not have an associated view You are able to add more than one Pig Launcher to the elevation profile of a PIPESYS Extension However PIPESYS will perform the slugging check between the pig slug catcher and the nearest upstream Pig Launcher If you do not insert a Pig Launcher into the profile PIPESYS will calculate the volumes fro
71. bic meters per day You must also enter the curve data into the matrix You should be able to obtain this information from the compressor manufacturer s specification sheets You must enter at least two data points to completely specify the compressor curve It is not necessary to enter the Point value as these numbers are automatically generated You must enter a value into the Reference Pressure input cell This value is the pressure at which the compressor was tested and should be recorded on the compressor specification sheets 7 7 7 8 7 8 The Compressor View Figure 7 3 Cl Neotec In line Compressor Branch 1 o xj m Compressor Curve FHp MMsctd SE Power Units Brake Power Flow lt empty gt Compression Ratio lt empty gt 78 Reference Pressure lt empty gt Connections Parameters Curve d Delete The Insert Remove and Remove All buttons can be used to alter the curve data after all points have been entered To insert select the entry that immediately follows the position where you want the new point to be located Press the Insert button and blank data cells will appear in the list To remove a data point select the specific cell to be removed and press the Remove button If you want to clear the list and start over press Remove All In line Compressor 7 1 4 Fuel Requirements Tab PIPESYS Compressor Units can remove gas from the st
72. ble Note The pump can only be added to an all liquid system 8 1 In line Pump View 8 1 1 Connections Tab Figure 8 1 K Neotec In line Pump Branch 1 iol xi J z Name Pm Pump Location Distance Elevation Unit Displacement 2900 m 280 0 m 3012 m S Connections Parameters 7 Curve Delete Figure 8 1 shows the Connections tab for the In line Pump The name and location of the pump are repeated here from the Elevation Profile tab of the Main PIPESYS View The location once defined in the Main PIPESYS View cannot be changed in any other view and is displayed here only for your reference If you need to change the location open the Elevation Profile tab of the Main PIPESYS View 8 1 2 Parameters Tab Here you must choose to model the pump by using a built in relation or by entering data to define a performance curve If you check the Activate Curve check box as shown in the upper left hand corner of Figure 8 2 the user defined performance curve will be enabled and you are required to enter the curve data on the Curve tab PIPESYS uses the 8 4 In line Pump View built in relation when it is left unchecked The only additional data you need to provide are values for some of the parameter input cells on this tab Figure 8 2 K Neotec In line Pump Branch 1 ioj x l E Parameters _ lt empty gt lt empty gt lt empty gt lt empty gt Speci
73. buttons are selected as in Figure 10 8 Figure 10 8 PIPESYS Extension Gas Condensate Pipeline ll xj Recomended Procedures Ze Gas based with liquid Liquid based with gas C User selected mSelections for Horizontal and Inclined Flou Selections for Vertical flow Vertical Upflow Overall Selection Flow Regime Prediction Overall Selection Flow Regime Prediction Gas based default Taitel and Dukler Gas based default Govier and Aziz Liquid Holdup Eaton et al Liquid Holdup Aziz Govier and Fogai Frictional Pressure Loss Oliemans Frictional Pressure Loss Aziz Govier and Fogar Uphill Correction No Correction KE Se SS Downhill Recovery Recovery Based on Ge Vertical Downflow Gas based default Beggs and Brill Reviset Beggs and Brill Reviset Beggs and Brill Flow Regime Prediction Liquid Holdup Frictional Pressure Loss Fluid Temperature Options Calculate Profile Specify Temperature Connections 7 Worksheet Methods Elevation Profile Stepsize Cooldown 10 9 Se 0 10 Adding a PIPESYS Extension 9 Select the Elevation Profile tab Here you will define the geometry and physical characteristics of the pipeline Enter 0 into the Distance cell and 2800 into the Elevation cell in the Pipeline Origin group box 10 Select the cell in the Pipeline Unit column that reads lt empty gt Then from Edit Bar at the top of the
74. calculation time step to be entered A default value of ten minutes is provided as a reasonable value for this parameter 3 22 The PIPESYS View 3 23 3 4 7 This tab allows you to select one of two options for handling fluid temperature effects in the pipeline The Fluid Temperature group box in the top left corner is also located on the Methods tab and it is included here only as a matter of convenience should you wish to change your initial selection Temperature Profile Tab To compute the pipeline pressure profile PIPESYS must know the fluid property behaviour and must therefore know the temperature of the fluids at every calculation point in the pipeline You can enter the temperature directly if known or if you are testing the sensitivity of the pipeline to temperature effects Figure 3 17 SM PIPESYS Extension Branch 1 EREM Eluid Temperature Pipeline Origin Calculate profile S A Ambient Temperature k empty gt C Specify temperatures Distance Elevation Cum Length Ambient T S C Surroundings Type 300 2 Pipe 1 lt empty gt Buried 551 4 Pipe 2 lt empty gt Buried 875 9 Pipe 3 lt empty gt Buried L Elevation Profile Cooldown Temperature Profile Alternatively you can request detailed heat transfer calculations Pipe surroundings and heat transfer parameters are entered in each Pipe Unit View while creating the pipeline elevation profile
75. ce of a 1000 hp compressor to that of a 750 hp compressor will be compared for this application 4 Add a Compressor to the upstream end of the PIPESYS extension Branch 5 To do so open the Elevation Profile page of Branch 5 click on the Pipe Unit and the select the Compressor from the Edit Bar drop down list PIPESYS Application 2 12 5 Figure 12 2 shows the Elevation Profile Page of Branch 5 with the added in line compressor W PIPESYS Extension Branch 5 Joj x Pipeline Dom Distance 0 00 Elevation 2030 00 Distance Elevation Run Rise D Length D Pipeline Unit Angle Label 0 0000 2090 0 0000 0 0000 0 0000 0 000 Compressor 1 Pipe 2110 1980 2110 20001 2113 2 984 Pipe 1 lt empty gt View Cut Copy Paste Global Change Connections _ Worksheet Methads Elevation Profile Stepsize perature Profile 777 L Cooldown Delete Close The performance of the 1000 hp compressor will be evaluated first Figure 2 3 shows the in line compressor Connections page Si Neotec In line Compressor Branch 5 ioj x E Name Compressor 1 r Compressor Locatiorr Distance Elevation Unit Displacement 0 0000 ft 2090 ft 0 0000 ft A Connections Parameters Delete Fuel Requirements 12 5 12 6 Optimization Application
76. ch 1 BSE PYC Foam RS Pipe Coatings L Coati Thickness Conductivity Insert ayer oan g mm W mK S 25 000 0 040 Remove All 1 lt empty gt Connections Dimensions 7 Heat Transfer Pipe Coatings Delete Pipe Unit View 5 2 Adding a Pipe Unit Carry out the following steps to define the pipe units Kei Open the Elevation Profile tab of the Main PIPESYS View If the table is not empty you may add the Pipe Unit to the end of the component list or insert it between two components already in the list Figure 5 7 W PIPESYS Extension Branch 1 ioj xi Pipeline Dom Distance 0 00 Elevation Tn 0 0000 1000 25 00 275 0 5 000 185 0 Delete To add a new Pipe Unit at the end of the pipeline select the cell containing lt empty gt in the Pipeline Unit column Select Pipe from the Edit Bar drop down list If you want to insert a new Pipe Unit within a set of Pipe Units select the Pipeline Unit that will be immediately downstream of the new Pipe Unit and choose Pipe from the Edit Bar drop down list Figure 5 8 W PIPESYS Extension Branch 1 Isp CSET Fitting Pinalina Init SE KS EE T ahal T 5 9 5 9 en ee Adding a Pipe Unit 5 10 The Pipe Segment Location data on this tab is read only It can be changed only on the Elevation Profile tab of the Main PIPESYS view In both ca
77. charge Pressure 8 5 Pump Efficiency 8 4 Rating Factor 7 7 References 13 6 Regulator 9 8 Connections Page 9 8 Parameters Page 9 8 Ce Relative Roughness 5 5 Reports HYSYS Report Manager 3 26 Neotec Maxi Report 3 27 Neotec Mini Report 3 27 Printing Reports 3 27 Report Builder 3 26 Requirements Software 2 3 System 2 3 Results Page 3 25 Rise 3 15 Run 3 15 sS Severe Slugging Check 9 13 Connections Page 9 15 Results Page 9 15 Soil Parameters 5 7 Stepsize Optimizer 3 19 Stepsize Page 3 18 Submerged Pipe 5 5 Suction Pressure 8 5 T Technical Support 1 8 Temperature Profile Page 3 23 U Unit X 9 6 Connections Page 9 6 Parameters Page 9 7 User Interface 3 8 v Valve Coefficient 9 10 Velocity Heads 9 10 W Wall Thickness 5 4 Warranty 1 7 Water Parameters 5 7 Worksheet Page 3 11
78. conditions in the pipeline PIPESYS computes two different severe slugging criteria based on conditions in the system at the point of interest If the actual value for the criterion is less than the critical value the model predicts that severe slugging occurs by filling in the check box in the Slugging column Additionally it should be noted that in the absence of a truly definitive criterion severe slugging should be predicted to be a potential problem unless both Pots 1985 and Fuchs 1987 models say otherwise If the current pipeline profile does not incorporate the geometry necessary for severe slugging to occur a warning will be issued by the software and appear on this tab 9 15 9 16 9 16 Erosion Velocity Check Erosion losses can be significant in sections of pipe where the flow abruptly changes direction 9 8 Erosion Velocity Check Erosion damage i e the wearing away of material may occur as a result of the impact of high velocity liquid droplets It may also be caused by solid particles such as sand entrained in the gas or liquid stream Erosion damage is typically controlled by limiting the maximum gas or liquid velocity in the system PIPESYS can calculate such limiting values for a wide range of flowing conditions Erosion caused by liquid droplets is primarily a concern in gas condensate or gas water systems but may also be a concern in oil gas systems where there is a very high gas oil ratio
79. d Well C respectively These curves can be used to evaluate compressor size that would be most economical for use in a particular pipeline network Locate 686 7 psia and 753 2 psia on the Well A wellhead curve and you should find that these correspond to flows of 11 1 MMSCED and 10 8 MMSCED respectively This indicates that the 1000 hp compressor would increase production by less than 5 over that of the 750 hp compressor It is therefore reasonable to conclude that adding compression to the system is worthwhile since both compressors lower the wellhead pressures by a large amount but the small increase in production may not be enough to justify the choice of the 1000 hp compressor For this example assume that economic and engineering considerations favour installing the 750 hp compressor In steps 4 through 6 it was determined that compression would significantly improve production and that the 750 hp compressor is the better candidate for doing so Now you must find the actual flow rates and wellhead pressures that correspond to having the compressor in the system This will be a process of adjusting the flow rates at each of the wells to manually converge on a particular point on the wellhead curves 7 Locate the flow rates on the wellhead performance curves that correspond to the pressures calculated in Step 6 Reading from the curves these should be Well Pressure psia Flow MMSCFD A 753 2 10 8 B 726 3 9 6 C 693 5 12 4
80. d are interested in only one particular aspect of the case select a Specsheet that confines itself to reporting the parameter of interest For example select the Pressure Temperature Summary for a record of the pressure and temperature at each of the Pipeline Units The Plot button allows you to view your data and results in graphical form such as the one in Figure 3 20 Press the Plot button to display the Plot view Display any of the plots listed on the left hand side by selecting the corresponding radio button The initial size of the plot may be to be too small so press the Pin button to convert the view to a Non Modal state and press the Maximize button To print the plot right click anywhere in the plot area and a pop up menu will appear you can then select Print Plot Flowing Temperature Branch 1 Temperature C Distance m Where two quantities are traced a plot legend is displayed on a yellow rectangular background If this obscures a plot line it can be moved by double clicking in the plot area This action selects the plot area to be modified and you can then drag the plot key to another location 3 27 3 28 3 28 The Main PIPESYS View For more information on the Graph Control see HYSYS Reference Manual 1 Section 5 3 Graph Control To modify the characteristics of the plot right click on the plot area and select Graph Control from the pop up menu that appears The Graph
81. d as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab 9 4 2 Parameters Tab Enter the regulator discharge pressure into the Maximum Exit Pressure input cell The Results group box displays the fluid pressure and temperature at the Inlet and Exit of the regulator once calculations are complete In line Facility Options 9 9 9 5 In line Fittings Fittings such as elbows tees valves and sudden expansions create a pressure drop in the system For long pipelines or multiphase flow it is rarely necessary to account for pressure losses through pipe fittings unless there are a significant number of fittings This is simply because the magnitude of the pressure drop caused by the fittings is small compared to the pressure losses brought about by all other causes There are a number of methods used to specify or calculate the pressure drop due to a fitting but you may select any of these provided you have suitable data Neotec In line Fittings Branch 1 ioj x Name Fitting 1 pr 7 e Dh r Fittings Locatiorr Distance Elevation Unit Displacement 2300 m 280 0 m 3012 m a Connections Parameters Delete 9 5 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab 9 5 2 Parameters T
82. d coatings are entered here This view also allows you to specify one of a number of external environments that affect the heat transfer from the flowing fluid including below ground open air and under water settings Hl Neotec Pipe Unit Branch 1 RISE 2 Name Pipe 3 Pipe Segment Location Distance Elevation Unit Displacement 2400 m 100 0 m 2481 m lt B Connections Dimensions Heat Transfer Delete Pipe Coatings 5 1 Connections Tab Some basic information about the Pipe Unit is displayed on this tab The pipe unit name and its profile location data appear here The location data is repeated from the Elevation Profile tab of the Main PIPESYS View and is read only here If you wish to change the Distance Elevation or Unit Displacement data you must return to the Main PIPESYS View and go to the Elevation Profile tab 5 1 1 Dimensions Tab The Dimensions tab features a built in data set with a comprehensive range of pipe sizes and wall thicknesses If you are using a standard pipe size in your project you need only select a nominal diameter and a pipe schedule and PIPESYS will automatically fill in the other input cells You can also use non standard pipe sizes by manually entering all relevant data 5 3 Connections Tab Hl Neotec Pipe Unit Branch 1 ISE 2 Pipe Dimensions Nominal Diameter I Pipe Schedule 40 x Outside Diameter 8
83. dmard A DeSouza B Math Garry A Gregory Ph D PEng Lisa Hugo BSc BA Chris Strashok BSc 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 Website www hyprotech com Technical Support support hyprotech com Information and Sales Info hyprotech com Detailed information on accessing Hyprotech Technical Support can be found in the Technical Support section in the preface to this manual Table of Contents a S U Tasse Tee aT 1 2 1 2 How This Manual Is Organized sese ee eee ee eee 1 5 UE GR 1 e E TEE 1 5 L t Copyright seen aeeoa ied 1 6 1 5 Acknowledogemente AAA 1 6 AB OT Te 1 Eesen Gast essisindeesieaesbieses esi aaieenede 1 7 1 7 Technical SUpport A 1 8 Installation neen seenen ER EK Ek KR KEREN KKK eene 2 4 2 1 System Requirements eee eee eee ee eee 2 3 2 2 Software Requirements eee eee ee eee eee 2 3 2 3 Installing BIREN entstoe cece eet giclee 2 4 The PIPESYS View ee EEREER KEE RRE KER KEE KE Kenne 4 1 dt PIPESYS Feature seed
84. e 1 Run ft 1167 Pipe Unit View Nominal Diameter 4 Inches Pipe Schedule 40 Centre Line Depth Default Temperature Profile Ambient Temperature F 40 11 14 PIPESYS Application mm Application 1 11 15 11 3 5 The Fourth PIPESYS Extension Branch 3 of this pipeline system is represented by the fourth PIPESYS extension Three Pipe Units in the elevation profile matrix correctly characterize the changes in elevation occurring over the length of the pipeline To save time add and define 15 The following table contains the information required to complete Pipe 1 and then use the Copy the fourth PIPESYS extension and Paste buttons to create Pipe 2 and Pipe 3 Connections Page Name Branch 3 Inlet Stream Well C Outlet Stream PS3 Energy Stream ES3 Elevation Profile Distance ft 0 Page Elevation ft 2125 Pipeline Unit Pipe 1 Pipe 1 Elevation ft 2077 Pipe 1 Run ft 528 Pipeline Unit Pipe 2 Pipe 2 Elevation ft 2080 Pipe 2Run ft 334 Pipeline Unit Pipe 3 Pipe 3 Elevation ft 2077 Pipe 3 Run ft 670 Pipe Unit View All Nominal Diameter 3 Pipe Units Identical Inches Pipe Schedule 40 Centre Line Depth Default Temperature Profile Ambient Temperature F 40 11 15 116 Setting Up the Case Setting Up the Case 11 16 11 3 6 The Fifth PIPESYS Extension The fifth and final PIPESYS extension for this case represents Branch 5 of the pipeline system In t
85. e already specified Brake Power you cannot supply a value for this parameter e Suction Pressure Generally the suction pressure or pressure immediately upstream of the pump is known from a calculation of the pressure to that particular location along the pipeline e Discharge Pressure The calculated pressure immediately downstream of the pump e Suction Temperature The temperature of the fluid at the pump inlet e Discharge Temperature The temperature of the fluid at the pump outlet You are not required to enter any data values for these parameters if you are using the pump performance curve method In fact you will be unable to enter any parameter values on this tab if the Activate Curve check box is checked as the parameter input cells will change to read only mode 8 1 3 Curve Tab If the Activate Curve check box on the Parameters tab is checked the Pump Performance Curve group box will appear as displayed in Figure 8 3 and be ready for data entry on this tab Figure 8 3 i Neotec In line Pump Branch 1 ll xj l l EI Pump Performance Curve Units for Flow Units for Head Flow Basis ft Liq Vol Flow Efficiency 6 0 0 850 8 2 0 850 lt empty gt lt empty gt lt empty gt Insert Remove Remove All Sort Connections 7 Parameters Curve Delete 8 6 8 6 In line Pump View Use the matrix on this tab to define the Head vs Flow Rate and the E
86. e components and data All units of measurement in this example are SI but feel free to change these to whatever unit system you are accustomed to using For this case a simple pipeline consisting of three pipe units and a pig launcher will be built to demonstrate the PIPESYS procedures Figure 4 1 shows a schematic of these four components with coordinate axes Elevation Pig aa Launcher 1200 300 2900 280 300 200 100 2400 100 Pipeline age Origin I 0 1000 2000 3000 Distance 4 1 Flow Sheet Set Up Before working with the PIPESYS extension you must first create a HYSYS case In the Simulation Basis Manager create a fluid package using the Peng Robinson equation of state Add the components methane ethane propane i butane n butane i pentane n pentane n hexane nitrogen carbon dioxide and hydrogen sulfide Property Package Components Peng Robinson C1 C2 C3 i C4 n C4 i C5 n C5 C6 Nitrogen CO2 H2S 4 3 Adding the PIPESYS Extension Create a stream called Inlet in the Main Simulation Environment and define it as follows Name Inlet Vapour Fraction 1 00 Temperature C 45 Pressure kPa 8000 Molar Flow kgmole h 300 signifies required input EES Plow ea 6595 LiqVol Flow m3 h 17 88 Heat Flow kJ h 2 783e 07 Comp Mass Frac methane 0 7822 Comp Mass Frac ethane 0 0803 C
87. e list of materials in the drop down bar Pipe Unit View 5 5 Hl Neotec Pipe Unit Branch 1 iof xj Ae Default Steel bare average field conditions Default Steel bare average field conditions _ r Pipe D Steel bare new Steel coated new Cast Iron bare Cast Iron coated Concrete rough Pipe Schedule yu IS e Absolute Roughness The standard sand particle equivalent roughness rating used to define the effective roughness of the pipe Pipe material service time and environmental conditions can be factors in the determination of this value PIPESYS has a comprehensive data set of roughness values cross referenced to pipe material types Once you have chosen a pipe material a corresponding roughness value will appear in this input cell This parameter can be adjusted to match measured frictional pressure losses in existing pipelines e Relative Roughness This value is calculated as the ratio of absolute roughness to inside pipe diameter 5 1 2 Heat Transfer Tab On this tab a number of different heat transfer environments can be specified and the parameters that influence the rate of heat transfer from the flowing fluid specified Figure 5 4 shows the Heat Transfer tab for the Pipe Unit view The following environments are available in the Heat Transfer Environment group box e User Specified If special circumstances preclude selection of any of the other environments or you wish to run your
88. e program that a particular parameter will be copied to other Pipe Units using the Global Change feature Request a Global Change for a particular parameter by entering the new parameter values into the input cells Once you have entered all the changes that you want to make press the Apply button and the Global Change dialog box will appear with a list of all the Pipe Units in the profile Select the Pipe Units in the list that will be included in the global change and press the OK button The program will then make the specified parameter the changes to all of the Pipe Unit parameters that were checked 3 4 5 Stepsize Tab PIPESYS computes the change in pressure due to friction hydrostatic head and kinetic energy and the change in temperature for the flowing fluid s These calculations are dependent on the physical characteristics and orientation of the pipe and its surroundings They are also dependent on the fluid properties i e density viscosity enthalpy phase behaviour etc Since these properties change with pressure and temperature it is necessary to choose some interval over which the average properties can be applied to the calculations i e a calculation length or step sufficiently small for property changes to be nearly linear The PIPESYS View 3 19 PIPESYS Extension Branch 1 RE Stepsize and Tolerances Pipe Lengths Pressure Convergence Initial dP Guess 68 95 kPa Minimum dP step 2
89. eate multiple streams and multiple pipeline units This is especially useful if pressure losses in the side stream are either inconsequential very short lines or irrelevant to the analysis What would otherwise be a complex system of pipes can often be reduced to a few pipelines with side streams Data for the calculations are entered in the Parameters tab of the Side Stream Pipeline Unit and main line results are displayed for the streams before and after the side stream In line Facility Options 9 9 1 Connection Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab Figure 9 10 Cl Neotec Side Stream Branch 1 ell Name fSideStream 1 Distance Elevation Unit Displacement_ Side Stream Location 2900 m 280 0 m 3012 m 2 Connections Parameters Delete 9 9 2 Parameters Tab This page is used to define the basic characteristics of the side stream In the Flow Direction group box there are two radio buttons from which you can choose the direction of the flow Inflow or Outflow Selecting the flow direction and flow rate specifies addition or removal of flow The side stream s flow rate can be specified as a e molar flow rate e mass flow rate ora standard liquid volume flow rate For an inflow stream when calculating the flowing fluid temperature
90. er is the sum of the theoretical power the power needed to compress an ideal gas and the additional power needed to compensate for compression losses Typically mechanical losses amount to 1 to 3 of the total brake power There are three ways of specifying the mechanical losses 1 Overall Efficiency This is a number less than one where Mechanical Losses 1 Mechanical Efficiency x Gas Power 2 Actual Losses Expressed as an actual power value in units consistent with the other compressor parameters 3 Exponent of Gas Power This value is used in the expression Mechanical Losses Gas Power A typical value for the exponent x is 0 4 7 1 6 Requirements Tab Here the operational requirements for your compressor are displayed These are the values calculated by PIPESYS and broken down on a per stage basis The Power Requirements group box contains a summary of required Gas Power Gas Head Losses and Brake Power for each stage and a total of these values for the entire compressor The Theoretical Cooling group box displays any cooling that was required if this proved to be necessary for each stage and the compressor outlet The sum of all duty required for cooling the gas is displayed in the Total Cooling cell 7 11 The Compressor View Figure 7 6 Si Neotec In line Compressor Branch 1 of x l A Power Requirements Losses Stage Brake Power Gas Power Head kw m lt empty g
91. ess to complete the Dimensions tab PIPESYS will use a default value for the roughness based on the material type that you select or if you choose User Specified for the Material Type you will be able to enter a specified roughness value i Neotec Pipe Unit Branch 1 BIS x SSS SS Pipe Dimensions Nominal Diameter 4 Inches zl E Pipe Schedule Outside Diameter 114 300 mm all Thickness 6 020 mm Inside Diameter 102 260 mm Default Roughnesses Default Steel bare bsolute Roughness 0 04572 mm Relative Roughness 0 000447 Connections _ Dimensions Delete Heat Transfer Pipe Coatings 5 On the Heat Transfer tab select the pipe surroundings for your case in the Heat Transfer Environment group box mHeat Transfer Environment C User Specified Buried merged Above Ground C Buried Submerged C Buried Exposed 5 11 eng AddingaPipe Unit Adding a Pipe Unit PIPESYS can calculate the heat transfer to the surroundings based on the characteristics of one of the external environments Buried Submerged Above Ground Buried Submerged or Buried Exposed A matrix of required parameters as in Figure 5 13 will appear in the group box on the right of the form when Heat Transfer environment is chosen When User Specified is selected an overall heat transfer coefficient for the system may be entered Buried Pipe Parameters en Default Conductivities De
92. essseeensseeensseeensees 9 3 4 1 CONNMECTIONSPFTAD sss vs T asees eee e eee e enoe 10 3 4 2 Worksheet Tab essen EE 11 3 43 Methods Tab EEGEN EE 11 3 4 4 Elevation Profile Tab 13 3 4 5 Stepsize Tab 18 3 4 6 Cooldown Tab 20 3 4 7 Temperature Profile Tab 23 3 4 8 Results Tab we 25 3 4 9 laie UEI coco HT J 28 3 1 The PIPESYS View 3 3 The PIPESYS Extension is a pipeline hydraulics software package used to simulate pipeline systems within the HYSYS framework The PIPESYS Flowsheet functions in the same manner as any HYSYS unit operation or application in terms of its layout and data entry methods The view consists of 10 worksheet tabs that may be accessed through the tabs At the bottom of each worksheet is a status bar which guides data entry and indicates required information as well as indicating the status of the PIPESYS simulation once the calculation has been initialized You define the pipeline by entering pipe units and in line facilities and specifying their length and elevation gain By using several pipe segments you can create a pipeline which traverses a topographically varied terrain PIPESYS has a comprehensive suite of methods and correlations for modelling single and multiphase flow in pipes and is capable of accurately simulating a wide range of conditions and situations You have the option of using the default correlations for the PIPESYS calculations or specifying your own set from the
93. etailed results by pressing the Detail button on the Results tab This will bring up the Pipe Segment Results view which displays a comprehensive array of hydraulic data for each calculation segment 25 Check to see if the program encountered any difficulties during the calculation phase by opening the Messages tab For this case there should have been no difficulties and the tab should read No calculation warnings encountered 26 To open the PFD press the PFD button on the Button Bar Right click anywhere on the PFD view to obtain a pop up menu 27 Select Choose Label Variable from the menu and the Select Variable for PFD Labels dialog box will appear You can use this dialog to display a number of process variables right on the PFD 28 Press the Change Variable button and choose Pressure from the Choose Label Variable dialog box 10 15 1046 Applying a Global Change 0 16 Applying a Global Change 29 Press the OK button on the Choose Label Variable dialog box and the inlet and outlet pressures will be displayed on the PFD See Figure 10 18 Figure 10 18 Gas Condensate Pipeline 1150 psia 1126 psia Pipeline Energy Transfer 30 To print the PFD schematic right click anywhere on the PFD and select the Print PFD command from the pop up menu 10 3 Applying a Global Change By using the Global Change feature you can quickly change the pipe size for all pipe units and then let PIPESYS recalculate t
94. f the computer Note that for computers which have the CD ROM Autorun feature enabled steps 3 and 4 will be automatically performed From the Start Menu select Run In the Run dialog box type d setup exe and click on the OK button where d corresponds to the drive letter of the CD ROM drive 5 Select PIPESYS from the following view to start the installation HYSYS PIPESYS License Server View Readme Browse CD AYPROTECH LIFECYCLE INNOVATION 2 4 6 The first dialog that appears welcomes you to the installation program and displays the name of the application you are trying to install If all of the information is correct click the Next button 7 The following dialog provides information regarding Hyprotech s new software security system Please read the information presented on this screen it is important Click the Next button to continue For additional information on the properties of HYSYS Unit Operations refer to the HYSYS Steady State Modelling Manual Installation 2 5 8 Specify a destination folder where the setup will install the PIPESYS files If you do not wish to install the application in the default directory use the Browse button to specify the new path When the information is correct click the Next button 9 The installation program will then allow you to review the information that you have provided If all of the information is correct click the
95. fault Steel Pipe Conductivity 48 461 Wim See Section 5 1 2 Heat Centre Line Depth 0 914m Soil Type Default Transf ad Tab for ine Soil Conductivity 0 865 W m K_ definitions of the pipe Inside Film Coefficient lt empty gt environment parameters PIPESYS requires sufficient data to calculate the heat transfer from the fluid to the surroundings Use the Default button to fill in required values for which you have no field data 6 In the Inside Film Coefficient group box select Specified to enter the resistance to heat transfer through the fluid film on the inside wall of the pipe Select Calculated to have PIPESYS calculate the value for you The default value is representative for turbulent flow Inside Film Coefficient Calculated C Specified This completes the information required for adding a pipe unit 5 12 Global Change Feature 6 1 h Global Change Feature 6 1 Global Change View sssssssseseessecseessesseesenseeeseesenseneseeseessesseesseenensenseneas 4 6 14 Connections Tab EE 4 6 1 2 Dimensions TAD if csvencececceencanccoteantencanccotenecsrcencevteabestenteevtengMroneeaveereense 5 6 1 3 Heat Transfer Tab ccccsccssscscccssessssssseecssesssstsseccscessceenpeitscesesenseseteteceses 6 6 4 4 Pipe Coatings 2 iccgs ieee ra eer eit ne NEE 6 6 2 Global Change Procedure ssscecsesseesseseeeseeeeneseeseeeseeseneseesenesenseneneeseneae 7 6 3 Making a Global Change
96. fficiency vs Flow Rate curves for your pump Curve data should be available from the pump manufacturer specification sheets Different units for the Flow and Head data may be selected from the drop down input cells above the matrix If you have not checked the Activate Curve check box on the Parameters tab the message No data is required as pump curve is not activated will be displayed on this tab In line Facility Options 9 In line Facility Options RRIT Oat E BE 3 9 1 1 Connections Tab Ann cretion ee i ei ee id 3 DL Parameters Tabs TT a a ai 3 9 2 In line Coole TTT 4 9 2 1 Connections Tabi renee Jn sesa eee sees esse seene enen 5 9 2 2 Parameters Tab OS Witness EEE EEEE OE EET OE 6 93 Connections Tab sss sss saez B enen 6 9 3 2 Parameters Tab 9 3 3 Results Tab eenn 9 4 In lime REQUIATOL ccetseceeeeeeeeesseeeseeeeseeseneeseeeeseeessnesseeeesaeessnesseeessneeseneeees 8 9 4 1 eelerer len EENEG 8 9 4 2 ParametoisMaBP CLAM EE 8 9 5 IM liMe EIttMOS2 ccsccesecsscsscssceasersMeemterceccesscsccnsesencersasseccesensersessecsessesensseneacenss 9 9 5 1 Connections Tab re ccesccecsssecssecsacssctasesecceensccecssseecensscerssstecsasees 9 925 2 Parameters Tab MMM oleic cha ce linecoa ENEE edd 9 9 6 Pigging Slug ei ET EE 11 9 6 1 Connections Tab iavcccisicscviseeseccssevssiudeccorsevsvaceviecveneetacnvasvuantebncrvenweansey 12 IGOA ROINE E MEN 12 9 7 Severe Slugging Check
97. fficient information in a Pipeline unt Delete Clase 3 13 am The Main PIPESYS View The Main PIPESYS View When defining the geometry of the pipeline you must be aware of the distinction between the two types of components The set of pipeline components in PIPESYS collectively known as Pipeline Units includes both Pipe Units which are straight sections of pipe and In line Facilities which are pieces of equipment such as compressors pumps fittings and regulators Pipe Units have a starting point and an ending point and occupy the intervening space but in line facilities are considered to occupy only a single point in the pipeline When a Pipe Unit is added to the pipeline the data required to fix the position ofits starting point and its ending point must be specified The starting point of the Pipe Unit is generally already determined since the Pipe Unit is attached to the previous unit in the pipeline All that remains is to enter the data that PIPESYS needs to fix the end point which can be done in a number of ways You can fill in the Distance and Elevation cells which define the end point of the Pipe Unit relative to the Pipeline Origin Alternatively you can use some combination of the Run Rise Length and Angle values to fix the end point relative to the Pipe Unit s starting point For instance you could enter a value of 10 in the Angle cell and 300 ft in the Run cell to fix the end point as being at a hori
98. fied Discharge Pressure Results Suction Pressure lt empty gt Discharge Pressure lt empty gt Suction Temperature lt empty gt Discharge Temperature lt empty gt lt Connections Parameters Curve Delete The parameters required to perform calculations with the built in pump relation are Brake Power or Specified Discharge Pressure these are mutually exclusive parameters and Efficiency The rest of the parameters on this tab are used to display results of the calculations These parameters are defined as follows e Brake Power The power required to operate the pump Enter a value here or in the Specified Discharge Pressure input cell to provide enough data to perform the pump calculation e Fluid Power The actual power delivered to the fluid system or the work done on the fluid per unit of time The fluid power is related to the brake power by the relation pup 22 n where BHP Brake Horse Power FHP Fluid Horse Power n pump efficiency e Efficiency The overall pump efficiency A value of 0 70 is typical for some pumps but you should consult the manufacturer s data sheet to obtain a value which properly represents the capabilities of your pump This value is required by the program to calculate pump performance In line Pump 8 5 e Specified Discharge Pressure The exit pressure from the pump Either the Discharge Pressure or the Brake Power must be specified If you hav
99. global changes to Select All UnSelect All 5 Press the Close button on the Pipe Property view The changes will be registered with the program but will not be implemented until this view is closed 10 17 1048 Applying a Global Change 0 18 Applying a Global Change 10 18 6 The program will immediately start to recalculate for the 10 diameter When the Object Status displays Converged you can look at the calculated results and compare them with the values obtained for the 12 pipe You have now completed the Gas Condensate pipeline example For a more in depth exercise in using the PIPESYS Extension see Gas Condensate Gathering System and Optimizing the Gas Condensate Gathering System in the PIPESYS Applications Binder PIPESYS Application 1 11 1 I PIPESYS Application 11 1 Gas Condensate Gathering System esssseessesessseeeeeseeseeeeeeeeeenseneee 3 11 2 Setting up the FloWShEeEet cceeceeeeeseeneeeseeseeeseeseeeseeeseeseesseseesseaeeeeeenes 6 11 3 Setting Up the CaS nirmi nienean aeania peee tana oaae eiaeia daue 8 11 3 1 Adding the First PIPESYS Extension 8 11 3 2 The Second PIPESYS Extension wi 12 11 3 3 Adding a Mixer vat 18 11 3 4 The Third PIPESYS Extension 14 11 3 5 The Fourth PIPESYS Extension ven 15 11 3 6 The Fifth PIPESYS Extension we 16 11 3 7 The Second Mixer a IZ 11 3 8 Well Stream Information A 18 DAA Teen e EEN rnessnnecccerssensnnseceressin
100. hange In this case the change will apply to all pipe units so press the Select All button to highlight all the pipe units Figure 6 15 shows the dialog box with the selected pipe units Figure 6 14 Global Change Dialog Box x Select the pipeline objects to apply the global changes to UnSelect All OK Cancel 6 11 e Making a Global Change Making a Global Change 6 12 The Global Change view must be closed to initialize the PIPESYS calculations 6 Press the OK button on the Global Change view and PIPESYS will recalculate the extension using the new diameter value This completes the Global Change example The following table compares calculated results for the Outlet stream for the 3 and 4 diameter pipeline Diameter 3 4 Vapour 1 00 1 00 Temperature C 27 06 28 06 Pressure kPa 7182 73 7630 47 Molar Flow kgmole h 300 00 300 00 Mass Flow kg h 6504 44 6504 44 Liq Vol Flow m3 h 17 78 17 78 Heat Flow kj h 2 79916e 07 2 80155e 07 In line Compressor 7 1 7 in line Compressor 7 1 The Compressor View sssscsscssseeesessseeseessneseeseneseeseeeseeseneseesenesenseeesenteneas 3 711 Connections Ee EE 3 7 1 2 Parameters TAD fs csvencecsctncanccoteantencanccosesecsrcevcevteabestenteevtengMrenecaveersessl 4 TEAS CUNG rT eaan n Aaa a a i a ann 7 7 1 4 Fuel Requirements Tab ccccscccssssescesccsessesssceseegetecssses
101. he flow parameters for the extension 1 Open the Elevation Profile tab on the Main PIPESYS View select the first pipe in the list and press the Global Change button 2 Select the Dimensions tab Choose 10 Inches from the Nominal Diameter drop down list and select 40 from the Pipe Schedule drop down list You should notice that the Change check box beside the Nominal Diameter drop down list became checked as soon as you made these changes This is to notify you that the program is aware that this parameter has changed and that this change can be duplicated for other Pipe Units in the pipeline 10 16 Gas Condensate Tutorial wm Tutorial 10 17 Figure 10 19 Neotec Pipe Unit Gas Condensate Pipeline ioj x z Pipe Dimensions Nominal Diameter Pipe Schedule 40 z Outside Diameter 10 020 in Change Default Roughnesses bsolute Roughness Relative Roughness Default Steel bare 0 00180 in 0 000180 Connections Dimensions Heat Transfer_ Pipe Coatings Se Des pa Press the Apply button on the Global Change property view gt The Global Change Dialogue Box will appear This dialogue box allows you to specify which Pipe Units will be subject to the changes In this case you are changing all of them so press the Select All button see Figure 10 20 and press the OK button Figure 10 20 Select the pipeline objects to apply the
102. head of the pig is occupied by the slug assuming that the pipeline is completely filled with liquid Dumping time is the time required for the slug to flow out of the pipeline under steady state conditions Figure 9 7 CH Neotec Pigging Slug Size Estimation Branch 1 lle x Pigging Slug Pig Velocity as fraction of Transit Time Slug Slug Dumping gas velocity for pig Volume Length Time 0 50 lt empty gt lt empty gt lt empty gt lt empty gt 0 55 lt empty gt lt empty gt lt empty gt emt 0 60 emp lt empty gt lt empty gt emp 0 65 lt empty gt lt empty gt lt empty gt lt empty gt 0 70 lt empty gt lt empty gt lt empty gt lt empty gt 0 75 ___ lt empty gt em lt empty gt emp 0 80 lt empty gt lt empty gt lt empty gt emp 0 85 lt empty gt lt empty gt lt empty gt lt empty gt 0 90 lt empty gt lt empty gt lt empty gt lt empty gt 0 95 lt empty gt lt empty gt lt empty gt lt empty gt 1 00 lt empty gt lt empty gt lt empty gt lt empty gt Connections Results Delete 9 7 Severe Slugging Check The Severe Slugging Check is an application of two different criteria to predict the likelihood of severe slugging at a particular point in the pipeline Severe slugging is a phenomenon associated with vertical or near vertical risers which are a common feature of pipelines connected to offshore
103. her at the suction side of the compressor or at the suction side of any subsequent stage the liquid is removed and compression is computed on the basis of the resulting vapour phase Any liquid removed is recombined with the outlet stream from the compressor at the discharge pressure and temperature conditions Furthermore a warning is issued to alert the user that some liquid separation occurred prior to compression In the Liquid Removed at Suction group box the amount of liquid removed at each stage of the compressor is reported For the case when a stream is determined to be single phase liquid either at the suction side of the compressor or any subsequent stage the entire stream is compressed and a warning Compressor Single phase liquid encountered is posted on the Messages tab Thus the compressor is capable of handling dense phase fluids that are reported by the equation of state to be single phase liquid 7 2 Adding a Compressor Carry out the following steps to add a compressor to your pipeline 1 Open the Elevation Profile tab of the Main PIPESYS View You can add the compressor to the end of the list of Pipeline Units or insert it at an intermediate point in the profile 2 To add the new compressor at the end select the cell containing lt empty gt in the Pipeline Unit column and choose Compressor from the Edit Bar at the top of the View Figure 7 8 W PIPESYS Extension Branch 1 5 x Compressor l
104. hese include but are not limited to the following list MSDOS and Windows are registered trademarks of Microsoft Corporation IBM is a registered trademark of International Business Machines Ltd Neotec and Hyprotech hereby agree to grant you a nonexclusive license to use the software program subject to the terms and conditions set forth in the license agreement S E 1 6 Warranty Neotec Hyprotech or their representatives will exchange any defective material or program disks within 90 days of the purchase of the product providing that the proof of purchase is evident All warranties on the disks and manual and any implied warranties are limited to 90 days from the date of purchase Neither Neotec Hyprotech nor their representatives make any warranty implied or otherwise with respect to this software and manuals The program is intended for use by a qualified engineer Consequently the interpretation of the results from the program is the responsibility of the user Neither Neotec nor Hyprotech shall bear any liability for the loss of revenue or other incidental or consequential damages arising from the use of this product 1 7 Technical Support 1 7 Technical Support There are several ways in which you can contact Technical Support If you cannot find the answer to your question in the manuals we encourage you to visit our website at www hyprotech com where a variety of information is available to you includi
105. his segment the total gas flows from Wells A B and C are merged and the endpoint of the extension is the gas plant 16 Enter the information for the final extension as defined in the following table Connections Page Name Branch 5 Inlet Stream FS5 Outlet Stream PS5 Energy Stream ES5 Elevation Profile Distance ft 0 Page Elevation ft 2090 Pipeline Unit Pipe 1 Pipe 1 Elevation ft 1980 Pipe 1 Run ft 2110 Pipe Unit View Nominal Diameter 6 Inches Pipe Schedule 40 Centre Line Depth Default Temperature Profile Ambient Temperature F 40 PIPESYS Application mm Application 1 11 17 11 3 7 The Second Mixer A second Mixer merges the streams from Branches 3 and 4 with the outlet stream entering Branch 5 17 Adda Mixer named Junction 2 to your simulation Inlet streams for the mixer are PS3 and PS4 and the outlet stream is FS5 See Figure 11 11 for the completed Connections Page Design Name funciona Connections Parameters User Variables Notes Inlets Outlet ES FS5 x EEE E lt lt Stream gt gt 18 On the Parameters page of the Mixer select the Equalize All radio button in the Automatic Pressure Assignment group box 11 17 Bests 1 18 Results 11 18 11 3 8 Well Stream Information To finish the case and have PIPESYS complete the calculation the following stream parameters for the wells are required 19 Finish specify
106. ile E Ambient Temperature C Specify temperatures Distance Elevation Cum SE Surroundings Type Ambient T F 3400 3401 Pipe 1 40 00 Buried 8550 2530 8563 Pipe 2 40 00 Buried 1 530e 004 Dem 1 531e 004 Pipe 3 40 00 Buried 2 230e 004 2550 2 231e 004 Pipe 4 40 00 Buried Connect Worksheet Elevation Profile Cooldown Temperature Profile Delete 22 Return to the Connections tab of the Main PIPESYS View Since data entry is complete you can instruct the program to begin calculations by removing the check in the Ignore this UnitOp During Calculations check box After a few seconds the program will find a solution and announce success by displaying Converged on the Object Status at the bottom of the Main PIPESYS View 10 14 Gas Condensate Tutorial wm Tutorial 10 15 23 You can view the results for each Pipe Unit on the Results tab on the Main PIPESYS View This tab shows pressure losses fluid temperatures and liquid holdup for each Pipe Unit See Figure 10 17 Figure 10 17 SY PIPESYS Extension Gas Condensate Pipeline BIS Cum Length Pipeline Unit Pipe a0 TT 1088 S EN Seef Pipe 8563 1146 108 5 5 185 0 3436 Pipe 2 Pipe 1 531e 004 1134 106 5 12 89 1 976 Pipe 3 Pipe 2 231e 004 1126 104 9 7 960 1 588 Pipe 4 Detail Report Plot 24 You can view more d
107. ine e Heater Adds heat to the flowing fluid s e Cooler Removes heat from the flowing fluid s e Unit X A black box component that allows you to impose arbitrary changes in pressure and temperature on the flowing fluid s e Regulator Reduces the flowing pressure to an arbitrary value e Fittings Used to account for the effect of fittings such as tees valves and elbows on the flowing system e Pigging Slug Size Check An approximate procedure for estimating the size of pigging slugs e Severe Slugging Check A tool for estimating whether or not severe slugging should be expected e Erosion Velocity Check Checks fluid velocities to estimate whether or not erosion effects are likely to be significant 3 2 Adding PIPESYS Adding a PIPESYS Extension to a HYSYS Case Carry out the following steps to add a PIPESYS Operation to a HYSYS Case 1 Your first task is to create a HYSYS Case suitable for the addition of the PIPESYS Extension As a minimum you must create a Case with a Fluid Package two Material Streams and an Energy Stream 2 With the Case open click on the Flowsheet command from the Menu Bar and click Add UnitOp Select the Extensions radio button and choose the PIPESYS Extension from the Available Unit Operations group box on the UnitOps view The Main PIPESYS View will open and be ready for input 57 UnitOps Case Main lol x r Categories Available Unit Operations SCH C AN Un Ops gtens
108. ine Origin e Inside Diameter Inside diameter of the pipe over the length of the Segment e Pressure The fluid pressure at the downstream end of the Segment e Temperature The fluid temperature at the downstream end of the Segment 3 25 3 25 3 26 The Main PIPESYS View e DeltaP Friction The pressure loss across the Segment due to friction e DeltaP Head The loss or gain in the elevation head across the Segment e Liq Volume Fraction The volume fraction of the fluid in the Segment in the liquid phase e Press Gradient The pressure change per unit of pipe length e Iterations The number of times that the program repeated the solution algorithm before convergence was obtained e Gas Density The average density of the gas phase in the Segment e Liquid Density The average density of the liquid phase in the Segment e Gas Viscosity The average viscosity of the gas phase in the Segment e Liquid Viscosity The average viscosity of the liquid phase in the Segment e Vsg The average superficial velocity of the gas in the Segment e Vsl The average superficial velocity of the liquid in the Segment e Flow Pattern When multiphase flow occurs the flow pattern or flow regime in a Segment is classified as being one of the following types Stratified Wave Elongated Bubble Slug Annular Mist Dispersed Bubble Bubble or Froth When the fluid system is in single phase flow Single Phase
109. ing streams Well A Well B and Well C with following data Well A Temperature F 105 Pressure psia 1060 Molar Flow MMSCFD 8 6 Well B Temperature F 115 Molar Flow MMSCFD 7 4 Well C Temperature F 110 Molar Flow MMSCFD 10 1 20 Save your case as network hsc 11 4 Results 1 Go to the Material Streams page of the main Workbook The results calculated for the product streams should appear as follows Well B Well C PS1 PS2 0 9655 0 9709 0 9688 0 9586 0 9640 105 0 115 0 110 0 31 81 100 4 1060 1044 1018 3933 393 3 SE LP 1109 9443 BIB 2 257e 004 1 942e 004 2 651e 004 2 257e 004 1 942e 004 4215 3627 4951 4215 3627 LL _ 3 641e 007 3 117e 007 4 262e 007 _ 3 656e 007 _ 3 134e 007 3 855e 004 23 837e 004 3 843e 004 3 871e 004 3 857e 004 PS3 PAI PS5 ESA FS5 0 9658 0 9597 0 9607 0 9612 0 9622 102 8 92 62 93 73 95 75 96 53 972 1 972 1 963 0 993 3 972 1 Molar Flow lbmole hr 1103 _ 1757 2866 __1757 2866 Mass Flow lb hr 2 651e 004 4 199e 004 6 850e 004 4 199e 004 6 850e 004 Liquid Volume Flow barrel day 4951 7842 1 279e 004 7842 1 279e 004 Heat Flow Btu h Atert Eifer 1 108e 008 6 790e 007 1 107e 008 3 850e 004 3 068e 004 3 065e 004 3 965e 004 3 961e 004_ q To optimize the performance of the gas condensate gathering system created in this example see PIPE
110. ion BEES Erens Saturate Extension Cancel C Vessels C Heat Transfer Equipment Rotating Equipment Piping Equipment Solids Handling C Reactors C Prebuilt Columns C Short Cut Columns Sub Flowsheets Logicals Extensions C User Ops A gas condensate system is a good example of a gas based with liquid system because while liquid is often present only the gas component is present under all conditions The PIPESYS View 3 5 Select Material Streams from the Inlet and Outlet drop down lists on the Connections tab of the PIPESYS view Select an Energy Stream from the Energy drop down list If you have not yet installed these streams in the Case they can be created by directly entering their names on the Connections tab To define the stream conditions right click on the name and select View Open the Methods tab Decide on the most appropriate description of your fluid system gas based with liquid or liquid based with gas Your choice is not determined so much by the relative amounts of gas and liquid as it is by the phase that is present under all conditions of temperature and pressure in the pipeline Select the radio button in the Recommended Procedures group box that corresponds to the best description of your system If the system is determined to be single phase in the course of finding a solution all multiphase options will be ignored K PIPESYS Extension Branch 1 BRISE
111. is reported here e Surface Tension The liquid property caused by the tensile forces that exist between the liquid molecules at the surface of a liquid gas interface PIPESYS Specsheets are available to the HYSYS Report Manager and can be added to a Report using the Report Builder For more information on using the HYSYS Report Manager and Report Builder see Section 6 2 Reports in the HYSYS Reference Manual You can also preview and print PIPESYS Specsheets directly from the Results tab Press the Report button to bring up the Select a Specsheet dialogue Here you can choose from a number of different Specsheets E iol x PIPESYS Extension Branch 1 Available Specsheets 3 26 Neotec Maxi Report Connections Calculation Procedures Stepsizes and Tolerances Pipeline Units Profile Pipe Dimensions Heat Transfer Data TY Proof Quality C ASCII Output Preview Print Hines a E es Cancel The PIPESYS View 3 27 The Neotec Mini Report provides a summary of selections and results from the PIPESYS case The Neotec Maxi Report includes the same information as the Mini Report and has additional detailed calculation results for the Pressure and Temperature profiles and Fluid Transport properties Press the Preview button to view the formatted Specsheet on the screen or press the Print button to print it directly If you do not need the complete report results from the PIPESYS case an
112. l 66 2 381 1020 Fax 66 2 381 1209 Tel 401 330 0125 Fax 401 311 3463 Tel 52 5 546 5440 Fax 52 5 535 6610 Tel 55 11 533 2381 Fax 55 11 556 10746 Tel 54 11 4555 5703 Fax 54 11 4551 0751 Tel 58 2 264 1873 Fax 58 2 265 9509 Tel 7 095 202 4370 Fax 7 095 202 4370 Internet Website www hyprotech com E mail info hyprotech com 1 12 Technical Support Installation 2 1 2 Installation 2 1 System RequireMent cccsceecssceeesseeeeeseeseeeseeseeeesesseessesseeseesseeseneseasenesents 3 2 2 Software Requirements cceeesecseeseeseneeesesseeeseeseeseneseeseeesesseesseeseeseenenees 3 2 3 Installing PIPESYS assi a a apaapa eaaa eta et oani ki danean 4 2 3 1 PIPESYS Extension Instalaton sees sees sese ereer eee eee 4 2 3 2 Starting PIPESYS 2 1 Installation 2 3 2 1 System Requirements PIPESYS has the following fundamental system requirements System Component Requirement Operating System Microsoft Windows 2000 NT 4 0 98 95 Disk Space Approximately 6 MB of free disk space is required The green security key is used with the standalone version of HYSYS and can only be attached to a serial Serial Port communications port of the computer running the application do not plug in a serial mouse behind the security key SLM keys are white Sentinel SuperPro keys manufactured by Rainbow Technologies The Computer ID key is installed on the parallel port Parallel P
113. lculate the pressure loss The Hooper procedure is a reliable method for predicting the excess head loss in a fitting due to turbulence caused by abrupt changes in direction and speed of flow The Inside Diameter and Absolute Roughness group boxes are used to specify the inside diameter and inside surface roughness of the fitting The first input cell in each group box is associated with a drop down list from which you may select From Profile or User Specified If the former is selected the program will obtain the diameter and roughness data from the adjacent components in the elevation profile The User Specified setting allows you to enter your choice of values for diameter and roughness The Results group box displays the calculated results of the inlet and exit pressure and temperature for the fitting A pig is likely to average between 50 and 80 90 of the steady state gas velocity in the pipeline A Pig Launcher allows you to begin a Pigging Slug Check in the middle of a pipeline Ifa Pig Launcher is not added to the elevation profile the test is taken from the beginning of the profile to the pig slug catcher In line Facility Options 9 11 9 6 Pigging Slug Check Pigging a pipeline to remove liquids or accretions of material on the inside pipe wall is a transient operation involving a time varying buildup of a liquid slug in front of the pig Rigorous calculation of the growth of the slug is a highly complex proced
114. line measured from the ground surface to the centre line of the pipe Soil Type You may select from a variety of commonly encountered soil types or choose User Specified The soil type is used by the program to determine a value for the soil conductivity If you have chosen User Specified you may enter your own value in the Soil Conductivity input cell Soil Conductivity The thermal conductivity of the soil surrounding the pipe Submerged Water Density The density of the water surrounding the pipe Water Viscosity The viscosity of the water surrounding the pipe Water Conductivity The thermal conductivity of the water surrounding the pipe Water Velocity The cross pipe velocity of the water surrounding the pipe This value is used in convective heat transfer calculations Water Heat Capacity The specific heat capacity of the water surrounding the pipe Above Ground Air Density The density of the air surrounding the pipe Air Viscosity The viscosity of the air surrounding the pipe Air Conductivity The thermal conductivity of the air surrounding the pipe Air Velocity The cross pipe velocity of the air surrounding the pipe unit This value is used in convective heat transfer calculations Buried Fraction The fraction of the pipe diameter that is underground This number must be a value between 0 0 and 1 0 Inside Film Coefficient Displays the calculated or user entered value for the inside film
115. list of available methods for each parameter PIPESYS is fully compatible with all of the gas liquid and gas liquid Fluid Packages in HYSYS You may combine PIPESYS and HYSYS objects in any configuration during the construction of a HYSYS Flowsheet PIPESYS objects may be inserted at any point in the Flowsheet where single or multiphase pipe flow effects must be accounted for in the process simulation 3 1 PIPESYS Features The PIPESYS extension is functionally equivalent to a HYSYS Flowsheet Operation It is installed in a Flowsheet and connected to Material and Energy streams All PIPESYS extension properties are accessed and changed through a set of property views that are simple and convenient to use Chief among these and the starting point for the definition ofa PIPESYS Operation is the Main PIPESYS View e Main PIPESYS View Used to define the elevation profile add pipeline units specify Material and Energy streams choose calculation methods and check results The PIPESYS extension includes these pipeline units each of which is accessible through a property view e Pipe The basic pipeline component used to model a straight section of pipe and its physical characteristics e Compressor Boosts the gas pressure in a pipeline 3 4 Adding PIPESYS For further details on creating a HYSYS case refer to the HYSYS Reference Manual 1 Section 1 3 Starting a Simulation e Pump Boosts the liquid pressure in a pipel
116. ll respects identical to the heater except that it removes heat from the flowing fluid instead of adding heat Like the heater the cooler has an effect on the fluid system only when both pressure and temperature profiles are being calculated In line Facility Options 9 5 9 2 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab Cl Neotec In line Cooler Branch 1 o xj KEE Name ode Cooler Location Distance Elevation Unit Displacement 2900 m 280 0 m 3012m Connections Parameters Delete 9 2 2 Parameters Tab As with the heater you must enter values for the Pressure Drop which is assumed to be constant and independent of the flow rate and for one of Temperature Drop Specified Exit Temperature or Theoretical Duty The remainder of the cells will display results based on the cooler calculations The following parameters appear on this tab e Pressure Drop The pressure loss experienced by any flow through the cooler A constant flow rate invariant quantity e Temperature Drop An incremental drop in temperature applied to the flow through the cooler e Specified Exit Temperature This is the required temperature for the fluids leaving the cooler e Theoretical Duty The amount of heat that must be removed from the stream based on
117. m the beginning of the pipeline Use the Cut button on the Elevation Profile tab to remove any undesired Pig Launchers Figure 9 6 wy Neotec Pigging Slug Size Estimation Branch 1 m ojx Name Pias lugCatcher 1 Pigging Slug Size Check Location Distance Elevation Unit Displacement 2900m 280 0m 3012 m 2 Connections Results Delete 9 6 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab 9 6 2 Results Tab There are no data entry requirements for this calculation Parameters are all taken from the calculated conditions in the pipeline Severe slugging is associated with veritcal or near vertical risers which are acommon feature of offshore production platforms In line Facility Options The Results tab provides three measures of pigging slug size for a range of pig velocities You must use your own judgement to decide which pig velocity is likely to match the actual situation For each value of pig velocity the pig transit time slug volume slug length and slug dumping time are displayed in the results matrix The transit time is the time taken for the pig to travel from the launching point to the check location Slug volume is the volume of liquid ahead of the pig as discussed above and slug length measures how much of the pipeline a
118. make sure that Family Class is set to Hydrocarbon 6 Open the Critical tab of the Hypothetical Component Property View and enter 122 into the Molecular Weight cell 7 Enter 760 kg m into the Ideal Liquid Density cell by first selecting that cell and then typing 760 into the Edit Bar Select units of kg m from the Edit Bar drop down list and the program will automatically convert the liquid density to 47 45 lb ft 10 3 ma Setting Up the Flowsheet 0 4 Setting Up the Flowsheet 10 4 Workbook button 8 Finally press the Estimate Unknown Props button to complete specification of the hypothetical component Verify that the Critical tab appears as in Figure 10 1 before closing the view pil cz lt L Base Properties Ideal Liq Density Ib ft3 47 45 Critical Properties 10 11 12 On the Fluid Package view select the C7 component in the Hypo Components list and press the Add Hypo button to add it to the Current Component List to complete the specification of the fluid Close the Fluid Package view Press the Enter Simulation Environment button at the bottom of the Simulation Basis Manager view Open the Workbook To change the Workbook display select Workbook from the Main Menu bar and then Setup to display the Setup view Figure10 2 Press the Add button in the Variables group box to display the Select Variable s for Main dialog box Select Std Gas Fl
119. meters Tab On this tab you define the parameters that determine the effect of the heater on the fluid system You must enter a value for the Pressure Drop which is assumed to be constant and independent of the flow rate and for one of either the Temperature Rise Specified Exit Temperature or Theoretical Duty The remainder of the cells are for displaying results 9 3 9 4 In line Cooler The following parameters appear on this tab Pressure Drop The pressure loss experienced by any flow through the heater A constant flow rate invariant quantity Temperature Rise An incremental rise in temperature applied to the flow through the heater Specified Exit Temperature This is the required temperature for the fluids leaving the heater Theoretical Duty The amount of heat that must be transferred to the stream based on the fluid properties and amounts of gas and liquid in the mixture to achieve the required heating effect Inlet Temperature The temperature of the fluid at the heater inlet Exit Temperature The temperature of the fluid at the heater outlet Inlet Pressure The fluid pressure at the heater inlet Inlet Pressure The fluid pressure at the heater outlet If you have specified a fluid temperature profile for the pipeline this tab will display the message Heater bypassed because you selected the option to specify the fluid temperature profile 9 2 In line Cooler The In Line Cooler is in a
120. n Se Gas based with liquid Liquid based with gas C User selected mSelections for Horizontal and Inclined Flow rSelections for Vertical How gt Vertical Upflow Overall Selection Flow Regime Prediction Gas based default Taitel and Dukler Overall Selection kengt Gas based default Flow Regime Prediction Govier and Aziz Liquid Holdup Eaton et al Liquid Holdup _ Aziz Govier and Fogai Frictional Pressure Loss Oliemans Frictional Pressure Loss Aziz Govier and Fogar Uphill Correction No Correction Downhill Recovery Recovery Based on Ge Gas based default Beggs and Brill Revisec Beggs and Brill Reviset Beggs and Brill Fluid Temperature Options Calculate Profile C Specify Temperature Connections Worksheet Methods Effective use of the settings on this tab requires you to correctly classify the fluid system as being either gas based with liquid or liquid based with gas A gas based system has a gas phase that is present under all conditions and there may or may not be a liquid phase Conversely a liquid based system has a predominant liquid component The liquid component will be present under all conditions and the gas phase may or may not be present If the software detects that only a single phase is present in the stream i e pure water dry gas all multiphase options are ignored and pressure loss is computed u
121. nce 0 00 Elevation pos 00 E Distance Elevation Run Rise D Pipeline Unit ngth Pipe 945 0 2110 945 0 15 00 945 1 0 909 Pipe 1 Pipe 2055 2030 1110 20001 1110 1 032 Pipe 2 _ Pipe 3111 2090 1056 0 0000 1056 0 000 Pipe 3 lt empty gt 4 I View Cut Copy Paste Global Change Connections 7 Worksheet F Methods Elevation Profile Stepsize perature Profile 77 Close L Cooldown 10 Go to the Temperature Profile page and enter 40 F in the Ambient Temperature cell in the Pipeline Origin group box Figure 11 8 Pipeline Origin Ambient Temperature This completes the first PIPESYS extension for your case 11 11 mm Setting Up the Case Setting Up the Case 11 12 11 3 2 The Second PIPESYS Extension The second PIPESYS extension consists of a single Pipe Unit 11 Enter the required information for the second extension as defined in the following table Connections Page Name Branch 2 Inlet Stream Well B Outlet Stream PS2 Energy Stream ES2 Elevation Profile Distance ft 0 Page Elevation ft 2015 Pipeline Unit Pipe 1 Pipe 1 Elevation ft 2090 Pipe 1 Run ft 2822 Pipe Unit View Nominal Diameter 3 Inches Pipe Schedule 40 Centre Line Depth Default Temperature Profile Ambient Temperature F 40 PIPESYS Application mm Application 1 11
122. nce and Elevation input cells in the Pipeline Origin group box these define the position of the beginning of the pipeline where the inlet stream is attached 3 5 Adding PIPESYS Pipeline Dom Distance k empty gt Elevation Kempty gt Starting with the nearest upstream unit enter each pipeline unit by selecting the lt empty gt cell in the Pipeline Unit column and choosing a unit type from the drop down list on the Edit Bar SX PIPESYS Extension Branch 1 Sisi Pineline Init EE Sei RE E Anae Tahal T To insert the unit at an intermediate position rather than adding it to the end of the list select the unit which will be immediately downstream of the new unit Choose the unit type from the Edit Bar and the new unit will be inserted in the list before the unit that you previously selected A Property View for the unit will appear You should enter all required data for the unit into this Property View before proceeding The PIPESYS View 3 7 W PIPESYS Extension Branch 1 Joj x Pipeline Dom Distance 0 00 Elevation 0 00 ft Angle Label 10 00 200 0 1 909 Pipe 1 15 00 250 0 5 711 Pipe 2 872 0 25 00 322 0 40 00 324 5 7 081 Pipe 3 4 ES L p 4 L View Cut Copy Paste Global Change Connections Z Worksheet Z Methods Elevation Profile Stepsize perature Profile 7777 Tr sulfficient inform
123. neceseeesseeseesessees 9 7 1 5 Mechanical LOSSES Tabor ceri MRine sss eceesseeenddveceeseesseeseceeeseevseeseeeeees 10 7 1 6 Requirem ms Tab n I 11 TAT RESUS TAD EEN MET 12 7 2GAddINg a COmptesSsS0r v vessa ennon enne BEE eeneesneensesneeneeseesneeseesnersessnee 13 7 1 In line Compressor 7 3 This view is used to enter all of the data required to specify the characteristics of a compressor unit in a PIPESYS extension PIPESYS contains five different compressor models which operate either on performance data built into the program or on data entered by the user Compressors can be installed in pipelines in which there is also a liquid phase If conditions are such that there is a liquid phase at the compressor suction side PIPESYS will automatically remove the liquid and perform the compression calculations on the remaining gas phase The liquid phase is assumed to be pumped around the compressor and the two phases are then recombined at the discharge side 7 1 The Compressor View 7 1 1 Connections Tab You may give the compressor a unique name by entering a label into the Name input cell This label is the same as that displayed in the elevation profile matrix in the Main PIPESYS View The location of the compressor in the profile is specified in the Compressor Location group box using these parameters e Distance the horizontal position of the compressor using the Pipeline Origin as the reference point e Elevation
124. nerate a default value Open the Curve tab Depending on the type of compressor selected you may have to supply data for a Compression Ratio vs Brake Power Flow If no curve data is required the message No data required for compressor type selected will appear on this tab If curve data is required a matrix will appear for data entry 7 15 7 16 7 16 Adding a Compressor 9 On the Mechanical Losses tab there are three parameters used to specify mechanical losses for the compressor Figure 7 12 0 850 __sempty gt lt empty gt Only one of these may be selected as they are different and mutually exclusive methods for specifying mechanical losses Entering a value for one of these parameters improves the accuracy with which the compressor is modelled and it is recommended that you supply the PIPESYS with this data if you are able to obtain it from the manufacturer s specification sheets If you are unable to obtain this data leave the input cells empty and the mechanical losses will not be computed 10 At this point you are finished entering the required data on the Compressor View You can now close this View by pressing the Close button 11 Finally check that the location data for the compressor on the Elevation Profile tab of the Main PIPESYS View is correct This data has been automatically determined using the position data of the preceding unit in the pipeline so you should verify that it ha
125. ng answers to frequently asked questions example cases and product information technical papers news bulletins hyperlink to support e mail You can also access Support directly via e mail A listing of Technical Support Centres including the Support e mail address is at the end of this chapter When contacting us via e mail please include in your message Your full name company phone and fax numbers The version of HYSYS you are using shown in the Help About HYSYS view The serial number of your HYSYS security key A detailed description of the problem attach a simulation case if possible We also have toll free lines that you may use When you call please have the same information available 1 7 1 Calgary Canada AEA Technology Hyprotech Ltd Suite 800 707 8th Avenue SW Calgary Alberta T2P 1H5 Barcelona Spain Rest of Europe AEA Technology Hyprotech Ltd Hyprotech Europe S L Pg de Gracia 56 4th floor E 08007 Barcelona Spain Oxford UK UK clients only AEA Technology Engineering Software Hyprotech 404 Harwell Didcot Oxfordshire OX11 ORA United Kingdom Kuala Lumpur Malaysia AEA Technology Hyprotech Ltd Hyprotech Ltd Malaysia Lot E 3 3a Dataran Palma Jalan Selaman VG Jalan Ampang 68000 Ampang Selangor Malaysia Yokohama Japan AEA Technology Hyprotech Ltd AEA Hyprotech KK Plus Taria Bldg 6F 3 1 4 Shin Yokohama Kohoku ku Yokohama Japan 22
126. ngs Apply The Global Change Property View is almost identical to the Pipe Unit Property View Global Change Feature 6 7 6 2 Global Change Procedure The steps to implementing a global parameter change for some or all of the Pipe Units in the elevation profile are outlined in the following procedure 1 Select any one of the Pipe Units in your elevation profile matrix and press the Global Change button The Global Change Property View will appear and display the data from the selected unit Figure 6 8 E Neotec Pipe Unit Branch 1 Cl Name Copy of Pipe 1 Global Change Either select the data to apply in the global change or make changes to the pipe data and have those changes applied Connections Dimensions Heat Transfer Z Pipe Coatings 2 Request a Global Change for a particular parameter by entering the new parameter values into the input cells Each major group of Pipe Unit parameters has a check box beside it which will become automatically checked once a parameter has been changed Figure 6 9 Pipe Dimensions Nominal Diameter 3 Inches zl y Pipe Schedule 40 2 88 900 mm 5 486 mm 77 927 mm Outside Diameter all Thickness Inside Diameter Default Roughnesses T Change bsolute Roughness Relative Roughness Default Steel bare 0 04572 mm 0 000587 6 7 6 8 6 8 Global Change Procedure To select
127. nsities 13 3 13 4 PIPESYS Terms mixture velocity The average velocity of a multiphase fluid mixture calculated as the sum of the gas and liquid superficial velocities pig launcher The point in a pipeline at which pigs are introduced into the fluid stream pigging slug The accumulation of liquid that builds up in front of a pig as it moves through a pipeline In PIPESYS the volume of the pigging slug is calculated to be the total initial volume of liquid in the pipeline at steady state conditions less the amount of liquid that flows out of the line during the transit time for the pig Pipe Unit A straight line segment of pipe connecting two points on an elevation profile It is further defined by data such as diameter roughness heat transfer characteristics and environmental conditions Pipeline Origin The location of the beginning of a pipeline Vertical and horizontal coordinate values establish the physical location of the Pipeline Origin These values are entered on the Elevation Profile page of the Main PIPESYS View into the Distance and Elevation cells in the Pipeline Origin group box Pipeline Unit This is an all inclusive term that is used to refer to both Pipe Units and in line facilities All the physical units that make up a pipeline are referred to as Pipeline Units This term can be used interchangeably with the term components relative roughness The ratio of absolute roughness to the inside diameter
128. ocess Any Pipe Unit can be used as a data template for changing the other Pipe Units in the pipeline simply by selecting it prior to clicking the Global Change button Global Change 6 3 6 4 Global Change View For example after having made a pressure drop calculation for a pipeline consisting of 10 sections of 4 pipe you might wish to repeat the calculation for the same pipeline with all diameters increased to 6 Rather than changing each of the 10 Pipe Units individually you can apply the Global Change feature Using this feature you are required to execute only a few user interface operations to change the pipe diameters from 4 to 6 for all Pipe Units The Global Change Property View is almost identical to the Pipe Unit Property View Except as noted in this chapter you make changes to Pipe Unit parameters using the same interface features that are described Chapter 5 Pipe Unit View The distinguishing feature of the Global Change Property View is the Change check boxes that are associated with particular groups of parameters on each of the tabs as shown in Figure 6 3 Nominal Diameter 3 Inches E K These check boxes have two functions They become automatically checked when you change one or more of their associated parameters as a reminder that you have requested a Global Data change for the selected Pipe Unit or other Pipe Units As well they can be manually checked to indicate that the data
129. of the pipe resistance coefficient A dimensionless constant used to specify a pressure loss as a number of velocity heads step size The initial length of pipe over which the pressure and or temperature and or enthalpy changes are computed for a Pipe Unit If the computed change exceeds the maximum allowed in a step then the length is shortened When the optimizer option is selected the length of pipe for the calculation step will be increased if the computed change is less than the minimum specified This length is further constrained by a minimum and maximum step size If the software attempts calculation for a length of pipe smaller than the minimum step size the calculations are terminated and a warning message issued superficial gas velocity The volumetric gas rate divided by the total cross sectional area of the pipe 13 4 Glossary of Terms 13 5 superficial liquid velocity The volumetric liquid rate divided by the total cross sectional area of the pipe theoretical power The power required to operate a compressor assuming zero compression losses and an absence of mechanical losses velocity head The portion of the total head of a fluid flow attributable to the velocity of the fluid The velocity head is directly related to the kinetic energy component in the Bernoulli equation and is given by ve P where V fluid velocity p fluid density 13 5 13 6 References 13 2 References American Petroleum
130. omp Mass Frac propane 0 0290 Comp Mass Frac i Butane 0 0077 Comp Mass Frac n Butane 0 0246 Comp Mass Frac i Pentane 0 0074 Comp Mass Frac n Pentane 0 0072 Comp Mass Frac n Hexane 0 0012 Comp Mass Frac Nitrogen 0 0098 Comp Mass Frac C02 0 0409 Comp Mass Frac H2S 0 0097 4 2 Adding the PIPESYS Extension Once the case is created the PIPESYS extension can be added 1 Go to the UnitOps tab in the workbook and press the Add UnitOp button 2 From the available list select PIPESYS extension and click Add Elevation Profile Quick Start 3 On the Connections tab complete the form as shown in Figure 4 2 SM PIPESYS Extension Branch 1 BIS Name Branch 1 Outlet Outlet L Inlet Inlet L Energy Solving Behaviour IS PSYS Q e T Ignore this UnitOp During Calculations Elevation Profile Connections Worksheet_ Methods 4 3 Defining the Elevation Profile 1 Open the Elevation Profile tab As you can see from Figure 4 1 the coordinates of the Pipeline Origin have the value 0 0 Enter 0 0 into both the Distance and the Elevation cells in the Pipeline Origin group box Add a Pipe Unit to the matrix as follows 2 First select the lt empty gt cell in the Pipeline Unit column and then choose Pipe from the drop down list on the Menu Bar A Pipe Unit Property View will appear 4 5 4 5 Defining the Elevation Profile 3 Complete the
131. onductivity _ 0 500 Bud C Buried Submerged Inside Film Coefficient lt empty gt C Buried Exposed Inside Film Coefficient Calculated C Specified Connections Dimensions Heat Transfer Delete Pipe Coatings 11 9 11 10 Setting Up the Case 7 Close the Pipe Unit view and complete the Elevation Profile page by entering 945 ft for the Run parameter and 2110 ft for the Elevation parameter All other parameters are automatically calculated as shown in Figure 11 6 4 PIPESYS Extension Branch 1 BIS Pipeline Dom Distance 0 00 Elevation Pen Pipeline Unit eee Bead Pipe 945 0 2110 945 0 15 00 945 1 0 909 Pipe 1 lt empty gt 4 TE Cut Copy Paste Global Change Worksheet 7 Methods Elevation Profile perature Profile ff if Connections Insufficient information on the Temperature Profile screen Delete 8 Add the remaining 2 pipe units Because all the pipe units for the extension have identical properties to Pipe 1 you may use the Copy and Paste buttons as a time saving measure for adding the new units 11 10 PIPESYS Application mm Application 1 11 11 9 Complete the elevation profile as shown by adding the Elevation and Run parameters for all units Figure 11 7 Figure 11 7 W PIPESYS Extension Branch 1 ell Pipeline Dom Dista
132. ort printer port of your computer An arrow indicates which end should be plugged into the computer This is the new key that is used for both Standalone and Network versions of HYSYS Minimum usable SVGA 800x600 Recommended SVGA 1024x768 Required Note that a mouse cannot be plugged into Mouse the back of the green serial port key used with the standalone version of HYSYS Monitor Video 2 2 Software Requirements The PIPESYS Extension runs as a plug in to HYSYS That is it is uses the HYSYS interface and property packages to build a simulation and is accessed in the same manner as a HYSYS unit operation Therefore to run PIPESYS you are required to have HYSYS Version 1 2 or higher Note you will not be able to use PIPESYS without the proper HYSYS and PIPESYS licenses You can refer to Chapter 4 Software Licensing of the HYSYS Get Started Manual for information on licenses 2 3 2 4 Installing PIPESYS For instructions on installing HYSYS refer to Section 3 2 Installing HYSYS of the HYSYS Get Started Manual 2 3 Installing PIPESYS 2 3 1 PIPESYS Extension Installation The following instructions relate to installing PIPESYS as an extension to HYSYS HYSYS must be installed prior to installing the PIPESYS Extension 1 Shut down all other operating Windows programs on the computer before starting the installation process 2 Insert the HYSYS software CD into the CD ROM drive o
133. ow in the Variable s list Press the OK button in the Select Variable s for Main dialogue box Close the Setup view Gas Condensate Tutorial we Tutorial 10 5 Cl Setup x pj vrorkbook Tabs Tab Contents Add Object Name Streams Order Delete E Type Stream New Type Variables Variable Format Vapour Fraction 1 4 fixec Use Set i 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 A sig fig Molar Enthalpy 4 sig fig Order 14 Create anew Material Stream Name it Condensate and type 110 F into the Temperature cell and 1150 psia into the Pressure cell See Figure 10 3 below a Workbook Case Main 10 x Ibmole hr 7 Condensate lt empty gt 110 0 1150 Molar Flow lbmole hr Mass Flow lb hr lt empty gt Liquid Volume Flow barrel day lt empty gt Heat Flow Btuhr lt empty gt Molar Enthalpy Btu Ibmole lt empty gt Std Gas Flow MMSCFD lt empty gt L ST Energy Streams ProductBlock_Condensz UI Include Sub Flowsheets FeederBlock_Condensal oO Show Name Only Number of Hidden Objects 0 Streams 10 5 106 Setting Up the Flowsheet 0 6 Setting Up the Flowsheet 15 Enter 75 million standard cubic feet per day MMSCFD in
134. pecify otherwise Adiabatic Efficiency PIPESYS uses a default value of 0 73 unless you specify otherwise In line Compressor 7 7 e Interstage deltaP This parameter corresponds to the pressure loss caused by the interstage tubing and fittings PIPESYS uses a value of zero as a default value e Heat Capacity Ratio This parameter is a property of the gas and is expressed as Cp Cv It is needed for temperature rise calculations and for selecting values from the built in compressor performance curves PIPESYS will calculate this value using gas property data as a default or will use whatever value you choose to enter e Rating Factor This is a calibration factor which you can use to fine tune a compressor performance curve for either internal or user specified curves This factor arbitrarily increases or decreases the power value obtained from a performance curve Its purpose is to allow you to more closely model the performance of an actual compressor using the built in performance curves in PIPESYS 7 1 3 Curve Tab Use this tab to enter performance curve data when the Polytropic User Curve on the Parameters tab is chosen Otherwise the message No data is required for the compressor type selected will appear You must select the units used to specify the Brake Power Flow parameter You may choose from e Hp MMscfd Horsepower per million standard cubic feet per day e kW E3sm3d kilowatts per thousand standard cu
135. perature 3 20 The PIPESYS View 3 21 This is of course a complex transient heat transfer problem especially for multiphase fluid systems and a rigorous solution is generally not possible The cooldown calculations in PIPESYS should however provide approximate answers that should be capable of reasonable accuracy in many cases of interest H PIPESYS Extension Branch 1 ll 1 000 hours x Pipeline Fluid Cooldown Temperature Profiles Option Parameters pil ue mokoi ao tit Dveral Heat Transfer Coefficient lt empy gt e S SS PAamea Inside Film Coefficient ___ lt empty gt Temperature profiles computed at Thermal Conductivity of Fluid lt empty gt deat etl D CL HE 8 Heat Capacity of Pipe Material lt empty gt Profile of time to reach a specified Ti m ES S temperature after shutdown 2 R Basis First Intermediate Time Heat content of pipeline fluid only Second Intermediate Time 0 5000 Computed or specified inside film coefficient Third Intermediate Time 0 7500 Heat content of both fluid and pipe material Minimum Cooldown Temperature lt empty gt Ignore inside film resistance Calculation Time Step 10 00 Thermal Conductivity of Fluid Liquid Based z Default i Connections Z Worksheet Z Methods Elevation Profile Stepsize Cooldown perature Profile 77 fT sufficient information in a Pipeline unt Delete The
136. plication 2 12 9 14 Press the Go button When the program is finished pressures at the wells should be Well Pressure psia A 849 0 B 813 1 C 765 3 Now the pressure flow rate for Well A is reasonably close to the curve The pressures for B and C have changed a little but not significantly from the last iteration Fortunately the pressure at a given well is fairly insensitive to pressure changes at any of the other wells This process can be repeated to obtain a solution of any arbitrary precision subject to the limits imposed by the computer but this solution is accurate enough for further analysis Compression has increased flow rates by a considerable amount ompressio D D A 8 6 10 5 B 7 4 9 0 C 10 1 11 9 The engineering analysis shows that adding the compressor increased production by about 20 at each of the wells These results can be used in an economic study to further examine the value of adding compression to the pipeline system 12 9 Optimization Application Wellhead Performance Curve for Well A S a E 0 1 2 3 4 5 6 7 8 g 10 11 12 13 14 Gas Flow Rate MMSCFD 70 60 EX i CH 50 CH Cem 40 5 1300 L 110 T DU 90 80 700 GOSS HS my h eee E Se SS CH CH EA Ki Wellhead Pressure psia 50 40 CH EA C 30 20 e 12 1
137. pressure an iterative procedure is performed over the entire pipeline Calculations proceed until the calculated downstream pressure converges to the fixed downstream pressure within some tolerance specifically the Downstream Pressure Convergence Tolerance 3 4 6 Cooldown Tab In pipelines that are used to transport a relatively high pour point crude oil or a gas system that is subject to hydrate formation it is usually necessary to maintain a minimum flowing temperature to avoid excessive pressure losses or even line blockage Such pipelines are often insulated and may have one or more heaters When one of these pipelines is shutdown for an extended period of time it must generally be flushed or vented to remove the hydrocarbon fluid since the temperature in the system will eventually come to equilibrium with the surroundings Apart from the time and effort involved in this operation the subsequent re starting of the pipeline is more complicated after it has been purged than if it could be simply be left filled with the original hydrocarbon fluid In the case of an emergency shut down however it may be possible to carry out whatever remedial action is required before the temperature reaches the minimum allowable value In such cases the line can be re started much easier than if it has been purged and it is thus of interest to be able to predict with reasonable accuracy how long the fluid will take to cool down to any particular tem
138. production platforms but may also be encountered in pipelines that traverse uneven terrain Severe slugging occurs only at points where a steep riser inclined at 70 or more is immediately 9 13 Severe Slugging Check downstream of a gradually descending section of the pipeline and even then only under conditions of low to medium gas and liquid flow rates If the flow is stratified a liquid seal may form at the base of the riser and block the gas flow The liquid will continue to flow and accumulate in the riser forming a slug This slug will grow and expand to fill the riser if the rate at which the hydrostatic head of the slug increases is faster than the rate at which the gas pressure increases upstream of the slug Eventually the liquid will reach the top of the riser and continue to flow through the pipeline However this situation does not represent an equilibrium state because the gas flow remains blocked The hydrostatic head of the slug cannot further increase but the pressure due to the buildup of gas at the base of the riser will finally exceed the hydrostatic head of the slug and cause gas to enter the riser Sometimes the gas pressure can exceed the hydrostatic head of the slug before the liquid reaches the top of the riser but the end result is the same and gas moves into the riser As the gas displaces the liquid in the riser the hydrostatic head is reduced causing a corresponding expansion of the gas At some point the
139. r 1975 Gregory G A Comments on the Prediction of Minimum Unloading Velocities for Wet Gas Wells Technical Note No 14 Neotechnology Consultants Ltd Calgary Canada Dec 1989 Gregory G A Estimation of the Overall Heat Transfer Coefficient for the Calculation of Pipeline Heat Loss Gain Technical Note No 3 Neotechnology Consultants Ltd Calgary Canada Oct 1984 1st Rev Sept 1990 2nd Rev Mar 1991 Hooper W B The Two K Method Predicts Heat Losses in Pipe Fittings Chem Eng p 96 Aug 24 1981 Hughmark G A Holdup and Heat Transfer in Horizontal Slug Gas Liquid Flow Chem Eng Sci Vol 20 p 1007 1965 Hughmark G A Holdup in Gas Liquid Flow Chem Eng Prog Vol 58 No 4 p 62 Apr 1962 13 7 13 8 References Lockhart R W and Martinelli R C Proposed Correlation of Data for Isothermal Two Phase Two Component Flow in Pipes Chem Eng Prog Vol 45 No 1 p 39 Jan 1949 Mandhane J Gregory G and Aziz K A Flow Pattern Map for Gas Liquid Flow in Horizontal Pipes Int J Multiphase Flow Vol 1 p 537 1974 Mandhane J M Gregory G A and Aziz K Critical Evaluation of Friction Pressure Drop Prediction Methods for Gas Liquid Flow in Horizontal Pipes J Petrol Technol p 1348 Oct 1977 Mukherjee H and Brill J P Liquid Holdup Correlations for Inclined Two Phase Flow J Petrol Technol p 1003
140. r 7 5 8 4 Buried Pipe 5 5 Parameters 5 7 C Calculate Temperature Profile 3 24 Calculation Methods Horizontal and Inclined Flow 13 9 Vertical and Near Vertical Upflow and Downflow 13 10 Calculation Warnings 3 28 Compressor 7 1 Actual Losses 7 11 Connections Page 7 3 Curve Page 7 7 Exponent of Gas Power 7 11 Manipulating Curve Data 7 8 Mechanical Losses Page 7 10 Optional Constraints 7 6 Overall Efficiency 7 11 Parameters 7 6 Parameters Page 7 4 Power Balance 7 10 Requirements Page 7 11 Results Page 7 12 Compressor See In line Compressor Connections Page 3 10 Cooler 9 4 Connections Page 9 5 Parameters 9 5 Parameters Page 9 5 Cut and Paste Functions 3 16 Default Methods Changing 3 12 Default Roughness 5 4 Disabling PIPESYS 3 10 Discharge Pressure 7 5 Distance 3 15 Elevation 3 15 Elevation Profile Defining 4 5 Entering 3 15 Parameters 3 15 Elevation Profile Page 3 13 Erosion Velocity Check 9 16 Connections Page 9 17 Limiting Velocity Equation 9 16 9 17 Max Allowable Velocity 9 16 Results Page 9 18 F Features 3 3 Fittings 9 9 Absolute Roughness 9 10 Connections Page 9 9 Inside Diameter 9 10 Parameters Page 9 9 Fluid Systems 3 12 Fluid Temperature Options 3 13 3 24 Force Enthalpy Convergence 3 20 G Gas Based Fluid Systems 3 12 a Global Change 3 17 6 1 Example 6 9 Procedure 6 7 Global Change View Connections Page 6 4 Dimensions Page 6 5 Heat Transfer Page 6 6 Pipe Coatings 6 6 Glos
141. rameters in the Optional Constraints group box allow you to limit the output of the Unit X The pressure ratio and exit pressure can be limited to whatever values you choose to enter in these input cells Entering a value in the Pressure Ratio cell will cause the Max Pressure Ratio cell to be disabled and entering a value in the Exit Pressure cell will cause the Max Exit Pressure cell to be disabled 9 3 3 Results Tab The inlet and exit conditions for the Unit X are displayed here In line Regulator 9 4 In line Regulator The In Line Regulator is used to limit the pressure at any point in the pipeline profile The only data required is the maximum exit pressure for the regulator If the line pressure is less than the regulator exit pressure the regulator will be ignored If the temperature profile is being calculated and the fluid is a gas based system i e dry gas gas water gas condensate the discharge temperature will be computed assuming an isenthalpic expansion occurs PIPESYS bases this computation on the specific enthalpy of the fluids and so the Joule Thompson cooling effect is taken into account implicitly Figure 9 4 Hl Neotec In line Regulator Branch 1 Isi EE Name Beato 9 P ca Regulator Location E Distance Elevation Unit Displacement 2900 m 280 0 m 3012 m 2 Connections Parameters 9 4 1 Connections Tab As on all component views the location for the unit is displaye
142. ream being compressed to satisfy fuel gas requirements Data required to compute the fuel gas requirements for the compressor is contained on the Fuel Requirements tab of the Compressor Pipeline Unit Figure 7 4 H Neotec In line Compressor Branch 1 ioj x Euel Requirements Optional Percent of Throughput Fuel Flow 7 Power Units MMscfd Hp Fuel Flow 7 Power lt empty gt Thermal Efficiency lt empty gt Hei Heating Value lt empty gt Fuel Consumption lt empty gt Connections 7 Parameters 7 Curve Fuel Requirements Delete If fuel gas calculations have been requested PIPESYS will compute the fuel gas requirements for the compressor based on e aspecified percentage of throughput e a specified ratio of fuel gas to the overall brake horsepower e the net heating value of the gas thermal efficiency and overall brake horsepower In all of the above cases it is assumed that the fuel gas is taken from the suction side of the compressor after any first stage separation is done to remove liquids Fuel consumption reduces the total amount of gas that must be compressed and thus an iterative solution is applied to compute the compressor horsepower For the case when the net heating value of the gas and the overall brake horsepower is used to compute the fuel requirements the thermal efficiency of the compressor is required A value for the net heating value of the gas can also be ente
143. red If the value of the net heating value is left empty it is determined from the gas being compressed The fuel requirements are then computed as 7 9 7 9 SE The Compressor View 7 10 g 0 106798 BHP f h N where Qr total gas removed from the pipeline at the compressor station lb sec h net heating value of the gas BTU Ib n overall thermal conversion efficiency 7 1 5 Mechanical Losses Tab There are three optional parameters that can be entered on this tab These values improve the accuracy with which the compressor is modelled and it is recommended that you supply the program with this data if you are able to obtain it from the manufacturer s specification sheets If you leave the input cells empty PIPESYS will ignore mechanical losses Only one of these parameters may be set to a non zero value as they represent different and mutually exclusive ways of describing the mechanical losses that occur in a compressor process Figure 7 5 CH Neotec In line Compressor Branch 1 UL xj a as Mechanical Losses Optional Overall Efficiency lt empty gt ctual Losses lt empty gt Exponent of Gas Power lt empty gt Paramet Curve Fuel Requirements Mechanical Losses Delete The Power Balance for a compressor is Brake Power Gas Power Mechanical Losses In line Compressor 7 11 Brake Power is the total power required to operate the compressor Gas Pow
144. required to operate a compressor including all losses experienced during gas compression and all mechanical losses component All physical units that make up a pipeline Has the same meaning as the term Pipeline Units elevation profile A two dimensional coordinate scheme for defining the path followed by a pipeline as it traverses its route The elevation profile models the actual pipeline geometry as a series of connected straight line segments the end points of which are defined by horizontal and vertical displacement values gas power The power required to operate a compressor neglecting all mechanical losses in line facility Equipment used to handle or affect the fluid flow through a pipeline Compressors pumps heaters and coolers are examples of in line facilities inside film The layer of fluid adjacent to the pipe inside wall i e the boundary layer The inside film is assumed to account for all resistance to heat transfer between the flowing fluid and the pipe wall inside film coefficient A measure of the resistance to heat transfer between the fluid and the pipe wall due to convection effects Main PIPESYS View The interface window to all of the user definable characteristics of a PIPESYS extension It is used to choose methods add Pipeline Units specify temperatures and examine results mixture density The density of a multiphase fluid mixture calculated as a volume weighted average of the gas and liquid de
145. roper usage of calculation methods Certain combinations of methods are disallowed if there are incompatibilities and PIPESYS will display a warning message if such a combination is selected However there are many situations where a number of methods are valid but where some of these will give more accurate results than others for a given case Some methods tend to give consistently better results than others for particular fluid systems PIPESYS has been designed to default to such methods for these cases 3 4 4 Elevation Profile Tab On this tab the components and geometry of the pipeline system are defined A starting point for the profile must be specified at the top of the tab in the Pipeline Origin group box using the Distance and Elevation input cells The starting point for the profile can have negative zero or positive distance and elevation values but the position represented by these values must correspond to the point connected to the inlet stream of the PIPESYS extension Figure 3 11 SM PIPESYS Extension Branch 1 ioj x Pipeline Dom 0 00 Elevation 0 00 Distance Distance Elevation Run Rise Pipeline Unit Angle Label 10 00 300 0 10 00 550 0 15 00 250 0 25 00 251 2 Bo Pipe 2 872 0 25 00 322 0 40 00 324 5 7 081 Pipe 3 View Cut Copy Paste Global Change Connections 7 Worksheet Methods Elevation Profile Stepsize Z Cooldown Aperature Profile 77 fT su
146. rovided in this tab you need some information about your system You will need an estimate of sand production for the system in units of lb month or kg month and you need to evaluate the sensitivity of the system to erosion damage If you wish to eliminate erosion choose C 100 If this condition is too restrictive in terms of allowable velocity and a small erosion rate over the life of the pipeline can be tolerated use C 300 Using the actual mixture velocity as an assumed erosion velocity an effective C value is computed assuming no sand production This gives a measure of a minimum value for C for which erosion will not be a concern for this case Find the value of sand production in the Sand Production column that is closest to the value for your system This is expressed in lb month or kg month Read across to the allowable velocity value that corresponds to the value of C that you have chosen If this allowable velocity value is less than the Mixture Velocity in the Fluid Conditions group box erosion is likely to be higher than acceptable and you should make whatever changes are necessary to lower the mixture velocity at this location If the allowable velocity value is greater than the mixture velocity erosion is unlikely to be a problem 9 9 Side Stream A Side Stream Pipeline Unit in PIPESYS can be used to add or remove flow from the elevation profile For pipelines with multiple sources this provision eliminates the need to cr
147. rroundings Select either Calculate profile or Specify temperatures in the Fluid Temperature group box Fluid Temperature Calculate profile C Specify temperatures If you choose to specify temperatures you must enter at least one temperature value at the Pipeline Origin The program will use the temperature values that you do enter to fill in interpolated temperature values at each of the elevation profile points that you leave empty Following these steps allows you to complete the PIPESYS extension Once the calculations are complete as displayed by the Object Status bar the Results tab will display temperature and pressure data for the pipeline and you are then able to print summary or detailed reports The Messages tab reports any special problems or conditions encountered in the course of the calculations 3 3 PIPESYS User Interface The PIPESYS user interface is completely integrated into the HYSYS environment and conforms to all HYSYS usage conventions for operations and data entry If you are an experienced user of HYSYS you will already be familiar with all of the features of the PIPESYS user interface If you are a new user you should begin by studying the HYSYS Reference Manuals since you will need to learn more about HYSYS before you can use the PIPESYS extension The PIPESYS user interface consists of an assortment of property views PIPESYS Pipeline Units of which there are many types including pipe uni
148. s Click on the Units tab to change the unit set The workbook can also be accessed by using the hotkey combination lt Ctrl gt lt D gt For more information on creating a Hypothetical Component refer to Chapter 9 Hypotheticals of the HYSYS Reference Volume 1 Gas Condensate Tutorial 10 3 This example guides you through the construction of a gas condensate pipeline consisting of four Pipe Units A Fluid System with a hypothetical component is used in a pressure drop calculation for a predetermined flow rate through the pipeline All units for this example are Field 10 1 Setting Up the Flowsheet The following table shows the fluid package you will create for this example Property Package Components C1 C2 C3 i C4 n C4 i C5 C6 C7 Nitrogen CO2 H2S Peng Robinson 1 Start HYSYS and create a New case 2 Create a Select EOSs in the Property Package Filter group box and then PR in the Base Property Package Selection group box 3 Open the Components tab on the Fluid Package view and use the Pure button to add Cl C2 C3 i C4 n C4 i C5 n C5 C6 Nitrogen CO2 and H2S to the Current Component List 4 Select the Hypothetical radio button on the Add Comps group box on the Components tab and then click the Quick Create a Hypo Comp button This will bring up the Hypothetical Component Property View 5 On the Hypothetical Component Property View enter C7 into the Component Name cell and
149. s been positioned as you intended If not you can use the Cut and Paste buttons on the Main PIPESYS View to transfer the compressor to a new position Figure 7 13 W PIPESYS Extension Branch 1 ioj x Pipeline Unit ie Pipe Pipe 1 Compressor 1200 360 0 6 0000 0 0000 0 0000 0 000 Compressor 1 Pipe 2400 100 0 1200 260 0 1228 12 225 Pipe 2 PigLaunch 2400 100 0 0 0000 0 0000 um 0 000 PigLauncher 1 Pipe 2900 2800 5000 1800 531 4 19799 Pipe 3 lt empty gt R View Cut Copy Global Change Connections 7 Worksheet Methods Elevation Profile Stepsize perature Profile ff if aaa SaaS oie a as Delete In line Pump 8 1 H In line Pump 8 1 In line PUMP VieW csesceeseeseneeeseeesneessneeseeeesneesseesseeessneesseeseneeesneeseeeeens 3 8 1 1 Connections Tab geseet 3 8 1 2 Parameters Jah TTT aara i 3 Silk CUE E A ERM e 5 8 1 In line Pump 8 3 PIPESYS supports two different methods of pump performance modelling One method relates discharge pressure to fluid horsepower and volumetric flow rate using an equation The other method uses tabular data that you must enter to establish the head and overall efficiency as functions of the volumetric flow rate Both methods may be used interchangeably to model the performance of an actual pump so your choice of method is dictated by the type of data availa
150. sary of Terms 13 1 Graphs Graph Control 3 28 Plot Button 3 27 Printing 3 27 Heat Capacity Ratio 7 7 Heat Transfer Environments 5 5 Heater 9 3 Connections Page 9 3 Parameters Page 9 3 Hooper K1 amp Hooper K2 9 10 Ignoring PIPESYS 3 10 In line Compressor Adding 7 12 7 13 In line Compressor See Compressor In line Pump See Pump Inside Diameter 5 4 Inside Film Coefficient 5 6 Installation 2 1 2 4 Interstage deltaP 7 7 Isentropic Compressor 7 5 L Length 3 15 Liquid Based Fluid Systems 3 12 Main PIPESYS View 2 6 3 3 3 9 Max Discharge Pressure 7 6 Max Discharge Temperature 7 6 Max Interstage Temperature 7 6 Max Power 7 6 Messages Page 3 28 Methods Page 3 11 Minimum Allowed Pressure 3 20 Nominal Diameter 5 4 Number of Stages 7 6 o Outside Diameter 5 4 P Pig Launcher 4 8 9 12 Pigging Slug Size Check 9 11 Connections Page 9 12 Results Page 9 12 Pipe Coatings Page 5 8 Pipe Conductivity 5 6 5 7 Pipe Schedule 5 4 Pipe Segment Results 3 25 Pipe Unit Adding 5 9 Connections Page 5 3 Dimensions 5 4 Dimensions Page 5 3 Global Change 6 3 Heat Transfer Page 5 5 View 5 1 Pipeline Origin 3 13 Pipeline Units 3 3 3 14 PIPESYS and HYSYS Adding PIPESYS 3 4 Property Views 3 9 PIPESYS Methods and Correlations 13 9 Plots See Graphs Polytropic Compressor 7 5 Polytropic Efficiency 7 6 Pump 8 1 Connections Page 8 3 Curve Page 8 5 Discharge Pressure 8 5 Fluid Power 8 4 Parameters Page 8 3 Specified Dis
151. ses a new Pipe Unit will appear in the profile matrix and the Pipe Unit View will open 1 Neotec Pipe Unit Branch 1 ioj x Name Pipe 4 m Pipe Segment Location Distance Elevation Unit Displacement 560 0 m 5 000 m 562 2 m Connections Dimensions Delete Heat Transfer Pipe Coatings 2 Enter a label for this Pipe Unit or accept the default name provided automatically in the Name cell 3 Select the Dimensions tab on the Pipe Unit View Here you enter the physical dimensions and the effective roughness of the pipe If the nominal diameter and the pipe schedule are known choose these settings from the Nominal Diameter and Pipe Schedule drop down boxes Pipe Dimensions Nominal Diameter lt empty gt E 2lnehes 2 5 Inches 3 Inches 3 5 Inches 4 Inches Pipe Schedule Outside Diameter all Thickness Inside Diameter Default Roughnesses Absolute Roughness Relative Roughness 12 Inches 0 04572 mm lt empty gt Pipe Unit View 5 11 The program will obtain the corresponding dimensions from its internal database and fill in the Outside Diameter Wall Thickness and Inside Diameter cells Alternatively you can select User Specified in the Nominal Diameter drop down box and enter these values directly 4 Choose a material type from the Default Roughness drop down list or enter an Absolute Roughn
152. sing the Fanning equation If the vertical or horizontal orientation of a pipeline unit is such that you have a preference for a particular calculation method you are able to select it on this tab For instance if the prediction of liquid hold up in a pipeline is a particular concern you can manually select OLGAS to perform this calculation instead of using the default method However it is not advised to change the default settings unless you have reason to believe that a different calculation method will yield more accurate results Generally the safest procedure will be to use radio buttons in the Recommended Procedures group box to select either Gas based with liquid or Liquid based with gas whichever classification best describes the system under consideration PIPESYS will then set all of the selections for the various types of flows to those methods that will give the most consistent results The Pipeline Origin defines the point at which the inlet stream connects with the PIPESYS extension The PIPESYS View 3 13 In the Fluid Temperature Options group box select either Calculate Profile or Specify Temperature If the former is selected the program will perform simultaneous pressure and temperature calculations If the latter the temperature of the fluid will be fixed according to values which you enter on the Temperature Profile tab and only pressure calculations will be performed PIPESYS attempts to protect against imp
153. sport fluids over diverse topography and under varied conditions Ideally this would be done efficiently with a correctly sized pipeline that adequately accounts for pressure drop heat losses and includes the properly specified and sized in line facilities such as compressors heaters or fittings Due to the complexity of pipeline network calculations this often proves a difficult task It is not uncommon that during the design phase an over sized pipe is chosen to compensate for inaccuracies in the pressure loss calculations With multiphase flow this can lead to greater pressure and temperature losses increased requirements for liquid handling and increased pipe corrosion Accurate fluid modelling helps to avoid these and other complications and results in a more economic pipeline system To accomplish this requires single and multiphase flow technology that is capable of accurately and efficiently simulating the pipeline flow PIPESYS has far reaching capabilities to accurately and powerfully model pipeline hydraulics It uses the most reliable single and multiphase flow technology available to simulate pipeline flow Functioning as an seamless extension to HYSYS PIPESYS has access to HYSYS features such as the component database and fluid properties PIPESYS includes many in line equipment and facility options relevant to pipeline construction and testing The extension models pipelines that stretch over varied elevations and environments PIP
154. ss input cell depending on the compressor output method chosen in Step 4 Applying a Parameter defaults are provided for Adiabatic Efficiency Polytropic Efficiency Heat Capacity Ratio Rating Factor In line Compressor 7 15 constraint is not required but you may find that applying a constraint allows you to find an optimal operating point for the compressor Figure 7 11 CH Neotec In line Compressor Branch 1 ISI Wen T d Compressor Type Parameters lsentropic H S Diagram X Brake Power Specified 1500 05 JN Calculated lt empty gt Adiabatic Efficiency interstage delta P lt empty gt 189936 4 lt empty gt lt empty gt Default L Fuel Requirements Max Discharge Press Connections _ Parameters Curve Enter values in the Parameters group box that best represent the capabilities and type of your compressor These values may be available from the manufacturer s specification sheets or may be known to you from previous experience with the compressor Cells which will be filled in by the software but can be overwritten by you will be displayed in red Optional values such as Max Discharge Temp and Max Interstage Temp can be left empty Entries are required for all remaining cells If any of the required parameters are unknown to you pressing the Default button while the particular cell is selected will ge
155. stance entering the Distance and Elevation data will result in the Run Rise Length and Angle cells being filled in since all of these quantities can be calculated from a knowledge of the start and end points of the Pipe Unit If am The Main PIPESYS View The Main PIPESYS View you are entering an in line facility the location will be filled in automatically as the program will obtain this data from the previous Pipeline Unit 4 Optionally provide PIPESYS with a Label entry This is used by the PIPESYS program to uniquely identify each Pipeline Unit during calculations and for displaying error messages for a particular unit The program will automatically generate a default label but you may change this if you wish There is no restriction on the number of characters used for this label except that you may wish to use only as many as are visible at once in the cell The entire pipeline from the inlet to the outlet is thus described as a connected sequence of Pipeline Units Some of these units can be pipe segments of constant slope called Pipe Units while others can be in line facilities such as compressors pumps heaters and fittings Compressor Pig Launcher Pig Catcher Elevation Start of 6 line Start of 8 line Distance To make data entry easier for successive units especially when most of the properties remain unchanged from unit to unit make use of the Cut and Paste or the Copy and P
156. t Epe Pipeling Compressor o b Pump Heater eer S DS Saas Awe T ahel 7 13 7 14 7 14 Adding a Compressor Refer to Section 7 1 2 Parameters Tab for more detailed instructions regarding Optional Constraints 3 In the new compressor view that appears enter a label in the Name cell on the Connections tab if desired Figure 7 9 ei Neotec In line Compressor Branch 1 Name Compressor 1 Unit Displacement 3012m Elevation 280 0 m Distance Compressor Location 2900 m ES Connections Parameters 7 Delete Fuel Requirements Open the Parameters tab on the Compressor View Choose a compressor type from the drop down box in the Compressor Type group box See Figure 7 9 Compressor Type lsentropic H75 Diagram bed lsentropie H S Diagram 1 Polytropic Internal Curve Polytropic User Curve Isentropic GPSA Polytropic GPSA The compressor maximum output can be specified using one of two parameters You can enter a value for the Brake Power or the Discharge Pressure in the Specified input cell of these group boxes These are mutually exclusive parameters so entering a value for one precludes subsequently entering a value for the other In order to constrain the compressor output enter a value in the Optional Constraints group box You can enter a value into the Max Power or the Max Discharge Pre
157. t i lt empty gt lt empty gt lt empty gt Gas Total lt empty gt lt empty gt lt empty gt lt empty gt soe Cooling fter Cooling lt empty gt Gar otal Cooling lt empty gt MA A Fuel Requirements Delete Mechanical Losses _ Requirements 7 1 7 Results Tab The conditions at the suction side and the discharge side for each stage of the compressor are displayed on this tab See Figure 7 6 The compressor discharge conditions may be different from the conditions on the discharge side of the final stage if any after cooling has been installed These conditions for both pressure and temperature are displayed in the Compressor Discharge Conditions group box Figure 7 7 Neotec In line Compressor Branch 1 ioj xj Calculated Conditions Suction Side Discharge Side Pressure Temperature Pressure Temperature kPa C kPa C _ lt empty gt lt empty gt lt empty gt lt empty gt E Liquid Removed at Suction Compressor Discharge St Mass Flow Conditions age ton lt empty gt Pressure Temperature kPa Em lt empty gt Fuel Require Mechanical Losses Requirements Results 7 12 To insert a compressor in the middle of the elevation profile select the Pipeline Unit that will be placed immediately downstream and then add the compressor In line Compressor 7 13 If the inlet stream is multiphase eit
158. t to the pipe wall Heat transfer through this film is primarily by conduction but the thickness of the film depends on the flow rate and the fluid properties It is usual to define the resistance to heat transfer in terms of a convective coefficient The inside film can have a significant influence on the heat flow and can account for as much as half of the overall heat transfer coefficient value You may select Calculated and have PIPESYS calculate the inside film coefficient using fluid property data or select Specified and enter the value yourself The Parameters group box on the right half of the Heat Transfer tab contains a list of environment parameters specific to the heat transfer chosen The following list describes the parameters for the various environments For dual environments both sets of parameters will be available Common to All Pipe Environments e Default Conductivities This parameter is similar to the Default Roughness parameter of the Dimensions tab The pipe material type determines the value of the Pipe Conductivity parameter which is set automatically once the pipe material is Pipe Unit View 5 7 chosen If you want to supply your own value for Pipe Conductivity set Pipe Material to User Specified The Pipe Conductivity input cell will become user modifiable Pipe Conductivity This is the thermal conductivity of the specified pipe material Buried Centre Line Depth The burial depth of the pipe
159. temperature changes fall within the specified maximum and minimum As well a minimum and maximum stepsize can be entered to constrain the optimizer Since the relationship between fluid properties and pressure temperature change is implicit PIPESYS performs an iterative calculation of pressure and temperature change at each of the steps mentioned above Initial guesses for the change in pressure temperature or enthalpy can be specified or left as program defaults For multiple component multiphase systems iterations converge on 3 19 3 20 The Main PIPESYS View pressure and temperature For single component multiphase systems or systems which behave in a similar way iterations converge on pressure and enthalpy Pressure temperature and enthalpy convergence can be controlled by your input for convergence tolerance If PIPESYS encounters difficulty in converging to a solution perhaps due to unusual fluid property behaviour you should try to repeat the calculation with the Force Enthalpy Convergence check box selected This approach requires more computer time but may succeed where the temperature convergence fails The Minimum Allowed Pressure in the cell at the bottom left controls the point at which PIPESYS will terminate the calculations due to insufficient pressure The program default is one atmosphere When the case is such that PIPESYS is required to compute pressure at the inlet of the pipeline given a fixed downstream
160. the fluid properties and amounts of gas and liquid in the mixture to achieve the required cooling effect e Inlet Temperature The temperature of the fluid at the cooler inlet e Exit Temperature The temperature of the fluid at the cooler outlet 9 5 a rr e Inlet Pressure The fluid pressure at the cooler inlet e Exit Pressure The fluid pressure at the cooler outlet If you have specified a fluid temperature profile for the pipeline this tab will display the message Cooler bypassed because you selected the option to specify the fluid temperature profile 9 3 Unit X The Unit X is a generic component that allows you to impose arbitrary changes in pressure and or temperature on the fluid flow It can be used to simulate the effects of a wide variety of process devices in a simple manner and is particularly useful in preliminary studies K Neotec In line Unit X Branch 1 BIS E Name Unit 1 Unit Location Distance Elevation Unit Displacement 2900 m 280 0 m 3012 m Connections Parameters_ Results 9 3 1 Connections Tab As on all component views the location for the unit is displayed as read only data If you need to change this data open the Main PIPESYS View and go to the Elevation Profile tab In line Facility Options 9 7 9 3 2 Parameters Tab Pressure parameters for the Unit X can be specified in one of three ways on the Pressure Parameters group bo
161. to the Molar Flow cell on the Workbook view Figure 10 4 HYSYS will convert this value to 8235 lbmole hr Figure 10 4 10 6 Workbook Case Main 75 Condensate lt empty gt 110 0 1150 Molar Flow lbmole hr _ Mass Flow lb hr lt empty gt la x MMSCFD X a Liquid Volume Flow barrel day lt empty gt Heat Flow Btu hr lt empty gt Molar Enthalpy Btu Ibmole lt empty gt Std Gas Flow MMSCFD 0 6831 Streams Energy Streams ProductBlock_Condense FeederBlock_Condensal J Include Sub Flowsheets C Show Name Only Number of Hidden Objects 0 16 Double click the Molar Flow cell and the dialog box Input Composition for Stream Condensate will open Complete the composition detailed on the following tab as shown in Figure 10 5 and click OK Total fi 0000 Cl Input Composition for Stream Condensate xi zen 7 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 OK Gas Condensate Tutorial 10 7 17 Create asecond Material Stream which will be the outlet stream of the pipeline by typing Name this stream Outlet 18 Open the Energy Streams tab of the Workbook view Define an Energy Stream by entering the name Pipeline Energy Transfer
162. ts pumps and compressors are all accessible as property views In this User s Manual PIPESYS property views are referred to individually by the type of component they reference so you will encounter the terms Compressor View Heater View Fittings View etc The PIPESYS View 3 9 Like all HYSYS property views PIPESYS property views allow access to all of the information associated with a particular item Each view has a number of tabs and on each tab are groups of related parameters For example on the Dimensions tab of the Pipe Unit View See Figure 3 7 the physical characteristics of the Pipe Unit such as wall thickness material type and roughness can be specified Figure 3 7 K Neotec Pipe Unit Branch 1 ll sl E Pipe Dimensions Nominal Diameter 3 Inches E Pipe Schedule 40 E Outside Diameter 88 900 mm all Thickness 5 486 mm Inside Diameter 77 927 mm Default Roughnesses Default Steel bare bsolute Roughness 0 04572 mm Relative Roughness 0 000587 PR ST Connections Dimensions f Heat Transfer Delete Pipe Coatings 3 4 The Main PIPESYS View The Main PIPESYS View is the first view that appears when adding a PIPESYS operation to a HYSYS Flowsheet This view provides you with a place to enter the data that defines the basic characteristics of a PIPESYS operation Here you can specify pipeline units elevation profile data calculation procedures tolerances and all other
163. two Using the Run and Rise parameters specify the endpoint coordinates The Run value is 500 2900 2400 and the Rise is 180 280 100 Figure 4 7 shows the completed Elevation Profile tab SY PIPESYS Extension Branch 1 Pis E Pipeline Origin d Distance 0 00 Elevation poo Distance i Length Pipeline Unit Pipe 1200 360 0 1200 16 699 Pipe 1 Pipe 2400 100 0 1200 260 0 1228 12 225 Pipe 2 Pig Launch 2400 100 0 0 0000 0 0000 0 0000 0 000 PigLauncher 1 Pel 290 2800 5000 1800 531 4 19799 Been lt emply gt t View Cut Copy Paste Global Change Connections Worksheet Methods Elevation Profile Stepsize perature Profile 7777 The status bar at the bottom of the PIPESYS view indicates that there is Insufficient information on the Temperature Profile screen 12 Open the Temperature Profile tab Enter 20 into the Ambient Temperature cell of the Pipeline Origin group box You will notice that the Ambient Temperature value is automatically copied in the Ambient T cell for each individual pipe unit unless otherwise specified Once the Ambient Temperature information is provided PIPESYS begins calculating When completed the status bar reads Converged The Temperature Profile tab of the converged extension is shown in Figure 4 8 below 4 9 40 Defining the Elevation Profile Defining the Elevation Profile
164. ure and is not attempted in PIPESYS which is strictly a steady state flow simulator However PIPESYS is capable of performing some simple calculations that are adequate for purposes of sizing a slug catcher Sizing calculations are made with the assumptions that there is no slippage of fluid past the pig and that the resident liquid fraction in the pipe is given by the steady state case However while the pig passes through the pipeline from the pig launcher to the pig trap liquid continues to be produced from the downstream end at the steady state rate When the pig finally reaches the trap the amount of liquid in the slug is taken to be the total initial volume of liquid in the pipeline as predicted under steady state conditions less the amount of liquid that flows out of the line during the transit time for the pig Consequently the success of the calculation depends on obtaining a suitable estimate for the pig transit time As an upper bound the pig cannot travel faster than the average steady state gas velocity In fact it is reasonable to assume that even in a relatively flat pipeline it would be unlikely to average more than 80 to 90 of the average steady state gas velocity There will be a pressure loss across the pig itself and an increasing resistance to flow as liquid accumulates ahead of it On the other hand it is relatively unlikely to average less than 50 of the steady state gas velocity as the pressure buildup
165. x In the Specified column you can enter a value for one of the following three parameters e Pressure Change The difference in pressure between the inlet and outlet of the Unit X is set to a fixed increment or decrement Enter a positive value to specify a pressure gain and a negative value to specify a pressure drop e Pressure Ratio Specifies a fixed value for the ratio expressed as the outlet pressure divided by the inlet pressure e Exit Pressure This parameter allows you to specify a constant absolute value of pressure at the unit outlet The Calculated column displays the actual realized pressure parameters for the Unit X These may vary from the Specified values if the Optional Constraints parameters have been set in such a way as to limit the effect of the pressure parameter settings For example if you entered a Pressure Change of 100 kPa a pressure increase of 100 kPa and a Max Pressure Ratio of 1 5 for a Unit X with an inlet pressure of 100 kPa the outlet pressure would be constrained to 150 kPa rather than increase to 200 kPa Temperature parameters for the Unit X can be set in one of two ways as follows e Temperature Change Specifies a fixed increment or decrement for the fluid temperature across the unit A negative value corresponds to a temperature decrease and a positive value to a temperature increase e Exit Temperature Specifies a constant temperature value for the fluid at the unit outlet The pa
166. your data The PIPESYS View 3 11 3 4 2 Worksheet Tab This tab allows you to directly edit the Material and Energy Streams that are attached to the PIPESYS operation without having to open their Property Views PIPESYS Extension Branch 1 olx r Attached Streams Inlet Outlet PIPESYS Q 1 0000 1 0000 lt empty gt 30 00 21 58 lt empty gt 7500 4535 lt empty gt 500 0 500 0 lt empty gt 1 652e 004 8021 lt empty gt __25 98 25 79 lt empty gt 6 89470e 07 3 79317e 07 3 11359e 04 Cooldown Close Elevation Profile Connections Worksheet 3 4 3 Methods Tab Many correlations and models have been developed by researchers to perform multiphase flow calculations PIPESYS makes many of them available to you on the Methods tab Completion of this tab can be a simple matter of selecting one of the two fluid system classifications and allowing PIPESYS to automatically choose the calculation methods Alternatively if you are familiar with multiphase flow technology you are able to specify which methods should be used 3 11 2 The Main PIPESYS View The Main PIPESYS View 3 12 Examples of gas based systems include dry gas gas condensate and gas water systems Examples of liquid based systems include hydrocarbon liquid crude oil and oil gas systems H PIPESYS Extension Branch 1 ojx Recomended Procedures E
167. zontal distance of 300 ft from the starting point and lying ona downward slope of 10 The first three segments of a pipeline elevation profile and the parameters that are used to define its geometry If you enter values into Length and one of Distance or Run the PIPESYS assumes that Angle is positive If Angle is actually negative record the calculated Angle or Rise value delete the contents of the Length cell and enter the negative of the recorded Angle or Rise value into the respective cell 3 14 Enter the Pipeline Units into the Elevation Profile in the order that they appear in the flow stream The PIPESYS View 3 15 The Elevation Profile parameters used to define Pipe Unit endpoints are defined as follows Distance The horizontal position of the endpoint of the Pipe Unit using the Pipeline Origin as the reference point Elevation The vertical position of the endpoint of the Pipe Unit using the Pipeline Origin as the reference point Run The horizontal component of the displacement between the starting point and the ending point of a Pipe Unit Rise The vertical component of the displacement between the starting point and the ending point of a Pipe Unit Length The actual length of the Pipe Unit measured directly between the starting point and the ending point Angle The angle formed between the Pipe Unit and the horizontal plane This value will be negative for downward sloping Pipe Units

Download Pdf Manuals

Related Search

Related Contents

Tivoli Audio MUSIC SYSTEM User's Manual    hit 69 az hit 69 nz eurohit 69 az eurohit 69 nz  fluazinam  取扱説明書  DS9208 - Motorola Solutions  Télécharger - Communauté de Communes Moine et Sèvre  LBWC-26S - Tanguay  WS-100/WS-200S - Olympus America  

Copyright © All rights reserved. Failed to retrieve file