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Prode Properties

1. Stream Operating Select edit stream 10 z Save Components Operating Conditions 175 621 K 1 572e 006 Pa a 1 kg s Models BIPs Config Chemicals Feed and Operation BIPs Specifications 200 K 37 bar a 1 kg s Br Licence Specifications OUT 15 72 bara kW Phase Mol fraction j 0 000572496 CH4 0 982 0 982543 0 0334615 0 o o c02 0 018 0 0174567 0 966538 lo o o the procedure calculates an outlet temperature of 175 6 K at 15 72 Bar a there is a solid phase mainly composed by CO2 We can compare these results against vapor solid equilibria data Experimental data vapor solid equilibria 176 04 K 15 72 Bar a Calculated values 175 6 K 15 72 Bar a 27 In next example we estimate the initial discharging temperature of a fluid contained in a vessel protected by a safety valve the block valves have been closed and the fluid heated at constant volume the mixture is that already examined in previous examples Methane 0 7 Carbon Dioxide 0 15 Hydrogen Sulfide 0 15 with Soave Redlick Kwong model the operating conditions are 60 Bar a and 225 K the discharging pressure is 78 Bar a the method ESirV in cell B3 allows to define the operating conditions and to calculate the specific volume EStrV 1 B2 B1 where 1 is the stream B2 is the inlet temperature and B1 is the inlet pressure SOMMA y Xv amp amp EStrv 1 B2 B1 A Operating Pressure OperatingT
2. gt Plol o o ol o ol o o o o o o o o o gt 9 9 9 9 9 9 9 o9o jojojojojuovjovjN gt 19 9 9 9 9 9 9 9 9 9 9 9 9 oj jo gt 9 9 9 gt 9 o o ojojojojojofjNj j gt 9 9 9 9 9 9 9 9 9 o9oj jo IMPORTANT For BIPs the first two columns Ci and Cj define the component s position in the list i e 1 for the first component 2 for second and so on while othe colums allow to enter the values for the different BIPs required by selected model note that some values for example in Wilson NRTL etc models have units of cal gr mol Example binary of methanol and ethyl acetate UNIQUAC A12 64 1299 A21 644 1931 in the first two columns c1 c2 enter the components relative position in the list assuming that methanol is the first component and ethyl acetate the second c1 c2 BIP 1 BIP 2 1 2 64 1299 644 1931 MPORTANT Prode Properties allows to define Temperature Dependent BIPs for models as Soave or Peng Robinson Temperature Dependent BIPs provide a better accuracy than Temperature Independent BIPs the database includes many Temperature Dependent BIPs BIPs in database have been calculated from VLE points at temperatures about 300 K and may not produce reliable results at temperatures far from 300 K in those cases a typical application could be a phase envelope it is recommended to use Temperature Independent Blips or calculate new BIPs for the required
3. ef ee ae el Peng Robinson Standard Multiphase equilibria No multiphase only two phases Multiphase initialization Reduced tests quick Detect Phase State Phase diagram check stability against feed From Gibbs or Isothermal Compr and Liq Dens Discard unstable solutions Phase diagram specified phase fraction lines we can edit BIPs from Stream gt BIPs dialog Prode Properties Editor End when crossing phase boundary lines Stream Operating Components Models Config Chernicals BIPs Licence Remember if you have changed some values in Stream gt Operating dialog click on Save button to save the stream data Edit BIPs Get BIPs Select the model Get BIPs from database for canculating the phase envelope for test case 3 from Excel page phasenv xls enter 3 as stream and 0 001 as liquid fraction and click on button Compute phase diagram 20 A B is D E G H VAPOR LIQUID LIQUID PHASE DIAGRAM in Properties editor define for the specified stream the composition models BIPs for mixtures select Multiphase Vapor Liquid Liquid or Vapor Liquid Solid for calculating multiphase diagrams compute phase diagram 100 00 110 00 190 00 200 00 5000000 000000 4500000 000000 4000000 000000 3500000 000000 3000000 000000 2500000 0000
4. Cance Apply Prode Properties permits to define several different operating parameters these parameters are max number of streams max number of components per stream max number of interaction coefficients pairs per stream e reference temperature and pressure e base values for enthalpy and entropy calc s convergence tolerance max allowed time for solving a operation e Flow units e minimum liquid density to validate liquid phase IMPORTANT before to leave the application remember to save all data into the archive differently your changes will be lost 52 Chemicals data From this page you can e edit and change the physical properties data included in the databank save all data in a file Prode Properties Editor xj E Streary Config ACETYLENE E E Chemicals Sort by first name Data Sort by first name Settings Sort by second name Regess Sort by third name E BIPs Sort by formula E Licence Neene 1 ACETYLENE Neene 2 ETHYNE Noene 3 CAS Kentification number Molecular weight Critical temperature 325 Critical pressure 16 139 006 Critical volume 0 113 Acertric factor 0 187642 Electric dipole moment Radius of gyration 109452010 Solubilty parameter 590 713 Std Enthalpy form 1226766 Gibbs Energy of torm 209340 Erthaipy fusion pe 770 Normal boiling point liag ten Pe s re ox coa f w Edit
5. A simple way for accessing Prode Properties from Excel is to use the methods as macros within the cells supposing we have created a worksheet for solving some problem and we need the values of gas and liquid densities at some specified temperature and pressure first we need to define the stream and the units from Properties menu select Edit Properties to define compositions and the units of measurement x Notice that for the first stream for editing the different streams use the Select edit stream combo there is a mixture of three components already defined you can change the list of components and compositions from Stream gt components and models from Stream gt models MPORTANT Once you modify a list of components it is recommended to edit also Models and BIPs dialogs differently Properties adopts default values If you modify something do not forget to click the Save button before to edit a different stream or leaving the dialog Differently changes will be lost 11 once defined the stream we need to define the units which we wish to utilize in our problem for the pressure first row select Bar a notice that unit for temperature is K and density Kg m3 but you can set the units which you prefer then click on Ok for accept changes and leaving the Properties editor I MCCOOK x Pressure Temperature A Tespenmure Caloritic Value Catontic Value mole Erthalpy Streams Entropy Streams Tanks Heat
6. simplified procedures with limited features Personal Base Extended X X X E1 E1 E1 E1 E1 E1 E3 E3 E3 extended versions available with distribution license Installing the program this paraghaph provides information about system requirements procedures on installing Prode Properties software and upgrading from previous versions Sistem requirements e Microsoft Windows XP Vista 7 8 or later compatible system e 1GB of RAM installed if used in union with Microsoft Excel or other applications e 20 MB of available hard disk space Installation procedure 1 download the last version of the program from Prode server http www prode com 2 if there are previous installations of Prode Properties uninstall the previous version 3 run the program the automatic installation procedure will do the work for you follow the on screen installation instructions note in some operating system you must be logged as a user with administrative privileges to make the necessary changes if you do not have administrative privileges contact your system administrator for assistance To uninstall a Prode Properties installation Use the Add Remove Programs utility in the Windows Control Panel the procedure does all the work for you Obtain the licence Prode Properties is copy protected your personal copy has limited features and to access all the features you must obtain a licence from Prode there are se v
7. Working with Excel The Properties Add In creates a menu which permits direct access to Properties Editor save and load archives In Excel 2003 Properties adds a new item in main menu Dati Finestra 21 hy Properties Edit Properties Open Archive Save a Archive W gt Home Insert Page Layout Formulas Data Review View Add Ins Open Archive Save a Archive MPORTANT Excel 2003 Security Alert Macro when opening Properties files in Excel 2003 you may be requested to fix a Macro Security Warning see below issued by Excel Avviso di protezione x C Program Files Prode Excel props xls contiene macro Poich le macro possono contenere virus in genere consigliabile disattivarle se si desidera evitare eventuali problemi Se le macro provengono da una fonte sicura disattivandole si potrebbero tuttavia perdere alcune funzionalit Attiva macro Ulteriori informazioni To fix the Security Warning click Enable Macro in Security Alert dialog Excel 2007 Security Alert Macro when opening Properties files in Excel 2007 you may be requested to fix a Macro Security Warning see below Security Warning Macros have been disabled issued by Excel o s Home men Page layout Formulas Dete Review View Addins Properties Microsoft Ollice Security Options EEEE e Security Alert Macro Security w Mt t UED ees See Leen eee Macros
8. fid fopen pppdir txt hfile fgetl fid fclose fid loadlibrary ppp dll hfile h uimenu Labe Properties h1 uimenu h Label Edit Properties Callback edSS h2 uimenu h Label Open Archive Callback AOpen h3 uimenu h Label Save a Archive Callback ASave end d calllib ppp StrGD stream end By typing in Matlab the command gt gt SirGD 1 Matlab executes the code within the script it loads ppp dll if not in memory creates a menu bar with the standard Prode Properties commands and then executes the method StrGD to calculate the density Notice that the script creates a menu bar which permits to access directly Prode Properties from Matlab GUI there are three commands edit Streams open a archive save a archive Important features of menu bar the characteristics may depend from Matlab version if you delete the associated figure the menu bar is deleted to recreate the menu you must reenter the commands h uimenu Labe Properties h1 uimenu h Label Edit Properties Callback edSS h2 uimenu h Label Open Archive Callback AOpen h3 uimenu h Label Save a Archive Callback ASave 40 You can write scripts to solve more complex problems an example is the script phaseenvelope m which prints a phase envelope to test the script type in Matlab th
9. to load BIPs Prode Properties Editor Exi 26 We can model the pressure reducer with the predefined H P VLS operation this opetration solves a multiphase flash at specified pressure and enthalpy On first page click on button Save to define the new stream 10 in second grid select the stream 10 select the H P VLS operation define 200 K and 37 Bar a as inlet conditions define 1 72 Bar a as outlet pressure define 0 as dh adiabatic flash click on button Compute to get the results lt lt x Stream Operating Select edit stream 10 bd Save Components Operating Conditions 157 448 K 172000 Paa 1 kys Models BIPs Config Chemicals Feed and Operation BIPs Specifications 200 K 37 bar a j1 kgs Senet Specifications OUT 1 72 bara kw j 0 99957 0 00042961 o CH4 0 982 0 98242 0 00566758 o lo o c02 pms o 0175604 0 994332 p o 0 the procedure calculates an outlet temperature of 157 45 K at 1 72 Bar a there is a solid phase mainly composed by CO2 We can compare these results against vapor solid equilibria data Experimental data vapor solid equilibria 158 12 K 1 72 Bar a Calculated values 157 45 K 1 72 Bar a We can examine a different case define 15 72 Bar a as outlet pressure click on button Compute to get the results Prode Properties Editor
10. 1 stgef 7 1 stgdH 0 0 stgdH 7 0 prod_h stream1 btm_h stream2 fnr 1 fstr stream3 fpos 4 variables reboiler and total condenser specifications component 2 fraction in top product and bottom product to to feed ratio vnr 2 vtype 0 1 ptype 0 4 piv 0 2 prv 0 0 96 viype 1 2 ptype 1 3 piv 1 0 prv 1 0 4 variables reboiler partial condenser and 2 side streams liquid and gas phases specifications component 2 fraction in top product bottom product to feed ratio side streams flow to feed ratio vnr 2 vtype 0 1 ptype 0 4 piv 0 2 prv 0 0 96 viype 1 3 ptype 1 3 piv 1 0 prv 1 0 4 snr 2 sstr 0 stream4 spos 0 4 sft 0 LIQ_PHASE sflow 0 0 12 sstr 1 stream5 spos 1 7 sft 1 GAS_PHASE sflow 1 0 078 77 Methods for Reactors Note this method utilizes the standard ANSI C convention for exchanging parameters see the samples provided with the software simulation of reactors int res REACT int streamin streamOut int model int NrReactions double Conv double Pout double dHeat Parameters streamIn int inlet stream streamOut int outlet stream model int model for reactor see below NrReactions int number of reactions Conv double matrix NrComponents NrReactions to specify reactions Pout double output pressure dHeat double heat added removed Codes for models Gibbs 1 Equilibrium Reac
11. CompMw integer code given the component code returns the relevant molecular weight double tc CompTc integer code given the component code returns the relevant critical temperature double ac CompAc integer code given the component code returns the relevant acentric factor double vc CompVc integer code given the component code returns the relevant critical volume double pc CompPc integer code given the component code returns the relevant critical pressure double dm CompDm integer code given the component code returns the dipole moment double rg CompRg integer code given the component code returns the radius of gyration double sol CompSol integer code given the component code returns the solubility parameter double hf CompHf integer code given the component code returns the std enthalpy of formation double gf CompGf integer code given the component code returns the Gibbs energy of formation double sf CompSf integer code given the component code returns the enthalpy of fusion double nb CompNb integer code given the component code returns the normal boiling point 85 double mp CompMp integer code given the component code returns the melting point double p CompVP integer code double t given the component code and a temperature returns the calculated saturation pressure calculated via Chemical s file temperature dependent correlation double h CompHG integer code double t0
12. Release 1 17 2010 included method PIPE Release 1 18 2010 included methods HPFORM HTFORM Release 1 2 2012 maintenance version for porting in different platforms Features available vs Versions Database with more than 1600 chemicals Database with more than 25000 BIPs SRK PR vdW mixing rules SRK PR WS mixing rules LKP BWRS GERG AGA Steam Tables UNIFAC UNIQUAC NRTL Wilson CPA with association Solid Solution Model SRK PR HV mixing rules SRK PR MHV mixing rules SAFT with association GERG 2008 BWR Pitzer NRTL electrolytes Derivatives vs P T W of Fg H S V Properties of fluids and mixtures Vapor Liquid solid isothermal flash operation Vapor Liquid Pf T Pf P flash operations Vapor Liquid solid H P S P V P flash operations Complete set of flash operations Pf H S V Vapor Liquid phase diagram Vapor Liquid Liquid phase diagram Vapor Liquid Solid phase diagram VLE LLE SLE data regression Raw data regression utility Characterization of petroleum fractions Hydrate formation multiphase with std model Hydrate formation multiphase with complex model Multiphase gas liquid pipeline with heat transfer Isentropic nozzle HEM HNE Isentropic nozzle HNE DS NHNE Polytropic stage single phase gas Polytropic stage multi phase gas liquid Distillation column gas liquid Distillation column gas liquid liquid and liquid liquid Depressuring unit blow down Reactions
13. Config l Chemicals BIPs Data Regress Models Licence 85 101327 Pa a Max press in data set 101327 Pa a X Y data fitting error 0 358844 0 349532 0 309601 K12 T2 0 16291 0 528678 to test the accuracy of calculated BIPs in estimating freezing point depression in Prode Properties Editor select a new stream and define as composition H2O 0 728 CH40O 0 272 to test this point in the series x1 y1 T K P Bar g SLE 0 728 0 9999 233 45 0 CT x Components Sort by first name Models BIPs Molar fract 0 1 Config Chemicals BIPs Data Regress Models Licence then in Models tab select the same models adopted in data regression CPA PR for vapor CPA PR for liquid SP CPA for solid Prode Properties Editor E x 16 PRX UNIQUAC WS 17 GERG IS0 18453 18 AGA ISO 29765 19 PRX NRTL MHV2 20 PRX NRTL LCVM No multiphase only two phases v Multiphase initialization Standard tests x In BIPs tab select SLE BIPs Data set and click on Load BIPs button to get BIPs make sure that values shown on window are those previously calculated Prode Properties Editor xj Stream Operating Components Models BIPs Config Chemicals BIPs Data Regress c1 c2 BIP 1 BIP 2 BIP 3 BIP 4 BIP 5
14. E Chemicals B BIPs Do not accept calc X Y outside 0 1 range Mason o Dat measured VLE LLE date points hed Licence 0 15000 15000 E x 0 00904155 0 024782 3 9458 00603876 11 1947 0 1432 Ja 52579 e i di as alternative the procedure offers the option to calculate the best fitting parameters to VLE data points calculated with UNIFAC ale ul CN KA 0 257608 0 505018 0 602671 0 785693 this entirely predictive method doesn t require experimental data and in some cases can result useful 58 Select VLE points calculated with UNIFAC in Regress selector to use this method Prode Properties Editor a fevess iE portato wannrac VELLE X4 Y4 Temperature Pressure Xocal Eror Mie fossas fosrona s0507 Khios Eesajosass 00048209 C M a E T A pe fossis ososss7 s0175 Mhios esaj _Joostees6 Me pf rossse Josteose oor 006 hior Kesaj 7essos loosersee Moe gfo 7337 Jossaose oer 23 hosa ejos Me foses seers 2839 jo oe CCC CEC CE Ejo ye Bfosveres onznes_ sa770 o a os Once the paramters have been calculated you must select the Transfer button to transfer the results in BIPs gt Data page from that page you can save the calculated BIPs in database select Save button or store permanently in file select File button Prode Properties Edi
15. Prode Properties permits to define complex topologies as there is no limit to the number of operating blocks required for simulating a plant with Prode Properties for simulating a plant you convert the different sections into pieces of code to do so you can use the basic blocks available in all process simulators for esample e isothermal flash for calculating multiphase equilibria at the specified temperature ad pressure e flash unit enthalpy entropy or volume basis calculates output temperature or pressure with this unit you can simulate pipelines valves heat exchangers pumps compressors and many others operations e fixed vapor fraction flash for constructing phase envelopes calculating bubble and dew points etc e mixer to add the contents of two streams e divider to subtract a part of flow from a stream by putting together these blocks it is possible to simulate also complex plants Simulating a plant transform the flow sheet in a simulation block diagram fluid and energy flow diagrams are standard engineering tools you assign a number to the different streams and identify the basic blocks which will be solved by Prode Properties Notice the number which identifies each stream in this case different numbers mean possible different compositions we do not consider chemical reactions here the output of each block can be easily calculated providing the input has been defined 44 Working with archives save and load da
16. double t1 given the component code initial and final temperatures for integration returns the calculated ideal gas enthalpy calculated via Chemical s file temperature dependent correlation double s CompSG integer code double t0 double t1 given the component code initial and final temperatures for integration returns the calculated ideal gas entropy calculated via Chemical s file temperature dependent correlation double h CompHL integer code double t0 double t1 given the component code initial and final temperatures for integration returns the calculated ideal liquid enthalpy calculated via Chemical s file temperature dependent correlation double s CompSL integer code double t0 double t1 given the component code initial and final temperatures for integration returns the calculated ideal liquid entropy calculated via Chemical s file temperature dependent correlation double h CompHS integer code double t0 double t1 given the component code initial and final temperatures for integration returns the calculated ideal solid enthalpy calculated via Chemical s file temperature dependent correlation double s CompSS integer code double t0 double t1 given the component code initial and final temperatures for integration returns the calculated ideal solid entropy calculated via Chemical s file temperature dependent correlation double h CompHV integer code double t given the component c
17. modify data select a component from the component s list e edit modify the related fields see also the section with description of all fields select the Save button to save the modified data differently new data will be discharged Adding a new component e select the New button e edit the related fields see also the following page with description of all data fields e select the Save button to save the data differently new data will be discharged Remove a component select a component from the component s list select the Remove button IMPORTANT Updating the file which contains the databank this option permits to store all data into a file differently all changes will be lost when leaving the application select the File button CAUTION you may wish to create a backup of the file chem dat before to overwrite the file 53 Chemicals Settings From this page you can e edit informations CAS number required to identify some components Prode Properties Editor lee SSOS SCS Ewe OSSCS SSCS pie e pote Ci SC S pw SCiSSSC S Hn Ss Way e Ee 54 Regress raw data From this page you can regress raw data into values compatible with chemical s database Prode Properties Editor yearhteot 2 0 t 3 y exp a bt c in t a t S y a 1 tb c ln t r trys yea 1 tryb e 1 try 2ed 1 1r S yaarb 1 trec ln 1 trye
18. you may wish to utilize a different separator for eample EStrGD 1 300 1 0E5 instead of EStrGD 1 300 1 0E5 IMPORTANT as first step you must load the add in file properties xla which instructs Excel about Prode Properties library you need to go through this procedure only once to load the add in Excel 2003 open Excel and choose the Tools Add ins menu item you ll see a list of add ins some checked some not checked If Prode Properties isn t listed and it won t be unless you went through this procedure earlier browse for the properties xla file in Excel folder then back your way out Now Prode Properties should be listed in the list of add ins its box should be checked and you should see a Prode Properties menu in Excel If you close Excel and then reopen it Prode Properties menu must still be there Once you installed the add in you ll be able to access Prode Properties from within Excel see below Excel 2007 and more recent versions open Excel and choose Excel Options item then Add Ins on the bottom select Manage Excel Add Ins and click Go you ll see a list of add ins some checked some not checked If Prode Properties isn t listed and it won t be unless you went through this procedure earlier browse for the properties xla file in Excel folder then back your way out Now Prode Properties should be listed in the list of add ins its box should be checked If you click on Add Ins you should see the Properties menu see below
19. 0 7 Carbon Dioxide 0 15 Hydrogen Sulfide 0 15 this is the Mixture 1 provided as example a from Properties menu select Edit Properties b in Stream gt Operating dialog select the stream number 1 label Mixture 1 c In Stream gt Components verify the composition Methane 0 7 Carbon Dioxide 0 15 Hydrogen Sulfide 0 15 d In Stream gt Models we verify that model fugacity is SRK for gas and liquid e In Stream gt BIPs we input BIPs or verify that procedure loads BIPs from database f in Stream gt Components Save the stream g set as feed stream the first Mixture 1 as operation T P VL isothermal two phases flash as specifications 150 K for temperature and 10 Bar a for pressure then select Compute Prode Properties Editor xi Select edit stream 1 Test Case 1 Test Case 1 Save Operating Conditions 150 K 1e 006 Pa a 1 kg s The procedure detects one liquid phase a define TP VLL isothermal vapor liquid liquid and select Compute NOTE the procedure may detect two or three liquid phases depending from values of BIPs Prode Properties Editor x Steam Operating Components Models BIPs Feed and Operation 1 Test Case 1 i Config Specifications 150 K 10 bar a kgis Chemicals Specifications OUT Paa w BIPs w Licence Select edi stream 1 Test Case 1 Operating Cordiions 150 K i Test Case 1
20. 16 Next example permits to calculate and graph tables of values in a range of temperatures for many different properties liquid fraction cp cv density viscosity thermal conductivity speed of sound and for both gas and liquid phases for doing this we ll use a predefined Excel page from Excel menu File gt open in Excel folder in Prode Properties installation select the file props xls If you wish you can modify the stream composition or the units of measurement in that case as before from Properties menu access the Properties editor and modify the previous data Then enter in the proper units the desired range of temperatures cells B2 B3 and the operating pressure cell B4 and click on compute button to calculate the data Prode Properties will print the values with the desired units of measuremebt PECET UER E EEE C Bins GCS EEESC c 1 from Properties menu select the editor and define composition mod nosis ac options for the stream you wish to compute you can also specify the ur 2 on this page specify operating pressure and a range of temperatures LCp kJ4k ag KiGCp ki tha KYLCY kidk K GCyv kJikg K LOkgm3 GD kgm LV Pa s GVPa s LC Warn K 1 100 2S58E 00 O 00E 00 179E 00 OO0E00 664E 02 O O0E 00 164E 03 0 00E 00 2 418 01 100 263E 00 000E 00 169E 00 0 00E 00 6276 02 0 00E 00 6 38E 04 0 00E 00 205E 01 0 32 1766 00 2 24E 00 92E 01 1 53E 00 109E 03 7 39E 00 1 436 03 5 74E 06 2746 01 0 27 176E 00 8 2 03E 00 9
21. 40E 01 142E 00 106E 03 6 69E 00 7 72E 04 6 82E 06 2 56E 01 014 183 00 1 67E 00 S44E 01 1 20E 00 986E 02 6 97E 00 5 08E 04 8 13E 06 2 47E 01 0 00 000E 00 1 52E 00 000E 00 1 106700 000E 00 6 86806E 00 000E 00 9246 06 000E 00 000 000E 00 1536 00 O00E 0D 112E 00 000E 00 6 09E 00 000E 00 1 016 05 O00E 00 0 00 000E 00 154E 00 O00E 0D 1 14E 00 000E 00 5526 00 000E 00 1 096 05 000E 00 0 00 000E 00 1 56E 00 000E 00 147E 00 000E 00 5 05E 00 000E 00 1 17E 05 000E 00 0 00 OOOE 00 1 59E 00 000E 00 1 20E 00 O00E 00 466E 00 000E 00 1 25E 05 000E 00 No errors errors may be originated when accessing the chemical s data base with wrong parameters iL catculating liquid properties for ternperatures below freezing point or above criftcal point etc If You find errors lirait the temperature range Liqnad fraction vs temperature cick on rectangle Molar liquid Fraction vs temperature 17 Next example will permits to calculate and graph a phase diagram phase envelope to do this we ll use a predefined Excel page from Excel menu File gt open in Excel folder in Prode Properties installation select the file phasenv xls If you wish you can modify the stream composition or the units of measurement in that case from Properties menu access the Properties editor and modify the previous data remember to set the same equation of state for gas and liquid fugacity and dont forget to save the stream button Save in first dial
22. 8 402213 1246848 6 65E 18 57 791 44 300 15045 503573 5 27 92731 0 426463 6 540123 6 052677 1290783 5 54E 17 57 724 43 300 40037 504235 7 27 8959 0 424897 6 474781 7 789158 1320706 4 57E 16 57 675 42 300 57011 504898 27 87445 0 424013 6 439535 7 597766 1341315 3 75E 15 57 644 41 306946 5055102 27 85993 0 423533 6 419117 7 461665 1355561 3 06E 14 57 6231 40 300 79124 506122 4 27 95021 0 423306 6 406866 7 366011 1365403 2 5E 13 57 608 39 30066972 5067347 27 84387 0 423244 639955 7 299302 1372177 2 03E 12 57 598i 38 300 93595 507346 9 27 83988 0 423235 639541 7 253066 1376811 1 65E 11 57 592 37 30099576 45079592 27 83753 0 423423 6 393393 7 221216 13 7995 1 34E 10 57 588 36 301 04574 508571 4 27 83633 0 423604 6 392825 7 199435 1382047 1 08E 09 57 586 35 301 0935 509189 7 27 83593 0 423822 6 393254 7 104656 1383417 8 74E 09 57 504 34 301 13572 509795 9 27 53608 0 424066 6 394374 7 17484 138428 7 066 08 57 584 33 301 18181 510408 2 27 83662 0 424328 6 395974 7 168409 1384791 57E07 57 504 32 301 22351 511020 4 27 83743 0 424603 6 397904 7 164354 1385056 4596 06 57 505 31 301 26426 511632 7 27 83833 0 424884 6 400042 7 161925 1385145 3 7E 05 57 5861 Eih cote L E auuu T R AGG 146 7 160414 1365067 0 000296 as HA Column 4 the report includes 1 the verified errors in mass and energy balance 2 reboiler and condenser duties 3 temperature and pressure in each stage 4 total and component vapor flows in each stage 5 total and com
23. Number of stages 0 1 with feeding temp set to O procedure calculates teq at specified liquid fract 2 Number of stages 1 0 vapor 1 liquid 0 1 0 no flow 1 all feed flow D not present 1 reboiler 2 total condenser 3 partial condenser 18 Specification type 1 reflux ratio 2 ratio top to feed 3 ratio bottom to feed 4 comp fract in top 5 comp fract in bottom 19 Required value 20 Component component position in list of components for specifications 4 5 0 not present 1 reboiler 2 total condenser 3 partial condenser 1 reflux ratio 2 ratio top to feed 3 ratio bottorn to feed 4 comp fract in top 5 comp fract in bottom 25 Component component position im list of components for specifications 4 5 2 n Solve Column Results 2 29 Error mass and energy balance BW Reboiler duty 31 Condenser duty The steps to define a column are easy to follow 1 define the number of stages 2 define pressure distribution bottom and top stage 3 define stage efficiency 4 define the number of feeds each feed flow rate and compositions click on the proper Feed button to access the stream editor each feed stage remember that reboiler if present is stage 1 and condenser if present is stage N and the liquid fraction or the temperature of each feed 5 Define the number of side streams if any the stage the type vapor or liquid flow and the flow specification 6 Define variables as c
24. form of Dynamic Library DLL Active X for direct access from Windows applications Microsoft Excel Visual sae applications including NET Borland applications MATLAB MathCad etc Windows XP Wndows Vista Wndows 7 8 etc support for up to 500 different streams with up to 100 components per stream user can redefine e Several compilations of chemical data and BIPs are available the user can add new components and BIPs e Comprehensive set of thermodynamic models e Acomplete set of flash operations T P H P H T S P S T V P V T H V S V H S constant energy phase fraction Functions for calculating specific properties of mixtures critical point Cricodentherm Cricondenbar cloud point etc e Functions which calculates values and derivatives of fugacities enthalpy entropy volume vs temperature pressure composition e Functions which return equilibrium lines at specified phase fractions generation of phase diagrams e Functions for simulating operating blocks as mixer gas separator liquid separator distillation column compressor pipe e Functions for component property access from database e Functions for stream property calcs density conductivity and viscosity for both gaseous and liquid phase surface tension speed of sound Joule Thomson etc Dynamic Link Libraries A dynamic link library is a binary file that acts as a shared library of functions that can be used simultaneously by multiple applications these l
25. in Excel A 5 MEH D E F G H I J K F M N o P 4 HYDRATE FORMATION CURVE 2 From Properties editor define the composition including at least one hydrate former C1 C2 C3 IC4 nC4 N2 CO2 H2S and water amount 3_you can specify different inhibitors as Methanol Ethanol Ethylene glycol plus salts electrolyte model required 4 Tmin ist Tmax Compute Hydrate Formation Curve 6 Model 1 SI SIl SH 2 SI 3 SIl 7 Stream 8 Errors No errors 9 10 240 00 250 00 260 00 270 00 280 00 290 00 300 00 310 00 Hydrate Formation Conditions 11 42000000 00 K Paa 12 250 00 480384 87 13 252 27 530562 97 14 254 55 578975 91 15 10000000 00 256 82 624493 19 16 259 09 665074 15 Be 28 1 5 8000000 00 265 91 736468 29 PyISegedes y HE aga TF sas 6000000 00 275 00 916982 78 pie a8 E F 1 rfl Mm 27 4000000 00 28409 301496160 28 286 36 3899372 39 29 288 64 4939146 20 30 290 91 6008937 95 AnnAnAN AN M4 gt gt Foglio 3 Tal m 38 Getting started from MATLAB IMPORTANT Microsoft MATLAB support files are located in the directory Prode MATLAB MATLAB provides two ways to access external libraries as Prode Properties direct access access through scripts and mex files Direct Access Direct access is through the command line interface this interface lets you load an external library into MATLAB memory and access functions in the library to load Prode Properties in MATLAB ente
26. integer cj given a stream position in interaction coefficients list and second component reference sets the component s reference in interaction coefficient s list int model getMB integer stream integer pos given a stream and position in interaction s coeff list returns the related model an integer that identifies the model integer res PutMB integer stream integer pos integer model given a stream position in interaction coefficients list and a model identifier sets the model in interaction coefficient s list 73 double BIP getBIP integer stream integer pos integer id given a stream position in binary coeff list and BIP identifier 0 max nr of BIPs for that model returns BIP integer res PutBIP integer stream integer pos integer id double Kji given a stream position in binary coeff list BIP identifier 0 max nr of BIPs for that model and value stores BIP in that position of the list 74 Methods to define stream s operating conditions Prode Properties includes a set of functions to define the intial operating condition of a stream these can be utilized as alternative to the standard initialization via setOp method typical application E call rstValidSop define compostion in phase 1 with putW define phase fraction with putPF define phase type with putPT set phase 1 as valid setValidPhase continue with another phase 2 n define temperature with putT defin
27. integer stream given a stream returns the acentric factor mole fraction average 72 Methods for stream s definition Prode Properties includes a set of functions to define a stream by program as alternative to utilize the Properties Editor typical application E call initS define the list of components with putCC define the mole fraction of each component with putZ call setS to define the stream utilize the methods described in paragraph Methods to define thermodynamic models to define the models call setW to define the flow call loadSB to load the BIPs from database as alternative to define specific BIPs utilize the methods PutCi PutCj PutMB PutBIP integer res initS integer stream given a stream initializes all data for successive data transfer operations This method must be called before restoring stream s data from archives files etc integer res putCC integer stream integer pos integer compcode given a stream component s position in component s list and component code sets the code in component s list integer res putZ integer stream integer pos double Zi given a stream comp s position and Z sets the comp s pos in Z vector composition molar basis for that stream integer res setS integer stream given a stream performs a sequence of validating operations on data This method must be called after to have restored stream s data from archives files etc Met
28. integer stream given a stream returns the specific heat capacity constant pressure liquid phase double cv StrLCv integer stream given a stream returns the specific heat capacity constant volume liquid phase double cp StrSCp integer stream given a stream returns the specific heat capacity constant pressure solid phase double ss StrMSS integer stream given a stream returns the speed of sound gas liquid as calculated with HEM model for mixed phases double ss StrGSS integer stream given a stream returns the speed of sound in gas phase double ss StrLSS integer stream given a stream returns the speed of sound in liquid phase double jt StrGJT integer stream given a stream returns the Joule Thomson coefficient in gas phase double jt StrLJT integer stream given a stream returns the Joule Thomson coefficient in liquid phase double ic StrGIC integer stream given a stream returns the isothermal compressibility coefficient 1 V dV dP in gas phase double ic StrLIC integer stream given a stream returns the isothermal compressibility coefficient 1 V dV dP in liquid phase double v StrGVE integer stream given a stream returns the volumetric expansivity coefficient 1 V dV dT in gas phase double ic StrLVE integer stream given a stream returns the volumetric expansivity coefficient 1 V dV dT in liquid phase 70 double s StrGS integer stream given a stream ret
29. phase fraction range 0 1 state gas liquid solid and position n calculates and returns the nth n 1 5 equilibrium pressure along the specified phase fraction line double t LfPF integer stream double p double If Given a stream the pressure and Liquid fraction range 0 1 calculates and returns the first equilibrium temperature along the specified phase fraction line double p LfTF integer stream double t double If Given a stream the temperature and Liquid fraction range 0 1 calculates and returns the first equilibrium pressure along the specified phase fraction line double t HPF integer stream double p double h double et Given a stream final pressure the required final enthalpy see the method StrH for the definition and a estimated value for final temperature or 0 for automatic estimate method solves the flash operation enthalpy basis and returns final temperature double p HTF integer stream double t double h double ep Given a stream final temperature the required final enthalpy see the method StrH for the definition and a estimated value for final pressure or 0 for automatic estimate method solves the flash operation enthalpy basis and returns final pressure double t SPF integer stream double p double s double et Given a stream final pressure the required final entropy see the method StrS for the definition and a estimated value for final temperature or 0 for automatic es
30. range of temperatures 50 Config Units From this page you can e define the unit of measurement for the different properties Prode Properties Editor xj gt Stream doira Unts Temperature dt Settings E Chemicals BIPs Calorific Value Licence Calorific Value molar Enthalpy Streams Entropy Streams Flow mass basis Flow gas mass basis IMPORTANT Prode Properties is a collection of functions for thermodynamic calculations these functions receive data of properties such as temperature or pressure a reference to a stream etc and perform some operations With Prode Properties you have complete control over the engineering units this means that program permits to select from a list of different units for each property and Prode Properties automatically converts the input values and the results according to the selected units 1 if you set Bar a as unit for pressure all inputs and outputs will be in that unit 2 if you wish to define your own set of units remember before to leave the application to save data into a archive otherways your changes will be lost 51 Config Settings From this page you can e define the different settings as max number of streams the temperature and pressure at reference conditions the base values for entalpy and entropy convergence tolerance etc Prode Properties Editor mamsen ax runter ot components persen SSS
31. stream pressure and temperature performs an isothermal flash and returns the flammability rich limit gas phase double s ESirS integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the relative entropy gas liquid phase double d EStrLD integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated liquid density at operating conditions double d EStrGD integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated gas density at operating conditions double tc EStrLC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated liquid thermal conductivity at operating conditions double tc EStrGC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated gas thermal conductivity at operating conditions double v EStrLV integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the r calculated liquid viscosity at operating conditions double v EStrGV stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated gas viscosity at operati
32. stream returns the averaged molecular weight all phases double v StrV integer stream given a stream returns the specific volume as sum of specific volumes of all phases double mw StrGMw integer stream given a stream returns the averaged molecular weight gas phase double mw StrLMw integer stream given a stream returns the averaged molecular weight liquid phase 69 double h StrH integer stream given a stream returns the total stream enthalpy gas liquid solid phases double h StrGH integer stream given a stream returns the total stream enthalpy gas phase double h SirSGH integer stream given a stream returns the specific unit weight enthalpy gas phase double h StrLH integer stream given a stream returns the total stream enthalpy liquid phase double h SirSLH integer stream given a stream returns the specific unit weight enthalpy liquid phase double h StrSH integer stream given a stream returns the total stream enthalpy solid phase double h StrSSH integer stream given a stream returns the specific unit weight enthalpy solid phase double cp SirGICp integer stream given a stream returns the ideal gas heat capacity double cp SirGCp integer stream given a stream returns the specific heat capacity constant pressure gas phase double cv StrGCv integer stream given a stream returns the specific heat capacity constant volume gas phase double cp SirLCp
33. the internal reference user defined for atmosferic pressure quantity 92 Application examples We present here some notes about Prode Properties applications in form of FAQ that should assist users to easily extend features or add interfaces Tips on creation of Prode Properties applications Include a command menu button etc for accessing the Properties Editor method edS stream e Ensure that units of measurement are those defined in Prode Properties or include methods to set the units Use isSDef method to test a streams validity before accessing the stream Accessing an undefined stream generates a large numbers of errors e Include functions for controlling error messages if you have extended calculation sequences When managing error messages ensure that you test at the end of the calculation sequence to capture any problems that may have occurred e When debugging always attempt to limit the complexity of problems and expand progressively to the full application retesting at intervals as you expand the scope of your problem User defined ID for accessing the components in chemical s file In Prode Properties each component in chemical s file includes a ID which permits to access that component this feature permits to maintain a unique identification number also when the chemical file changes The ID must be a integer type as default the CAS number has been adopted but the user may edit and change this value from
34. the molar entropy Kj Kmol K and related derivatives vs temperature pressure composition integer res SirVv integer process integer state double t double p double w double V Given a predefined stream the required state vapor liquid solid and operating conditions returns the molar volume M3 Kmol integer res SirVvd integer process integer state double t double p double w double V double dVt double dVp double dVw Given a predefined stream the required state vapor liquid solid and operating conditions returns the molar volume M3 Kmol and related derivatives vs temperature pressure compositionMethods for stream s data access 82 Extended methods for accessing stream s properties These functions which are otherways equivalent to standard methods permit in addition to set the operating conditions at which the required property must be evaluated This may result useful in many cases for example when utilizing Prode Properties methods as macros from Excel cells Caution the isothermal flash will reset any previous settings and you should use with care these methods in sequential calculus double mw EStrGMw integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the molecular weight for gas phase double mw EStrLMw integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns
35. 0 T get all prop ShowLF Text ShowGF Text ShowLD Text ShowGD Text us 26 UM c ShowDUM Text ShowLV Text ShowG Text 31 We ShowVUM Text ShowLc Te ShowGc Text us 30 om ShowCUM Text geestns um ShowLS Text CStr StrLss Stream ShowGs Text CStr Stress Streem us 37 UM code for velocity you can then modify the code according your requirements 43 Solving problems introduction There are several different classes of problems which Prode Properties can help to solve but the most common are probably e physical properties of pure fluids and mixtures equipment design e system simulation Prode Properties provides many methods for the prediction of physical properties in general a single instruction is required for calculating a property The design and rating of unit operations as distillation columns towers pumps compressors valves heat exchangers etc is another area where Prode Properties can result useful the use of programming languages is generally suggested when dealing with complex problems while some formula in a worksheet can solve the usual work The system simulation may be used in the design stage to evaluate parameters to help achieve an improved design or applied to existing systems for optimizing operating conditions Generally the required solution is the list of operating conditions at the input and output of the operating blocks in t
36. 00 2000000 000000 1500000 000000 1000000 000000 500000 000000 0 000000 Errors Pc 1 Te 1 Pc 2 Te 2 CricoT CricoP Vap Lig 111 596928 116 596928 121 596928 126 596928 131 596928 136 596928 141 596928 146 596928 151 596928 156 596928 161 596928 166 596928 171 596928 176 596928 181 596928 183 354908 185 048330 186 684247 188 270443 189 819317 191 411627 gt WiN Foglio1 Disegno i Formey a OoN s2 el a Ov wvrAe saturation point pressures at a given temperature fd No errors Pa a 101327 400000 150101 857739 214993 381501 299063 519059 405520 615220 537693 093286 699009 438355 892984 620532 1123212 303718 1393361 830073 1707178 401977 2068483 534626 2481168 746341 2949161 313631 3476277676446 3676277676446 3876277676446 4076277 676446 4276277 676446 4476277 676446 4676277676446 Observe that for this mixture the dew line the red line below the critical point shows up to three different equilibrium points at the same temperature the area around 190 k if you add the saturation point on the bubble line black line we have atotal of four Prode Properties can calculate accurately all these points Prode Properties includes methods for calculating equilibrium points at specified conditions see the paragraph Methods for thermodynamic calc s for details methods LfPF LfTF as the name says are based on a liquid fraction specification th
37. 16701 215 570475 219 245639 222 990765 226 869453 230 974772 235 464574 240 676261 251 657871 261 687871 Pa a 101327 400000 209821 932583 387163 901311 653260 311412 1026788 594670 1623711 144481 2155559 267187 2927065 724007 3832537 367877 4850233 641685 250233 641685 5650233 641685 6050233 641685 6450233 641685 6850233 641685 7250233 641685 7650233 641685 8050233 641685 8450233 641685 8974287 488365 8852859 810615 Operating e y Test Case 2 Components Operating Conditions Models BIPs Config Chemicals Feed and Operation 1 Test Case 1 BIPs Specifications 288 15 Licence Specifications OUT 19 we can edit the list of components and the fraction of each component selecting the Stream gt Components dialog this mixture includes two components with molar fractions Methane 0 999 n Butane 0 001 Prode Properties Editor Stream Operating Components Models BIPs Config Chemicals H BIPs Licence ABIETIC ACID Sort by first name Molar fract 0 1 Add Component Remove Clear Molar fract 0 1 METHANE n BUTANE we can modify models and options in Stream gt Models dialog in this test case we adopt Peng Robinson PR VDW for both gas and liquid Prode Properties Editor Stream Operating Components Models BIPs Config Chemicals BIPs Models Licence
38. 2 1000000 000000 197 745203 4183740 460403 esa 202 745203 4694444 623736 204 639752 4894444 623736 MPORTANT The procedure for calculating a phase diagram allows different settings you can modify these settings from the dialog Stream gt Models in Properties editor Multiphase equilibria Multiphase vapor liquid Multiphase initialization No multiphase only two phases z Multiphase vapor liquid Volume correction cubic EOS Multiphase vapor liquid solid Detect Single Phase State From Gibbs Energy or Isothermal Compressibility Check stability against feed Discard unstable solutions Phase diagram specified phase fraction lines End when crossing phase boundary lines Select EOS roots according state Phase diagram calculation Lola lel Set EOS Parameters Standard Parameters Check stability against feed option permits to test stability of calculated points against feed unstable points are not printed to show all calculated points change the settings Phase diagram specified phase fraction lines allows to end or continue lines after crossing a phase boundary set to end when crossing phase boundary lines to avoid generating lines containing inconsistent data Phase diagram calculation option allows to select the EOS root for minimum Gibbs energy or according the state Hpwever the most important setting is the multiphase equilibria oprion which allows to calculate 1 vapor liquid phase di
39. 5 x fe EstrH 1 B2 B1 B4 vi A A e 1 Inlet Pressure 8900000 Pa a 2 Inlet Temperature 246 K 3 Outlet Pressure 7912000 Pa a 4 Heat Duty 71 9 Kw 5 Specified Enthalpy 5068 730115 kw 6 Calculated Outlet Temperature 232 1537271 K 7 then with HPF you calculate the final temperature at specified enthalpy the initial enthalpy calculated at 89 Bar a and 246 K plus or minus the specified heat duty HPF 1 B3 B5 0 0 where 1 is the stream B3 is the outlet pressure B5 the required heat duty and 0 0 is the estimated final temperature set to 0 0 for automatic initialization B6 v fe HPF 1 B3 B5 0 A i ci i 1 Inlet Pressure 8900000 Pa a 2 Inlet Temperature 246 K 3 Outlet Pressure 7912000 Pa a 4 Heat Duty 71 9 Kw 5 Specified Enthalpy 5068 730115 Kw 6 Calculated Outlet Temperature 232 15372711k 7 Prode Properties can solve multiphase equilibria vapor liquid solid hydrate at specified value of enthalpy entropy volume pressure temperature additional specifications are possible 25 in next example we model a pressure reducing valve adiabatic process the stream has composition 0 982 Methane 0 018 CO2 the valve reduces the pressure from 200 K 37 Bar a inlet conditions down to 1 72 Bar a We wish to investigate if at outlet conditions a solid phase is present As first step we define a new stream with composition 0 982 Methane 0 018 CO2 On first page Operating we select first row the stream n
40. 8 From Microsoft Excel edSS edS 8 start editing stream nr 8 From Microsoft Visual C edSS edS 8 start editing stream nr 8 45 Stream operating From this page you can e select a stream select edit stream e define a name for the selected stream save edited stream data e Compute different flash operatins Prode Properties Editor E xj Define a new stream edit existing streams e select the stream you wish to edit define from the Select edit stream list go to page Components define the list of components and relative weights go to page Models define the models for the different properties define settings load BIPs back to page Operating put a name for the stream and click on Save e check that correct stream composition appears on the second grid Compute a flash operation make sure a feeding stream has been properly defined composition models settings then select the feeding stream e select the flash operation e define the required specifications and clik on Compute IMPORTANT before to leave the application remember to save all data into the archive otherways your changes will be lost 46 Predefined Flash Operations Prode Properties allows to solve directly from editor many Flash operations T P VL vapor liquid two phases at specified temperature and pressure T P VLL vapor liquid liquid m
41. 8000 4 0 00977 10246 3 16218 066 33 amp 5000 4 0 0244141 10005 248 15433 553 34 6 4000 4 0 0610352 9473 9284 13880 612 35 2000 4 0 1526879 8458 1037 11372 795 36 0 4 t f a i i 7 7 7 0 3814697 6925 4802 8262 6612 37 0 0002 0 0006 0 0016 0 0039 0 0098 0 0244 0 0610 0 1526 0 3815 0 9537 0 9536743 5144 3443 5276 6996 38 29 Quality The Non Equlibrium models are mainly of interest for short nozzles where the final equilibrium condition predicted by HEM models is not reached cause the residence time of the fluid is too short The HNE models require specific parameters for Prode HNE model a value of 0 75 is suggested for short nozzles but different values may be defined to fit specific data sets 32 Next example permits to solve a distillation column refer to paragraph Methods for solving staged columns for additional information here we use a predefined Excel page as interface to Prode Properties methods From Excel menu File gt open in Excel folder in Prode Properties installation select the file column xls In this page you can define different kind of columns with reboiler condenser one or more feeds and one or more side streams SIMPLE STAGED COLUMN SIMULATION 1 2 3 Number of stages 4 iTop stage pressure 5 Bottom stage pressure 6 7 8 Stage efficiency Number of feeds Feed stage 9 Feeding liquid fraction Feed 1 Feed2 Feed3 Select the button to define feed composition 1
42. BIP 6 a H Models 1 l2 0 349532 0 309601 0 16291 o 528678 o 4 Licence 0 jo Finally in Operating tab click Save Button to define the stream and solve a TP VLS flash operation to evaluate the point of incipient solidification Prode Properties Editor the calculated point is about 235 1 K compare this value with the experimental data 233 45 K utilized in data regression error is about 1 6 K 62 Parameters of models From this page you can e edit the parameters required by the different models available in library Prode Properties Editor Edit modify data e select the components from the component s lists e select the model e edit modify the parameters e select the Save button to save the modified data differently new data will be discharged IMPORTANT Updating the file which contains the Model data this option permits to store all data into a file differently all changes will be lost when leaving the application e select the File button CAUTION you may wish to create a backup of the file bips dat before to overwrite the file 63 Accessing Prode Properties library The technique for accessing the methods available in Prode Properties library will depend on which programming language You use Languages such as FORTRAN C C or Microsoft NET VB C exhibit differences in parameter passing in and out of functions This may requ
43. CS method Release 1 191 1996 Added a set of extended functions for direct access from spreadsheets read the paragraph Accessing Properties from spreadsheet s cells for additional information Release 1 1h 1996 Included a procedure for defining the path to the working directory of program now the file Properties dll can reside in the system directory of Windows while the other files on a different directory Modified the licensing scheme the user receives a signature file this permits to distribute the software via internet Release 1 1h1 1997 Revised the base class for managing memory now the users can specify the number of streams the number of components per stream the number of components in database etc additional information on paragraph Configure Properties Release 1 1h2 1997 Included the procedure edST which permits to define the title when accessing the Stream s dialog included procedures for defining via software the units of measurement modified methods setKM getKM Release 1 1i 1998 New installation procedure Release 1 12 1999 New methods StrSGH StrSLH StrSGS StrSLS StrmCopy Release 1 13 2002 New methods AOpen ASave editSS StrN MStrN putN MputN getSUMS MgetSUMS Release 1 14 2002 New methods StrHC StrFML StrFMH EStrHC EStrFML EStrFMH Release 1 15 2005 New methods getOM setOM Release 1 16 1 5 2009 upgraded dialog interface
44. Capacity hang Meat Capecty mole in Jkmol Flow mass basis kg s Plow gas mass basis bos Denst bgt Density molar bmolim3 Specific Volume mAg Speortic Volume moter miAmol Thermal Conductivity WAMI moonty dynamic Pats telte ke kete kelte ke ke tate ke ke tetetete teketeke Surtace Tensior Nim Lenght finally we can calculate the densities for the specified mixture directly in the cells in B3 we enter the macro EStrLD 1 B1 B2 for calculating liquid density of stream 1 at temperature specified in B1 and pressure specified in B2 in B4 we enter the macro EStrGD 1 B1 B2 for calculating the gas density and in B5 the macro EStrLf 1 B1 B2 for calculating the liquid fraction DSBSHBSI4 4 B 9 IB i DBO BSISG E B 9 SOMMA y X y amp EStrLD 1 B1 B2 SOMMA XV amp EStrLf 1 B1 B2 1 Temperature _2 Pressure 3 Liquid density EStrLD 1 B1 B2 3 Liquid density 1086 37371 4 Gas density 7 1180864917 4 Gas density 7 118086491 Liquid fraction 0 309050931 5 Liquid fraction EStrL 181 B2 6 In B1 we enter 200 as temperature remember we have K as unit and in B2 we enter 5 as pressure remember we have set Bar a as unit densities are in Kg m3 notice that when you change B1 or B2 Prode Properties recalculates these values Now you can modify the stream 1 changing the list of components the compositions or models or the
45. Fortran includes definitions and sample code for Fortran applications Prode NET VBprops includes definitions and samples for Microsoft NET VB applications Prode NET C props includes definitions and samples for Microsoft NET C applications DELteMil stomielle e IMPORTANT When running Properties requires to access several files these are placed in a directory Prode in user space to avoid possible conflicts with code reserved areas the exact path depends from Windows version and settings for example in Windows XP they could be placed in C Documents and Settings All Users Application Data the list of files includes chem dat pseudo dat bips dat mod dat def ppp res lan lic dat do not remove or rename these files if Prode Properties cannot access these files for example because they have been disseminated in different directories an error message Corrupted file error reading data file will be generated Getting Started from Microsoft Excel IMPORTANT the different versions 32 or 64 bit of Excel require different versions of Prode dll library Excel 32 requires Prode dll 32 bit while Excel 64 requires Prode dll 64 bit when installing Prode Properties you must select the version suitable for your copy of Excel IMPORTANT Microsoft Excel support files are located in the directory Prode Excel IMPORTANT Define the proper separator to be used in Macros in Excel Reegional Settings here we assume as separator
46. G CompSol EStrLc HTFORM StrFvd StrLD StrsGs VLLSep getMS putBIP setSOp CompHL CompTc EStrLCp LFLine StrFvdv StrLH StrSH defErrMsg getMSNr putcc setTc CompHS CompVP EStrLCv LSep StrGc StrLIc StrSLH edCF getMV putCi setUMC CompHV CompVc EStrLD LfPF StrGCp StrLJT StrSLs edcs getMod putCj setVc CompHf DCOL EStrLIC LfTF StrGCv StrLMw Strss eds getOM putGij setWm CompID DPF EStrLJT MixF StrGD StrLs StrSSH edss getP putGji CompLC DPLine EStrLMw PIPE StrGH StrLss Strsss edstT getPNr putKji to access a method in a shared library MATLAB provides the command calllib to call functions in the library the syntax for calllib is calllib ppp FunctionName arg argN the FunctionName and arguments are detailed in Prode Properties manual for example we can call the method edSS to edit streams with the command gt calllib ppp edSS in the same way you can access other methods in Prode Properties for example to calculate cp cv and speed of sound for vapor fraction of stream 1 at 300 K and 5 Bar gt gt Calllib ppp EstrGCp 1 300 500000 calllib ppp EstrGCv 1 300 500000 gt gt ans 1 3211 gt gt Calllib ppp EstrGSS 1 300 500000 gt gt ans 374 1625 you can call even complex functions as those to plot a phase envelope or calculate a column for these remember before to pass an array from Matlab to Prode Properties that you must allocate the memory to avoid system errors Finally you can use t
47. ISO std database contains values in Kj Kg Flammability limits mixing rule according Le Chatelier as discussed by Coward amp Jones 1952 Limits in thermodynamic calc s Enthalpy Entropy calc s In Prode Properties the user can specify different initial conditions for enthalpy and entropy see the paragraph Config settings for additional details Temperature pressure ranges Temperature range 1K 5000 K Pressure range 1 Pa 1000 Bar 97 Chemical s File format Note all data dependent correlation s in chemicals file have a range of temperature for application outside this range they may provide inconsistent results Prode Properties checks for this range as defined by high and low limits in chemicals file and attempts to extend data when required when operating conditions are outside the range of application of correlations this may produce in some cases inconsistent results with simple models and properties which require differentiation for example specific heat capacity Flexible data format Prode Properties utilizes proprietary code which allows up to 30 correlations and custom units to define each temperature dependent property all major standards including DIPPR and others are supported Chemical s data file Prode Properties base version adopts the following format Formula string 12 chars max Name 1 main list string 40 chars max Name 2 user defined list string 40 chars max Name 3 us
48. P W Prode Properties includes methods for fast access to the procedures for calculating thermodynamic properties to access these methods create one or more processes with method DPinit passing a integer as process code permitted range of values 1 5 to identify each process and a stream caution must define the stream i e the list of components and molar fractions before to call DPinit then call in sequence the methods for calculating ther modynamic properties passing as first parameter the process code the methods will return the properties calcu lated for the stream associated with that specific process Note Base version allows to define up to 5 iindependent processes example of application DPinit 1 stream StrHv 1 0 t 0 X amp HL StrHv 1 1 t 0 amp HV integer res DPinit integer process integer stream Given a process code 1 5 and a stream the method loads all data integer res StrFv integer process integer state double t double p double w double fg Given a predefined stream the required state vapor liquid solid and operating conditions returns the vector of fugacities Pa integer res StrFvd integer process integer state double t double p double w double fg double dfgt double dfgp double dfgw Given a predefined stream the required state vapor liquid solid and operating conditions returns the vector of fugacities Pa and related derivatives vs temperature K pressure Pa
49. Prode Properties Properties of pure fluids and mixtures User s Manual rel 1 2 PRODE www prode com Contents License agreement sicir ie Seca s an hee stead weet E aE ae s dace el a eins dedecdidoes scan bide deena da eens senna eee 3 GUSTONNG FSU OM issis saa a teeneeatareadetgsecqfaec E E cients ates 3 WAtROGUCHIOMN socorre dives cblet shaved bedee bet lags Eaa aE ended a cael Mak aE bad cvadeddide pecans EEA AEAEE E EEE 4 What S 9 aeeeeeeper rte terre rerere erator a rerrer sy rrcr reer creer Pecer eer mterrr errr eee eree ore reeer eter esr err errr rer erecta erent ere re 5 Installing the program zisrann aae sang ai oe ates Ee ie aea a aaa aE aaa ee aaa 7 Prode Properies QUCK Stal nases eron noie r ANEETA TENE AAA REA E ETEN A AEN ATI ANAG 8 Data files folder siiin inn aadar asear aaea aeea a Oa Eiaa Taa A a aR Ra aa aR E ae ESA ETN oina REEE 8 Getting Started from Microsoft Excel si cs5 eaidcevat disesteniinn iwvlinasteendesltl E E E Leeds 9 Getting Started trom MATIEAB isnie seara iera aiae aada Eeoae a aea Oa SET AEE aA TENE EEEa EREN ENSS 39 ACCESS 10 1 PAWEL LO7 B meren a a A a a eearete terre reer ter 42 Getting started with Microsoft NET VB C applications 2 0 0 cece cecececeeeeeeeneeteeeeeeeeseaeeeaeeeeeeeeaeeseaeesaeeseeseeeseeeseaeeseeeseeeseeeeeeene 42 Solving problems inthOGUCHON aisidas aeaa alvin ania ear aa SE NEES 44 Working with archives save and load data default settings ceeceeececeeeeen
50. RX for solid and HPRX for hydrate the list with predefined packages shows two opions Hydrate CPA PRX based on CPA and Hydrate PRX based on Extended Peng Robinson for this example select Hydrate CPA PRX Prode Properties Editor 7 xi Predefined packages 21 Hydrate CPA PRX____x Hydrate CPA PRX Save 1 SRK standard 2 SRK Extended SRKX 3 PR Standard 4 PR Extended PRX 5 CPA SRK CPA H6 CPA PR 7 LKP 8 BWRS 9 Steam Tables IAPWS 199 PRX V10 PRX Witson REGULAR HYD CPA EIk PRX NRTL 12 PRX UNIQUAC 13 PRX UNIFAC 14 PRX Wilson WS 15 PRX NRTL WS er 46 PRX UNIQUAC WS Multiphase vapor liquid solid hydrate X 17 GERG ISO 18453 Reduced tests quick 18 AGA ISO 29765 From Gibbs or Isothermal Compr and Lig Dens 19 PRX NRTL MHV2 Phase diagram check stability a 20 PRXNRTL Levu Accept all solutions Do not end when crossing phase boundary lines Include all structures which may be generated by formers alela lla H S Hydrate PRX 4 35 IMPORTANT solving hydrate phase equilibria you must define BIPs Prode Properties includes many precalculated BIPs for VLE LLE SLE and Hydrates phase equilibria you may utilize these values when meaured data points are not available if there are doubts about the range of application you may inspect the database for the range of temp
51. Van der Waals and Plateeuw two models available simplified model in Base version and complex model in Extended versions 102 UNIFAC functional groups The underlying idea in UNIFAC method is that a molecule can be considered as a collection of functional groups The main advantage of this approach is that from a relatively small number of functional groups the properties of many different molecules can be predicted The UNIFAC model is useful for estimating solution behaviour in the absence of experimental data Prode Properties incorporates the UNIFAC Group Contribution revision 5 January 1992 J P Baker Following the main groups and subgroups table Code Main Subgroup Example 1 CH2 CH3 Hexane 2 CH2 n Hexane 3 CH 2 Methylpropane 4 C Neopentane 5 C C CH2 CH 1 Hexene 6 CH CH 2 Hexene 7 CH2 C 2 Methyl 1 butene 8 CH C 2 Methyl 2 butene 70 C C 2 3 Dimethylbutene 9 ACH ACH Naphthaline 10 AC Styrene 11 ACCH2 ACCH3 Toluene 12 ACCH2 EthylBenzene 13 ACCH Cumene 14 OH OH n Propanol 15 CH30H CH30H Methanol 16 H20 H20 Water 17 ACOH ACOH Phenol 18 CH2CO CH3CO Butanone 19 CH2CO Pentanone 3 20 CHO CHO Propionic aldehyde 21 CCOO CH3COO Butyl acetate 22 CH2COO Methyl propionate 23 HCOO HCOO Ethyl formate 24 CH20 CH30 Dimethyl ether 25 CH20 Diethyl ether 26 CHO Diisopropyl ether 27 THF Tetrahydrofuran 28 CNH2 CH3NH2 Methylamine 29 CH2NH2 Ethyl amine 30 CHNH2 Isopropylamine 31 CNH CH3NH Dimethylamine 32 CH2NH Di
52. Volume Mass Velocity Acceleration Force Time Heat Flux Thermal Resistance Heat Transfer Coefficent Flow volume basis Viscosity kinematic Energy Dipole moment Solubility parameter Flow Coefficient Compressibility coefficient Joule Thomson coefficient Flow molar basis Volume expansivity UNIT CONV_P CONV_DP CONV_T CONV_DT CONV_HM CONV_HMM CONV_HS CONV_SS CONV_CP CONV_CPM CONV_W CONV_WG CONV_D CONV_DM CONV_SV CONV_SVM CONV_TC CONV_V CONV_ST CONV_L CONV_A CONV_VOL CONV_M CONV_VL CONV_ACC CONV_FOR CONV_TM CONV_HF CONV_TR CONV_HTC CONV_VW CONV_VK CONV_EN CONV_EDM CONV_SP CONV_CV CONV_CC CONV_JTC CONV_WM CONV_VE CODE 15 16 17 18 19 20 21 22 23 24 25 26 27 28 29 30 31 32 33 34 35 36 37 38 39 40 41 42 43 44 45 46 47 48 49 50 51 52 53 54 66 DEFAULT UNIT Pa a pa vK vK Kj Kg Kj Kmol KW KJ K s kd kg K kJ kmol K Kg s Kg s Kg m3 Kmol m3 m3 Kg m3 Kmol W m K Pats N m um ama n m3 Kg m s m s2 wy g KW m2 K m2 KW KW m2 C m3 s m2 s KJ Rein g m3 1 2 Ney 1 Pa K Pa Kmol s v 1 K Introducing Prode Properties library methods Prode Properties library includes a range of methods to deal with
53. agrams see above 2 vapor liquid liquid phase diagrams 3 vapor liquid solid phase diagrams 18 Next example will show a vapor liquid liquid phase diagram a In Excel load the file phasenv xls b select the stream 4 a predefined test case with a natural gas mixture including water c click on compute button to calculate the data A B S D E F G H VAPOR LIQUID LIQUID PHASE DIAGRAM in Properties editor define for the specified stream the composition models BIPs for mixtures select Multiphase Vapor Liquid Liquid or Vapor Liquid Solid for calculating multiphase diagrams Stream compute phase diagram Phase Fract 100 00 150 00 200 00 250 00 300 00 350 00 400 00 120000000 000000 100000000 000000 80000000 000000 60000000 000000 40000000 000000 20000000 000000 penean ae 0 000000 Notice the water dew point line the red line on the right Next example will show a phase digram with up to three dew points at the same temperature a In Excel load the file phasenv xls b from Properties menu select Edit Properties c in Stream gt Operating dialog we select the stream number 2 a predefined test case Prode Properties Editor Stream Errors Pc 1 Te 1 Pc 2 Te 2 CricoT CricoP No errors Vap Lig Lig 114 514024 124 514024 134 514024 144 514024 154 514024 164 514024 174 514024 184 514024 194 514024 204 514024 208 243595 211 9
54. all setS method to validate the data The following example shows how to define a 2 components stream Call initS Stream Call setMP Stream Fg Call setMP Stream Fg Call putCC Stream 1 Call putZ Stream 2 22 Call putCC Stream 2 Call setS Stream Call setW Stream W Call loadSB Stream 0 0 SRK 2 Call putZ Stream 1 21 see the paragraph setOp setOp setW putCC putZ setMP putCi putCj putBIP Codes used in Prode library define the models for all required properties and states validates stream flow load VLE BIPS from database 94 How to save and restore streams to from a file Archives are files which contain a copy of all compositions operating conditions units of measurement settings etc archives are useful for creating copies of your work otherways all data will be lost when leaving the application The library includes methods to load and save archives see the paragraph Methods to load save archives for the list Call AOpen open a file as archive browse for file Call AFOpen e def ppp open the specified file as archive Call ASave save a file as archive browse for file Call AFSave e def ppp save the specified file as archive 95 Error messages PROPERTIES may generate the following error messages For some of these an action is suggested Memory allocation error A limit in resources allo
55. am int phase given a stream and position in range 1 getPNr returns a ANSI C string with the description of type for detected phase VARIANT description MSirPts integer stream int phase given a stream and position in range 1 getPNr returns a string with the description of type of detected phase this is the Microsoft specific method double If StrLf integer stream given a stream returns the total liquid fraction molar basis in stream double pf StrPf integer stream integer phase given a stream and phase position in range 1 getPNr returns the phase fraction double w getW integer stream integer phase integer pos given a stream the phase position and component s position in component s list returns the component molar fraction in that phase double Zi getZ integer stream integer pos given a stream and component s position in component s list returns the comp s Z weight percentage molar basis integer res putZ integer stream integer pos double Zi given a stream comp s position and Z sets the comp s pos in Z vector composition molar basis for that stream integer nr getCNr integer stream given a stream returns the number of components defined in that stream integer nr getMCNr returns the maximum number of components in a stream double zv SirZv integer stream given a stream returns the relevant compressibility factor gas phase double mw StrMw integer stream given a
56. ange the temperature to 190 1 K we get different equilibrium pressures u u ua a oa Ay JA Ye Rispor B39 M fe 190 1 A l Bej c D E 37 38 39 It 130 11 40 P 1471532 33 Pa 41 P Q2 3682257 87 Pa 42 P 4373312 53 Pa AB cl 45 you may wish to test the method LfTF enter the macro LfTF 3 B39 0 where 3 is the stream B39 represents the temperature and 0 is the liquid phase fraction notice that you ll get the same values as for the first equilibrium point in PfTF Finally we can calculate the point on bubble line with the method LfTF LfTF 3 B39 1 where 1 is the specification 100 liquid for a point on the bubble line of course you get the same result with the method PfTF 3 B39 1 1 1 where the third value 1 is the phase fraction with 1 we specify a 100 fraction the fourth 1 is the state in Properties 0 gas 1 liquid 2 solid and the last is the required position for the point 22 Prode Properties includes several methods for solving multiphase vapor liquid solid phase equilibria plus enthalpy entropy or volume specifications specified enthalpy or entropy or volume and pressure specified enthalpy or entropy or volume and temperature constant energy and pressure the paragraph Methods for thermodynamic calc s provides additional information in this example we will examine the methods HPF and SPF which permit to solve the enthalpy HPF or entropy SPF and pre
57. ar a and 232 08 K In first dialog select the HP VL flash operation on second grid then set 89 Bar a and 246 K as inlet conditions 79 12 Bar a as outlet condition and 71 9 KW 61864 3 Kcal h as heat duty the negative sign means that energy is subtracted Please note that you must specify the value of energy to add or subtract to the total value of stream determined as specific enthalpy mass flow the mass flow in this case has been specified as 1 0 Kg s see the second row Prode Properties Editor x El Stream Operating Select edit stream 1 Test Case 1 F Test Case 1 Save Components z gt an operating contorns z3215 K rs120 maa O BIPs Config chen Fees and Operator 1 Test Case BIPs ra Models Licence maram nosso Joanie Jo pe Cn T S a C C e idoasrrsy foi C C e foresees foi Click on Compute buttom to solve the problem the procedure calculates an outlet temperature see the second row of 232 1 K which is close to the critical point giving a idea of reliability of procedure 24 As alternative to utilize Properties Editor you can solve the problem directly in Excel in cell B5 enter EstrH stream p t to define the initial conditions for stream 1 at 89 Bar a and 246 K and calculate the enthalpy EstrH 1 B2 B1 B4 where 1 is the stream B2 is the operating temperature B1 the operating pressure and B4 represents the additional duty B
58. ases and show the compositions Prode Properties Editor x Select edit stream 1 Test Case 1 x Test Case 1 Se Le e ee Oo Config E Chemicals E BIPs Models ts If you wish you can modify the units from Config gt Units dialog define Bar a as unit for pressure Notice that_when changing units you must close and reopen the editor to see the changes in editor The results are available directly in Excel set stream as 2 temperature as 187 K and pressure as 4154420 Pa a 40 atm g the nclick on Compute isothermal Flash at p t c D E G G H i J a A EN Stream 2 Temperature K 1 from Properties menu select the editor and define composition models options for stream 1 3 Pressure Paa remember to properly set the multiphase options when multiphase is required 4 Errors No errors 2 specify p t according the units defined in editor then compute the isothermal flash Compute Isathermal Flash at p t EE IE Component Formula 10 METHANE CH4 0 9000 11 n HEXANE C6H14 0 1000 Liquid Liquid Not present Not present Not present 0 9784 10 0000 0 0216 0 0000 0 0000 0 0000 Now you are able to calculate results at different operating conditions 15 Altough a slow process multiphase analysis permits to discover instabilities and formation of new phases examine the isothermal flash at 149 K 10 Bar a with API SRK as model and a mixture of Methane
59. calculated according ideal fluid law Wilson Properties calculated according Wilson GM Wilson 1964 NRTL Properties calculated according NRTL Renon and Prausnitz 1968 UNIQUAC Properties calculated according UNIQUAC Abrams and Prausnitz AICHE J 1975 UNIFAC Liquid activity coefficient calculated according UNIFAC Fredeslund Jones Prausnitz AICHE J 1975 Soave Redlich Kwong Different variants of Soave Redlich Kwong model Giorgio Soave 1972 are available base version includes standard and extended version of Soave Redlich Kwong model extended version includes for each fluid 5 parameters calculated to fit the set of experimental data saturation pressures densities latent heats available in DIPPR or DECHEMA pure fluid data collections PR Peng Robinson Different variants of Peng Robinson model D Y Peng D B Robinson 1976 are available base version includes standard and extended version of Peng Robinson model extended version includes for each fluid 5 parameters calculated to fit the set of experimental data saturation pressures densities latent heats available in DIPPR or DECHEMA pure fluid data collections BWRS Benedict Webb Rubin Starling Properties calculated according Benedict Webb Rubin Starling Han 1972 LKP Lee Kesler Plocker Properties calculated according Lee Kesler Plocker 1978 AGA ISO 20765 Gas volume calculated according AGA report ISO 20765 GERG ISO 18453 Fugacity calc
60. cation close applications release memory and restart Corrupted file error reading data file PROPERTIES cannot access a file this may depend from the file not being in the proper directory or being corrupted it is suggested that You reinstall PROPERTIES Internal error This error may depend from several different conditions the most common is a wrong parameter in a function i e an attempt to pass a value out of permitted range Check Your code too many local variables too many variables a limit in resources allocation see above calc on undefined stream data an undefined stream found while executing calc s edit and define the stream undefined stream s operating conditions pressure temperature or flow are undefined edit and define the stream error calling thermo calc procedure wrong input value calcs cannot converge or calcs outside temperature range check chemical s file for limits in temperature correlation s cannot converge calc s loop A wrong convergence condition has been specified i e in an adiabatic flash calcs a thermal condition that cannot be reached by varying temperature pressure or liquid fraction a parameter is outside range limits etc T P values outside H S range calcs Awrong condition has been specified and a parameter in enthalpy entropy calcs is outside range limits too many comp s ina stream when two or more streams are mixed the total nr of components may exceed the max
61. composition note derivatives vs composition as matrix n m integer res SirFvdv integer process integer state double t double p double w double fg double dfgt double dfgp double dfgw Given a predefined stream the required state vapor liquid solid and operating conditions returns the vector of fugacities Pa and related derivatives vs temperature K pressure Pa composition note derivatives vs composition as vector n m integer res StrHv integer process integer state double t double p double w double H Given a predefined stream the required state vapor liquid solid and operating conditions returns the molar enthalpy Kj Kmol integer res StrHvd integer process integer state double t double p double w double H double dHt double dHp double dHw Given a predefined stream the required state vapor liquid solid and operating conditions returns the molar enthalpy Kj Kmol and related derivatives vs temperature pressure composition integer res StrSv integer process integer state double t double p double w double S Given a predefined stream the required state vapor liquid solid and operating conditions returns the molar entropy Kj Kmol k integer res StrSvd integer process integer state double t double p double w double S double dSt double dSp double dSw Given a predefined stream the required state vapor liquid solid and operating conditions returns
62. d try d yeexp arhtecin t da 3 yrarbtect 2eg t Seet 4 2 __l yeat t trYbecttredtr 2 e tr 3 yrarb cAlsin ct 2 a eAicos et 2 Regress raw data e in Chemicals Data page select a chemical e in Chemical Regress page selet a property and the correlation for fitting raw data e enter the available data all temperature and value pairs with the proper units of measurement e if required you may enter initializing values and limits for calculated parameters e click on Calculate button evaluate calculated values and errors you may try different correlations for best data fitting e click on Transfer button to copy calculated values into Chemicals Data page e in Chemicals Data page select the Save button to save the data differently new data will be discharged IMPORTANT Prode Properties flexible datoase format supports more than 15 different correlations 30 in extended version so for each property you can select the correlation which best fits experimental data 55 Binary Interaction Parameters BIP From these pages you can e edit Binary Interaction Parameters add remove Binary Interaction Parameters regress VLE vapor liquid LLE liquid liquid SLE solid liquid data points save all data in a file Prode Properties Editor Edit modify data e select two components from the component s lists e edit modify BIPs for the different models e select the Save butto
63. d returns the number of different units of measurement available for that quantity VARIANT str MgetUMS integer UM integer sel given two integers the first identifies a quantity and the second the selection method returns a string identifying the selected UM this is the Microsoft specific method char str getUMS integer UM integer sel given two integers the first identifies a quantity and the second the selection method returns as ANSI C type the string identifying the selected UM VARIANT str MgetSUMS integer UM given a integer UM for quantity this method returns a string identifying the selected UM this is the Microsoft specific method char str getSUMS integer UM given a integer UM for quantity this method returns as ANSI C type the string identifying the selected UM double res UMCR double value integer UM integer SEL given a value the code for quantity and selection converts to reference and returns the result double res UMCS double value integer UM integer SEL given a value the code for quantity and selection converts from reference and returns the result integer res UMAU double a double b char name integer UM given the code for a quantity the parameters a b required for conversion and the name adds a new user defined temporary unit integer res UMRAU integer UM given the code for a quantity removes all additional temporary units Pao Co aE aoo ty double p getPatm returns
64. e command gt gt phaseenvelope 1 Matlab will invoke Prode Properties to calculate the phase envelope for the stream 1 then it plots the result File Edit Debug Desktop Window Help File Edit View Insert Tools Desktop Window Help x ie phaseenve lope 1 0ga 8 N IS AMD 2 Pa Ta BJE a g B gt gt x10 T P Phase Diagram on T T Pressure Pa a fo 120 140 160 180 200 220 240 Temperature K Notice that from Properties menu bar you can access Properties editor and modify the list of components or models of each stream Fie Edit Debug Desktop Window Help Fie Edt view Insert Tools Desktop Window Help Properties ey h gt gt phaseenvelope 1 Ocad As aoe a0 x gt gt ae 10 T P Phase Diagram E Stream Select edit stream 1 Test Case 1 Test Case 1 Save l Components a 5 Operating Conditions Models H a BIPs E Config Hl Chemicals Feed and Operation 1 Test Case 1 T P VL BIPs Tae Licence Specifications 28815 K 101327 Specifications OUT Paa kW Not present Not present 41 Access from MATHCAD The files and the instructions required to link MathCad with Prode Properties are located in directory Prode MathCad The MathCad support files and the documentation have been provided by Dr Harvey Hensley Getting started with Microsof
65. e diagram and returns the number of equilibrium lines available integer Inr PELT integer stream integer line Given a stream and the line returns the line type see below 1 bubble line 2 dew line 3 three phase line integer Inr PELP integer stream integer line Given a stream and the line returns the line property see below 1 vapor liquid 2 vapor liquid liquid 3 vapor solid 4 liquid solid integer nrpt PELine integer stream integer line double P double T int maxpt Given a stream the line and two arrays 0 maxpt elements the procedure returns nrpt lt maxpt equilibrium points in specified line integer nrpt PVLine integer stream integer line double P double T double H double S double V int maxpt Given a stream the line and five arrays 0 maxpt elements the procedure returns nrpt lt maxpt equilibrium points in specified line in additions to t p values this method returns enthalpy entropy and volume values calculated at equilibrium points this method allows to calculate a line with specified phase fraction in specified state gas liquid solid integer nrpt PFLine integer stream int line double pf double P double T int maxpt Given a stream the line a specified phase fraction and two arrays 0 maxpt elements the procedure returns nrpt lt maxpt equilibrium points in specified phase fraction line 81 Methods for direct access to properties F H S V and derivatives T
66. e pressure with putP set conditions as valid with setValidSop integer result rstValidSop integer stream Given a stream clears the compostions of different phases at operating conditions integer result setValidSop integer stream Given a stream sets the compostions of different phases at operating conditions as valid integer result setValidPhase integer stream integer phase Given a stream and phase sets the phase compostion as valid integer result putW integer stream integer phase int compnr double w Given a stream phase component number and component s molar fraction in that phase stores the value integer result putPF integer stream integer phase double fraction Given a stream phase and phase fraction stores the phase fraction value integer result putPT integer stream integer phase int type Given a stream phase and phase type vapor liquid solid stores the phase type nteger result putT integer stream double t Given a stream and operating temperature stores the value nteger result putP integer stream double p Given a stream and operating pressure stores the value Copy of streams to make a copy of a stream utilize the method integer res StrCopy integer stream1 integer stream2 Given two streams stream1 and stream2 copies the stream 2 into stream 1 75 Methods for solving staged columns Note this method utilizes the standard ANSI C convention for exchanging parameters see
67. e v double et double ep Given a stream the required final entropy see the method StrS for the definition the required specific volume see the method StrV for the definition and estimated values for final temperature and pressure or 0 for automatic estimate method solves the flash operation integer result HSF integer stream double h double s double et double ep Given a stream the required final enthalpy see the method StrH for the definition the required final entropy see the method StrS for the definition and estimated values for final temperature and pressure or 0 for automatic estimate method solves the flash operation double t EPF integer stream double p double E double aout double et Given a stream final pressure outlet area the term E equal to Hin 1 2Vin 2 and a estimated value for final temperaure or 0 for automatic estimate method solves the constant energy flash and returns final temperature Hin 1 2Vin 2 Ho 1 2Vo 2 this method permits to model adiabatic irreversible expansions when the contribute of kinetic energy cannot be neglected integer result MixF integer stream1 integer stream2 double et Given two streams stream1 and stream2 and a estimated value for final temperature or 0 for automatic estimate method solves a mixer operation and returns the result on stream1 the feed streams are adiabatically flashed to the lowest inlet stream pressure integer result Div
68. eaeeeaeecaeeeacessaeeeaeeseaessaeeseaeseaeseaeeseaeeeaeessaeeseeseaeessaeeeaeeeaees 65 Unis ot measurement scredecs fos eec ees ace tel leaden E ea Sea eA DS eR Se 66 Introducing Prode Properties library MethOdS 0 0 0 eeceeeeeneeeeeeneeeeneee eee eeeteaaeeeeaeeeeeaeeeeeeeeeseeeeeseaeeeseaeeeseeeeescaeesseeeeseneeeeeneeeeeas 67 Methods for thermodynamical Sessies oa aa a ebia sade a laaa dialed aie Kaai aE a ia 67 Methods tor stream S data ACCESS risisco naa a aaa NE E Aa Aaaa EA aE EAE EE E Ea E aa aaa aa 69 Methods Torsiream S definitioner iesist ne a a E tle ata ere eed 73 Methods to define stream s Operating conditions 0 0 ee eee ee eeeeeeeeeeeeeeeeeeeeaaeeeeeeeeeseaeeeeeaaeeeeaaeeeseaaeeeeaaeeseaeeeessaeeeeeaeeeeeeneeeseeeess 75 GO YOR SINS AINNS ccs can Seca tener oats cch teres EE AE S O E OE N EE 75 Methods tor solving Staged COMMS sis ccsssciviseses scvts cdsieacsedecevsaca wash adevas stone atten terea daoa Ee ANa Aea desea EROA ENO r aa NTE EAEE ete 76 MethOdS TOF REACTORS esanaren a N E coe Bee eee ees 78 Methods Tor fluid flow problems iiss aiias ea a tansenedscceceaelageiedendudeateterelascacheaiesseasdessinieniensceateesdivess 79 Methods Tor Hydrates phase equilibria ca e cccapcediscecasceecassennshg tes 2eebndeqdeetesuee Cashes ea a ea aaa aa Oha edad oaea 79 Methods for solving a Polytropic Operation 2 ccceccccseeceeeeeneeeseeeeeeeeeeeenneeenseneeseaenensaeemenseeeeseseneeseesenenenesesceeneseesensneneneseeeees
69. eam Methods to load save archives Archives are files which contain a copy of the data used by Prode Properties to manage stream s and units of measurement when you open an archive the stream s data and units are loaded when you choose to save an archive these data are stored in a file Archives are useful to create copies of your work otherways all data will be lost when leaving the application Prode Properties includes methods for operations on archives integer res AOpen open a file as archive browse for file integer res AFOpen char path open the file specified in path as archive integer res ASave save a file as archive browse for file integer res AFSave char path save the file specified in path as archive Methods for accessing defining the units of measurement Prode Properties includes methods for accessing and defining the units of measurement these methods utilize a numeric code for identifying the correspondent quantities refer to the paragraph Access via software to the units of measurement for a list of these codes integer res getUMC integer UM given a integer that identifies a quantity method returns the selected UM for that quantity integer res setUMC integer UM integer sel given two integers the first identifies a quantity and the second the selection method selects a UM for that quantity integer res getUMN integer UM given a integer that identifies a quantity metho
70. ed that User doesn t remove or alter any part of the software or of the licensing codes and threat the software as a whole unit You cannot decompile disassemble or reverse engineer the files containing the licensed software or any backup copy in whole or in part You cannot rent lease or sublicense the Licensed Software without express agreement by Prode The software is provided as is where is Prode does not warrant that software is free from defects or that any technical or support services provided by Prode will correct any defects which might exist Prode shall not be liable for any damages that may result directly or indirectly from the use of these software programs including any loss of profits loss of revenues loss of data or any incidental or consequential damages that may arise out of use of these software Your license is effective upon your acceptance of this agreement and installing the Licensed Software e This license agreement shall remain in effect until the Licensed Software will be in use e You may terminate it at any time by destroying the Licensed Software together with all copies It will also terminate if you fail to comply with any term or condition of this Agreement You agree upon such termination to destroy all copies of the Licensed Software in any form in your possession or under your control Customer support Prode will provide the licensee with limited technical support by teleph
71. edure models a relief valve at specified operating conditions and returns the calculated area models available 1 HEM Homogeneous Equilibrium Solution of Mass Flux integral 2 HNE Homogeneous Non equilibrium HEM with Boling Delay and Gas Liquid Slip Contributes 3 HNE DS Homogeneous Non equilibrium 4 NHNE Non homogeneous Non equilibrium model recommended range of values for correction parameter HEM not required HNE 0 7 0 8 for safety valves HNE DS see the paper NHNE 0 7 0 8 for safety valves additional models available from Prode 80 Methods for calculating equilibrium lines in phase diagrams Note these methods utilize the standard ANSI C convention for exchanging parameters the distribution includes samples to show how to utilize these methods in different languages Prode Properties includes methods for calculating different types of phase diagrams vapor liquid vapor liquid liquid vapor liquid solid feature available in extended versions typical application E define the stream set the required phase equilibria vapor liquid vapor liquid liquid vapor liquid solid E call PELnr to calculate the phase diagram and obtain the number of lines available E on each line call PELP PELT PELine to obtain the data for the different lines E if required call PFLine to calculate a line with specified phase fraction ad state integer Inr PELnr integer stream Given a stream calculates the phas
72. eeeeeeeeeeeeeeeeeeeeeeeeeesecaeeeeeeseaaeeeeeeseqeaeeeeeseenieeeeeeeeees 45 Properties editor Stream operating Predefined Flash Operations sivi pai tngns ies eee eee ae Heide este Fg Snatch ieee eee 47 Stieam Compos spiras earar ae E e tae ase debes cde di Easton E E E a oe Meaglieca sat us epegeta laces cd ducdiesela a E 48 oiean Models irae Perret a S crecener E E a a creer teers errr 49 BUNS E E E E E T E A A E T leaded iba dadigeeeatisieaet Sins 50 COMI WAS eseserari aea a e edie th a eee 51 CONN S EWINA S enren a eaea e a a a aa a meee creer 52 Ghemicals dala mersa r A E EEA e E ESE ES 53 EEAS e E E E E A E N E E E EE A E Galt 54 Regress taw datanomin eaa E E A a cg A 55 Binary Interaction Parameters BIP cccc ssissaseechsissehedsesecisssessascccepedescvasaeeedaicnantalgcnsesccensicceecucs eadauaecetarslascccerajesiehadcandeusuaresesaceeacteats 56 Regress VEE LWUE SME Gates asmi iino aie aeea ia ae a aee Ea Eaa a E EEr aao eDi EaR E a a EEEa iT 57 Parameters Of models sisisi E E A Eaa p E AEEA AE SE T EANNA 63 Accessing Prode Properties library giire dats ie ei R i ve E ee es 64 Translate resources to different languages eeeeeeeeeseeeseeeeeeeeteeeeaeeeseeseaeesaeessaeeeseessaeesseesaeseaeessaeeeaeessaeseaeesseeseaeesieeseaeeteaeeeaeene 65 MicrOSOIPAp plications and SMN Eses esae a AE EEEN SAE EAE Ea E Ceadeans2ee acct eatepestepancatitceaeea ets 65 Define models compatibility With Old VEriONS 02 eeeeeeceeseeeeneeteeeeeeeet
73. eeeeeeeeeeeeeteeeeteeeeeeeeeneeeeaeeseeetenees 101 Oe E vad ies E E A E T 102 UNIFAG functional Groups 3 2ciertesccett deere scedhes asein nieve dae NE O o e ene A ieee 103 License agreement Agreement made between Prode Prode and User Prode is the owner of the product Prode Properties including but not limited to dynamic link libraries static libraries header files sample programs utility programs together with the accompanying documentation collectively known as the software User desires to obtain the right to utilize the software the parties hereby agree as follows Personal license A version with limited features is available for personal use at home or in educational establishments for teaching purposes all other applications without first obtaining a commercial license from Prode are expressly prohibited Commercial license Upon full payment of the license fee the User has full right to utilize the purchased number of units of the software a unit is defined as one copy of the software or any portion thereof installed on one stand alone computer for networked computers one unit shall be applied for each user having concurrent access and one unit shall be applied for the server For all applications e Prode grants the nonexclusive nontransferable right to use the software User has a royalty free right to reproduce and distribute the software as available from Prode Internet server personal licence provid
74. eesenes 79 Methods tor relief valves design s rating erosie inina a ad ine a a N E a eens 80 Methods for calculating equilibrium lines in phase diagrams cceeceeeeeeeeeeeneeeeeeeeeeeceeeeeeeeceeeeseeeeaeeseeseeseeeeeeeseaeeeneeseeeeeeeeeaes 81 Methods for direct access to properties F H S V and derivatives T P W ccecceseeeeeeeeeeeseneeeeeeeeeeeseeseaeeseeeseeseaeeeneeteeeeeeeeaes 82 Extended methods for accessing Stream s properties eeececeeeneeeeeeeeeeeeeeeeeeeeeeeeeeeeeaeeseaeeeaeesaeeeeesneeseaeeseeeseaeesieeseeesieeseaeeeneees 83 Methods tor chemicals tile access i scsccidstitise aneele ets dinette de ep ee ea 85 Methods to set access different options eccescsesceseeeceecesseeeeaeessaeeeaeeeseeeeaeesaeeeaeecaeeeaeesaeesaeesacesaeesseeeaeesaeeseaeeeaeeeaeeeeneteaes 87 GOdes used in Prode brary ss eset eds casts E E EE blade Gi eodeasitssheaict E AEA T S 87 Methods to define thermodynamic Models siinse aa aa RE AAE AEE EEEa AAEE SaaS na 89 Methods to define base values for Enthalpy and Entropy viisistusi atadian kaitai 89 Methods to set ACCESS streams MAIMES ececccceseeeteeeeeeseeeenesenen sa eeeeesseeeneeneneaaeeeesaesesesenenseseeenseasensenseseseeeeeseesensnsensenenessesens 90 Methods to access Model s data ic toss scccecetsceaseceseancact sere cagae scnnsctpavactgp vena e E ERE Eaa Ee Ea 90 Methods to control errors MOSSAGES sc sc cescccnsenccedseedeeccccetasditene suse ianiai irai iea Ni
75. emperature Operating Specific Volume EStrV 1 B2 B1 Im3 Kg Discharging Pressure 7800000 Pa a Calculated Outlet Temperature 248 9628834 K Ga NE to calculate the Outlet temperature for the isochoric process in celll B5 we enter VPF 1 B4 B3 0 where 1 is the stream B4 is the final pressure B3 the required specific volume equal to inlet volume and 0 0 the estimated final temperature the value 0 0 means we require the automatic initialization SOMMA y X v amp VPF 1 B4 B3 0 A eS Operating Pressure 6000000 Pa a OperatingTemperature 225K Operating Specific Volume 0 006222516 m3 Kg Discharging Pressure 7800000 Pa a Calculated Outlet Temperature VPF 1 B4 B3 0 On Wiha a IMPORTANT due to the calling mechanism of Microsoft Excel in some cases Prode Properties may return a 0 0 value even when a solution is available in those cases you can get the correct results by forcing the cell recalc with the Enter key 28 In next example we estimate the discharge temperature and the power absorbed by a single stage compressor with determined adiabatic efficiency the theoretical power requirements can be calculated as enthalpy at outlet conditions enthalpy at inlet conditions mechanical efficiency The outlet temperature is calculated with four steps a model the compressor as isentropic process and calculate the final temperature b calculate the final enthalpy for the isentropic process c calculate
76. er defined list string 40 chars max Identification number CAS as default Molecular weight Critical temperature Critical pressure Critical volume Acentric factor Dipole Moment Radius of Gyration Solubility parameter Standard enthalpy of formation 298 K Gibbs free energy of formation 298 K 1 atm Normal boiling point Enthalpy of fusion Melting point Flammability lean limit range 0 100 Flammability rich limit range 0 100 Autoignition temperature Net heat of combustion Gas heat capacity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Vapor viscosity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Vapor thermal conductivity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Heat of vaporization correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters 98 Liquid vapor pressure correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Surface tension type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameter
77. eral types of licence e software copy protection distribution via email installation on a single computer identified by an installation code e hardware dongle copy protection we ship the dongle installation on single or multiple computers e network installation Order a software copy protection licence the licence file is based on the installation code which the program generates automatically Run an applications which does access Prode PROPERTIES once in the Properties editor the licence page will show the installation code ID see below it s the string IGSGH2 e when placing the order specify the installation code a Stream Operating Components Models BIPs Config Chemicals BIPs Licence User Prode Properties with limited database and features for personal use at home or in educational establishments for teaching purposes all other applications without first obtaining a commercial license from Prode are expressly prohibited GSGH2 Order a hardware copy protection licence There are versions for stand alone computer and network connected computers please contact Prode for details 7 Prode Properties Quick Start With Prode Properties you can solve complex problems with only minor programming effort Much of the functionality is provided by the library In this chapter you will learn step by step how to access Properties from your favourite application This chapter is for those of you that wa
78. eratures and estimated errors see the paragraph Binary Interaction Parameters BIP for details Consider data regression from measured data the recommended option for the details see the paragraph Regress VLE LLE SLE data for this example select Hydrate BIPs as Data Set and click on Get BIPs from Database button to load the values Prode Properties Editor xj Hydrate BIPs Get BIPs from database BIP 2 BIP 7 1 2 9 99966 9 88622 0 132157 0 0984578 9 98532 8 4843 0 0885419 1 3 0 0 0 0 10 8 95037 0 148292 1 4 4 69217 4 07074 0 100458 0 107384 0 0145097 0 0101197 7 22766 2 3 0 0 0 0 0 00221651 4 87661e 005 10 2 4 7 81091 8 34428 0 126252 0 0236688 0 467694 0 935554 0 379489 3 4 0 0 0 0 3 62764 10 0 0933972 then back to Operating tab and click on Save button to store the values in Prode Properties once saved you can calculate hydrate phase equilibria immediately selecting the TP VLSH flash operation setting temperature 277 K and Pressure 15 Bar a click on Compute button to see the results at specified condotions the model indicates that hydrates can form Prode Properties Editor x Stream Operating Select edit stream 6 Test Hydrate gt Test Hydrate Operating Conditions 277 kK iitseoos ee tis BIPs Config Chemicals BIPs Models Licence 6 Te
79. ethod returns as ANSI C type the string identifying that stream integer res putN integer stream char str given a integer that identifies a stream and a ANSI C string identifying that stream this method sets the label Methods to access Model s data Prode Properties includes models for calculating properties as fugacities enthalpies entropies volumes viscosities etc these methods allow to access the models available integer nr getMDnr returns the number of models available in this version char str getMDN int model given the model position in the range 1 number of models available method returns as ANSI C type the string identifying that model integer res getMDP int model int prop int state given the model position in the range 1 number of models available the required property and state returns TRUE if model can calculate the specified property otherwise returns FALSE integer code getMDC int model given the model position in the range 1 number of models available returns the code of the model Methods to control error s messages PROPERTIES includes a set of functions to control the error messages By default PROPERTIES produces an error message via a Microsoft Windows Dialog Box every time an error is discovered This approach can slow down the process when a long sequence of errors occurs in an extended calculation sequence such as an iterative convergence calculation A better solution in that si
80. ethyl amine 33 CHNH Diisopropylamine 34 C 3N CH3N Trimethylamine 35 CH2N Triethylamine 36 ACNH2 ACNH2 Aniline 37 Pyridine C5H5N Pyridine 38 C5H4N 2 Methyl pyridine 39 C5H3N 2 3 Dimethylpyridine 40 CCN CH3CN Acetonitrile 41 CH2CN Propionitrile 42 COOH COOH Acetic acid 43 HCOOH Formic acid 44 CCl CH2Cl Butane 1 chloro 45 CHCI Propane 2 chloro 46 CCI 2 Methylpropane 2 chloro 47 CCl2 CH2Cl2 Methane dichloro 48 CHCI2 Ethane 1 1 dichloro 49 CCl2 Propane 2 2 dichloro 50 CCI3 CHCI3 Chloroform 51 CCI3 Ethane 1 1 1 trichloro 52 CCl4 CCl4 Methane tetrachloro 53 ACCI ACCI Benzene chloro 54 CNO2 CH3NO2 NitroMethane 55 CH2NO2 Propane 1 nitro 56 CHNO2 Propane 2 nitro 103 Code Main ACNO2 CS2 CH3SH Furfural DOH Br C C DMSO ACRY CICC ACF DMF CF2 COO SiH2 SiO NMP CCIF CON OCCOH CH2S Morpholine Thiophene Subgroup ACNO2 CS2 CH3SH CH2SH Furfural DOH l Br CH C C C DMSO Acrylnitril Cl C C ACF DMF 1 DMF 2 CF3 CF2 CF COO SiH3 SiH2 SiH Si SiH2O SiHO SiO NMP CCI3F CCI2F HCCI2F HCCIF CCIF2 HCCIF2 CCIF3 CCI2F2 CONH2 CONHCH3 CONHCH2 CON CH3 2 CONCH3CH2 CON CH2 2 C2H502 C2H402 CH3S CH2S CHS MORPH Example Benzene nitro Carbon Disulfide Methanethiol Ethanethiol Furfural 1 2 Ethanediol lodoethane Bromoethane Hexyne 1 Hexyne 2 Dimethylsulfoxide Acrylnitrile Ethene trichloro Hexafluorobenzene N N Dimethylformamide N N Diethylfo
81. ey returns the first point along the specified liquid fraction line at the specified pressure or temperature Methods PfPF and PfTF can accept a gas or liquid fraction solid fractions in extended edition as specification they can calculate up to 5 points at specified pressure or temperature along the line with specified phase fraction double p PfTF integer stream double t double pf int state int n which requires the stream the equilibrium temperature the phase fraction range 0 1 the state gas liquid solid and the position 1 5 of the equilibrium point In cell B39 we define the temperature as 190 208 K then in cells B40 B41 B42 we enter the macros PfTF 3 B39 0 1 1 in cell B40 PfTF 3 B39 0 1 2 in cell B41 PfTF 3 B39 0 1 3 in cell B42 where the first value 3 is the stream the second cell B39 represents the temperature the third 1 is the phase fraction with 1 we specify 100 gas or a point on dew line the same would be by setting the state as liquid and phase fraction as 0 0 the fourth 0 is the state in Properties O gas 1 liquid 2 solid and the last is the required position we require the points 1 3 along the dew line D a d a oe oo l Risp somma X v f amp PfTF 3 839 0 1 1 A BT c D 3 39 t 190 208 40 Pay 339 0 1 1 _ IPa 41 P 2 3651193 24 Pa 42 P 3 4397597 78 Pa 43 44 45 the procedure calculates the three equilibrium points if we ch
82. given a stream returns the calculated liquid thermal conductivity at operating conditions double tc StrGC integer stream given a stream returns the calculated gas thermal conductivity at operating conditions double v StrLV integer stream given a stream returns the calculated liquid viscosity at operating conditions double v StrGV stream given a stream returns thecalculated gas viscosity at operating conditions double st StrST integer stream given a stream returns the calculated surface tension at operating conditions Integer cpnr StrCPnr integer stream given a stream returns the number of critical points detected and calculated to get a critical point use the methods StrPc and StrTc setting value of pos in the range 1 cpnr double p StrPc integer stream Integer pos given a stream and the critical point position in the list see method StrCPnr returns the critical pressure double t StrTc integer stream Integer pos given a stream and the critical point position in the list see method StrCPnr returns the critical temperature 71 double p StrCBp integer stream given a stream returns the cricodenBar pressure double t StrCBt integer stream given a stream returns the cricodenBar temperature double p StrCTp integer stream given a stream returns the cricodenTherm pressure double t StrCTt integer stream given a stream returns the cricodenTherm temperature double ac StrAc
83. hase double jt EStrLJT integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the Joule Thomson coefficient for liquid phase double ic EStrGIC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the isothermal compressibility coefficient 1 V dV dP in gas phase double ic ESirLIC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the isothermal compressibility coefficient 1 V dV dP in liquid phase double v EStrGVE integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the volumetric expansivity coefficient 1 V dV dT in gas phase double v ESirLVE integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the volumetric expansivity coefficient 1 V dV dT in liquid phase double hc EStrHC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the net heat of combustion gas phase double fl EStrFML integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the flammability lean limit gas phase double fl EStrFMH integer stream double t double p given the
84. have been disabled Macros might contan viruses or other secsity hazards Do not enable the content unless you trust the source of the fie 83 CG 50 e Warning It is not possible to determine that this content came from a A a Cc E trustworthy source You should leave this content disabled unless the content provides critical functionality and you trust its source t SIMPLE STAGED COLUMN SIMULATIO Mace nformeben 2 Patu C z _ 3 Number of stages File Patt C Program Files Prode Exce cotumn ats 4 Top stage pressure 6 Bottom stage pressure 6 Stage efficiency 7 Number of feeds 8 Feed stage 9 Feeding liquid faction 10 Feeding temperature 11 12 Number of Side Streams 13 Side stream stage 14 Side stream state 15 Side stream fow ratio to teed 16 O Hep protect me fom unosan content recommended Enable ts content To fix the Security Warning click the Options button and select Enable this content in Security Alert dialog 10 IMPORTANT before to evaluate the sample files read the paragraph Working with archives save and load data default settings while working in Microsoft Excel use the commands Open Archive and Save a Archive to save and restore data IMPORTANT the values indicated in this manual as results of some operations can be different when calculated with software due to the different values of chemical s properties and BIP s stored in different versions of the software
85. he simulation block diagram When there are no recycle streams or controls the method for solving the system is very simple the output information from the first operating block is utilized as input for the second operating block and so on However when there are output conditions which may interfere with input conditions some sort of iteration is required since some or all the equations governing the system may be non linear There are two well known methods for solving such a system of non linear equations the method of successive substitutions and Newton Raphson refer to good books of numerical analysis for additional information Streams Most thermodynamic calcs in Prode Properties library take as reference a stream entity For example when simulating a plant it makes sense to define different streams to represent flows in different sections a stream usually defines compositions and operating conditions Prode Properties supports a variable number of streams and most methods in Prode Properties require a reference to a stream the reference is a numeric code a progressive integer starting from 1 for first stream Streams attributes As in process simulators each stream may include following information e alist of components and relative weights e avalue for the operating pressure e avalue for the operating temperature avalue for the operating flow e thermodynamic models for different properties e alist of BIPs Working with streams
86. he unloadlibrary function to unload Prode Properties library from Matlab and free up memory gt unloadlibrary ppp 39 Access from Matlab through scripts In addition to direct access you can utilize Prode Properties from Matlab with scripts or mex files compiled scripts In many cases this way is more immediate since you use the original names of the functions in Prode Properties without need to write additional code Prode Properties includes a large number of Matlab scripts installed in directory Prode MATLAB m Before to utilize the scripts you must move the files into a Matlab directory i e a directory where Matlab can access the scripts read Matlab documenta tion for additional information edit the file pppdir txt this file contains a string with path and name of the header file required to instruct Matlab about the methods avalialable in Prode Properties library once you have edited move the file on the same location of script files How the scripts work Scripts act as interface between Matlab and Prode Properties scripts have names identical to Prode Properties meth ods then when you invoke the script StrGD which is the method in Prode Properties to calculate density of vapor phase MATLAB simply executes the commands found in the file calls the method StrGD in Prode Properties and returns the result by the way the script StrGD m contains these MATLAB commands function SirGD stream if not libisloaded ppp
87. hods to define a initial condition for a stream nteger res loadSB integer stream integer btype given a stream loads all BIP available in database This method must be called after the stream has been defined since it requires the list of components Codes for btype are 0 for VLE 1 for LLE 2 for SLE 3 for Hydrates double Zi getZ integer stream integer pos given a stream and component s position in component s list returns the comp s Z molar fraction integer cc getCC integer stream integer pos given a stream and component s position in component s list returns the component code a integer that identifies the component in chemical s file integer nr getMBPNr returns the maximum number of interaction coefficients binary pairs in a stream int ci getCi integer stream integer pos given a stream and position in interaction s coeff list returns the first component reference a integer that identifies the component in component s list integer res PutCi integer stream integer pos integer ci given a stream position in interaction coefficients list and first component reference sets the component s reference in interaction coefficient s list int cj getCj integer stream integer pos given a stream and position in interaction s coeff list returns the second component reference an integer that identifies the component in component s list integer res PutCj integer stream integer pos
88. i integer stream1 integer stream2 double wdiv Given two streams stream1 and stream2 and a flowrate fraction 0 1 performs a divider operation so that stream 1 is shifted into two streams stream1 stream2 of the same composition temperature and pressure flowrate fractions are subdivided as specified by wdiv stream2 wdiv stream1 1 wdiv integer result psep integer stream1 integer stream2 integer phase Given a stream stream1 performs an isothermal flash to simulate a phase type vapor liquid solid separator and returns the result as stream2 68 Methods for stream s data access Prode Properties includes a set of functions for accessing stream parameters and calculating transport properties Note that when calculating transport properties the program performs a VLE flash and returns 0 zero value when no associated liquid or gas phase is found integer res isSDef integer stream given a stream returns TRUE integer 1 if stream has been defined otherwise returns FALSE 0 double t getT integer stream given a stream returns stream s operating temperature double p getP integer stream given a stream returns stream s operating pressure integer nr getPNr returns the maximum number of phases that procedure can detect integer type StrPt integer stream int phase given a stream and position in range 1 getPNr returns the phase type vapor liquid solid char description StrPts integer stre
89. ibraries are compatible with almost all Microsoft Windows applications and being compiled code they run very fast They also integrate tightly with your application allowing it to run as an autonomous program unit rather than being dependent on external modules of a different application Prode Properties includes file I O graphical interfaces etc for a total of about 200000 lines of code all the code compiled with last version of Microsoft C compiler resides in a library ppp dll of about 7 Mbytes it s a very compact and efficient code easy to distribute with your application Reference Literature Although Prode Properties may appear easy to utilize also to people without a background in chemical engineering a basic knowledge in this area is useful for selecting the proper methods and critically evaluate the results There are good books available we would suggest some titles e Introduction to Chemical Engineering Thermodynamics Smith Van Ness Abbott McGraw Hill e Chemical and Engineering Thermodynamics Sandler Wiley The Properties of Gases amp Liquids Reid Prausnitz Poling McGraw Hill Release 1 1 1994 First version of Prode Properties author Roberto Paron as part of Prode Calculator a tool distributed since 1994 Release 1 1f 1995 Updated the UNIFAC model included different options for calculating gas fugacity with liquid activity models Release 1 1g 1996 User can define units of measurement via ed
90. ick on Design button to estimate the outlet temperature head and power 19 Pout o Efficiency 0 1 Result No errors eam Flow spec 1 mass flow 2 volumetric flow at inlet condition 22 Flow kg s Ea Method 1 Huntington 3 Polytropic solution with phase equilibria 24 25 26 Tout 226 177 K _27 Head 64 653 kJ kg _28 Power 86 204 k 31 Next example allows to size a relief valve comparing the results of different methods for critical and two phase flow see the paragraph Methods for solving a Isentropic operation for additional information We use a predefined Excel page as interface to Prode Properties From Excel menu File gt open in Excel folder in Prode Properties installation select the file nozzle xls A B e D E F G H l J K L 4 select the most suitable model 1 HEM 2 HNE 3 HNE DS 4 NHNE and the parameter when required 5 the procedure estimates the isentropic nozzle flux and returns the required area 6 Stream i 7 8 Model 1 HEM 2 HNE 3 HNE DS 4 NHNE Model parameter model parameter as defined in operating manual 9 Pin 10 Tin Calculate solution 11 Pout 12 Flow 13 Corrections Ka Kb K Result No errors 14 15 Estimated tout 274 7390 K 16 Calculated area 4 229E 05 m2 17 Required Area 4 699E 05 m2 18 The steps to size a relief valve are easy to follow 1 fr
91. ilable for calc s Prode Properties Editor xj H BIPs cS a No multiphase only two phases Standard tests From Gibbs or Isothermal Compr and Liq Dens Discard unstable solutions End when crossing phase boundary lines Select EOS roots according state 4 4 EERESRBRSRRRBRLB oe cows i _ Define a new package Edit existing package e select a package in the list in Models and Options Window select the models and options for this package e define a name for the package e click on Save button to save this package Select a package e select a predefined package in the list Define a model e specify the model per each property and state Set a option e define multiphase as vapor liquid or vapor liquid solid e reduce the number of trial phases in multiphase e use iso compressibility coeff to detect the state of each phase e evaluate stability of each phase in equilibrium e in phase diagrams end lines with specified phase fractions when crossing a phase boundary e in phase diagrams select EOS root for minimum energy or state 49 From this page you can e input edit load BIPs for the different models Define a list of BIPs e click on Get BIPs for loading all BIPs available in library e if required add your own specific BIPs Prode Properties Editor x eee e em ooo OO O
92. imum some inconsistences in stream s data error accessing component s data archive unavailable data a unspecified component or calc s outside temperature range Stack error no memory reload procedure a limit in resources allocation see above Method not available in this version Attempt to define a method not available in that version edit the stream and define a new method A stream with Steam Tables model must have only 1 component You should specify a stream with one component only in order to apply ASME Steam Tables model 96 Calculation basis The user can specify which method to use selecting the models Please refer to the paragraph reference literature and Models for additional information about the methods Fugacity calculated according selected model Enthalpy calculated according selected model Entropy calculated according selected model Volume calculated according selected model Viscosity gas low pressure mixing rule according Wilke 1950 operating conditions correction according Stiel and Thodos 1964 liquid logarithmic average mixing rule pressure correction according Lucas 1981 Thermal conductivity gas low pressure mixing rule according Mason and Saxena 1958 operating conditions correction according Stiel and Thodos 1964 liquid mixing rule according Li 1976 Surface tension mixing rule according MacLeod Sugden Heat of combustion weight average mixing rule according
93. ire you to adapt your code from the examples shown here The calling convention determines how a program makes a call and where the parameters are passed PROPERTIES does use of standard calls of Windows API it pushes parameters on the stack in reverse order When accessing PROPERTIES You must also consider e Prode Properties real type is 8 bytes e Prode Properties integer type is 4 bytes parameters are passed by value with exception of strings which are arrays of characters IMPORTANT C C support files are located in the directory Prode C FORTRAN support files are located in the directory Prode FORTRAN Microsoft NET support files are located in the directory Prode NET Microsoft EXCEL support files are located in the directory Prode Excel Fortran add ppp lib file to the list of the files in Your project and include ppp f90 to instruct the compiler about the methods available in Prode Properties then access the methods as they were included in your code C this procedure returns the critical temperature of a compound INTERFACE TO REAL 8 FUNCTION TC C ALIAS CompTc comp INTEGER 4 comp VALUE END REAL 8 tc INTEGER 4 id C define the id value here tc TC id include the ppp h header e add ppp lib file to the list of the files in Your project make sure you use the calling convention of ppp h header file access the Prode Properties methods C C char name name CompN 1 returns the name of the fi
94. l s file temperature dependent correlation double tc CompSC integer code double t given the component code and a temperature returns the calculated solid thermal conductivity calculated via Chemicals file temperature dependent correlation 86 Methods to set access different options To set access the different options available in Prode Properties the library includes two methods getOM and setOM these methods accept return a 32 bit integer each bit in the integer represents a different option see below a short list of the most important options available int om getOM integer stream given a stream returns a code integer which defines the settings integer res setOM integer stream integer option given a stream and model code sets the options Codes used in Prode library Table of codes to specify the different options reference methods getOM setOM Caution The codes may change in different _versions Bit Decimal value Option 1 1 set multiphase vapor liquid 2 2 set multiphase vapor liquid solid 3 4 set multiphase vapor liquid solid hydrate 4 8 reduce the number of trial phases in multiphase 5 16 use iso compressibility coeff to detect single phase state 6 32 evaluate stability of each phase in equilibrium 7 64 end specified phase fraction lines when crossing phase boundary lines 8 128 includeall hydrate structures also those not normally generated by forme
95. lectrolyte 100 Steam tables IAPWS 1995 101 GERG ISO 18453 102 GERG 2008 105 AGA ISO 20765 111 COSTALD 112 VTPR 88 Methods to define thermodynamic models To define or retrieve the thermodynamic models associated with a stream the library includes several methods setKM works with predefined packages while setMP getMP allow to define specific models on each property Fg H S V integer res setKM integer stream integer Kcode given a stream and the code for the predefined package contact Prode for the list of predefined packages available in different versions sets the package integer res setMP integer stream integer mp integer model integer state given a stream property Fg H S model and state Vapor Liquid Solid Hydrate this method sets the specified model for that property and returns TRUE in case of success otherwise returns FALSE integer m getMP integer stream integer mp integer state given a stream related property Fg H S and state Vapor Liquid Solid Hydrate this method returns the specified model for that property and state Table of codes to specify the different properties in setMP and getMP reference methods setMP getMP Code Property Fugacity Enthalpy Entropy Volume Viscosity additional properties available in extended versions Methods to define base values for Enthalpy and Entropy The library allows to define the base values the tempe
96. lume V P VLSH equilibrium temperature vapor liquid solid hydrate multiphase at specified pressure and specific volume Copy Stream copy a stream into another stream Gas Separator simulates a gas separation at specified temperature and pressure Liquid Separator simulates a liquid separation at specified temperature and pressure 47 Stream Composition From this page you can e define a list of components by selecting components from the library e specifyi the amount of each component Prode Properties Editor Define the sorting criteria e select the preferred criteria Add a component to the list e select a component from the list of components e click on Add button Remove a component from the list e click on Remove button to remove the last component in the list Clear the list e click on Clear button to rclear all components in the list Enter normalize according Mole or Weight fractions e select the desired Mole or Weight fractions MPORTANT to obtain the maximum accuracy solving multiphase equilibria with solid and hydrate phases it is suggested to regress BIPs from VLE LLE data points models such as CPA PR can calculate accurately fugacities of solid phases with a suitable set of BIPs 48 Stream Models From this page you can e define up to 30 different packages with user defined models and options e define the model per each propertty and state gas liquid solid e set different options ava
97. n to save the modified data differently new data will be discharged IMPORTANT Updating the file which contains the BIPs data this option permits to store all data into a file differently all changes will be lost when leaving the application e select the File button CAUTION you may wish to create a backup of the file bips dat before to overwrite the file 56 Regress VLE LLE SLE data From this page you can e regress VLE LLE SLE data for calculating the best fitting paraneters of different models as first step in BIPSs gt Data page you must select two components in this example methanol and water Prode Properties Editor Bs The procedure permits to enter experimental measured VLE LLE SLE data points or fit automatically the model to VLE points calculated with UNIFAC Prode Properties Editor xi Type Temperature Pressure VIE win n K I Paa Ila n When entering measured VLE vapor liquid data points on each row include in X column the measured liquid molar fraction of component 1 in Y column the measured vapor molar fraction of component 1 for LLE liquid liquid equilibria include in X column the measured liquid molar fraction of component 1 in first liquid phase and in Y column the measured liquid molar fraction of component 1 in second liquid phase for SLE
98. ng conditions double st ESirST integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the calculated surface tension at operating conditions 84 Methods for chemical s file access Prode Properties includes a set of functions for chemical data file access Components are referenced via a component code which is an integer with value in the range 1 to getFCNR Integer nr getFCNr returns the number of components in Chemical s File VARIANT str MCompF integer code given the component code returns the relevant component formula eventually truncated to string maximum lenght this is the Microsoft specific method char str CompF integer code given the component code returns the relevant component formula eventually truncated to string maximum length this is the ANSI C compatible method VARIANT str MCompN integer code given the component code returns the relevant component name eventually truncated to string maximum length this is the Microsoft specific method char str CompN integer code given the component code returns the relevant component name eventually truncated to string maximum length this is the ANSI C compatible method int id CompID integer code given the component code returns component s ID it s the CAS number int cc CompClD integer id given the component ID returns the component s code double mw
99. nt to skip the tutorial and immediately start using Properties In the following sections you will learn how to utilize the samples provided with Properties When you run the samples you will get a broad overview of the possibilities available from using Properties you will notice the following features e The Properties editor permits a simple and quick access and editing of all data including streams units databases e The user can define on each different stream compositions operating conditions BIPs thermodynamic models per property fugacity enthalpy entropy volume e The Properties library solves problems as multiphase equilibrium critical points etc e Specific methods are provided for diagnostic error messages e Results of flash operations transport properties etc can be retrieved easily into your application Locating and testing the sample files As default the sample files including data files project files and other associated files are supplied with the program and placed in subdirectories under Prode main directory MPORTANT The installation procedure creates a directory Prode and different subdirectories Prode C includes definitions and code for C C applications Prode Excel includes samples for Microsoft Excel Prode LIB includes the versions of the library Prode MATLAB includes definitions and code for MATLAB applications Prode MATHCAD includes definitions and code for MATHCAD applications Prode
100. ode and a temperature returns the calculated latent heat calculated via Chemical s file temperature dependent correlation double v CompLvV integer code double t given the component code and a temperature returns the calculated liquid viscosity calculated via Chemical s file temperature dependent correlation double v CompGV integer code double t given the component code and a temperature returns the calculated gas viscosity calculated via Chemical s file temperature dependent correlation double d CompLD integer code double t given the component code and a temperature returns the calculated liquid density calculated via Chemical s file temperature dependent correlation double tc CompLC integer code double t given the component code and a temperature returns the calculated liquid thermal conductivity calculated via Chemical s file temperature dependent correlation double tc CompGC integer code double t given the component code and a temperature returns the calculated gas thermal conductivity calculated via Chemical s file temperature dependent correlation double st CompST integer code double t given the component code and a temperature returns the calculated surface tension calculated via Chemical s file temperature dependent correlation double d CompSD integer code double t given the component code and a temperature returns the calculated solid density calculated via Chemica
101. og before to click Ok and exit Then enter the desired liquid fraction for equilibrium line cell C6 and click on compute button to calculate the data Prode Properties will print the calculated values with the desired units of measurement herebelow an example with 3 components A B D E F G H J K E M 1 VAPOR LIQUID LIQUID PHASE DIAGRAM _2 in Properties editor define for the specified stream the composition models BIPs for mixtures Errors _3 select Multiphase Vapor Liquid Liquid or Vapor Liquid Solid for calculating multiphase diagrams Pc 1 4 Te 1 Stream compute phase diagram Pc 2 a Phase Fract Te 2 ze CricoT _8 100 00 120 00 140 00 160 00 180 00 200 00 22000 240 00 260 00 280 00 CricoP 9 10000000 000000 10 11 Bubble 42 9000000 000000 Vap Liq 43 Pa a 14 8000000 000000 15 112 745203 101327 400000 16 117 745203 147855 686407 Eiz 7090900 900000 122 745203 208736 128360 48 127 745203 286316 427646 449 6000000 000000 132 745203 382936 455994 20 137 745203 500885 439083 aa 5000000 000000 142 745203 642363 487966 22 147 745203 809446 461094 23 152 745203 1004052 903208 24 4000000 000000 157 745203 1227911 344423 E5 162 745203 1482526 284369 26 167 745203 1769140 340315 Ba 3000000 000000 172 745203 2088690 287766 28 177 745203 2441753 406471 29 2000000 000000 182 745203 2828480 213086 30 187 745203 3248508 297117 Bill 192 745203 3700849 226714 3
102. ollection text books e Technical Data Book Petroleum Refining Due to the large differences in critical and transport properties found in different sources DIPPR AICHE Design Institute for Physical PRoperty Data reference has been selected as a default Component s identification Components are identified by name from DIPPR list chemical formula and Identification number Regression procedures and results Coefficients in correlations have been calculated with a custom program that uses a modified version of Levenberg Marquardt algorithm reported errors at each fitting point are usually lower than 1 of input values for the most complex correlations i e vapor pressure however in some cases they may be higher Consistency tests When relations exist between thermodynamic properties i e acentric factor and critical pressure and temperature vapor pressure and heat of vaporization etc a consistency test has been performed Comparing Prode Properties results against those of different process simulators When comparing data from different tools one must verify that e the different tools do use the same thermodynamic models properties in databanks have siimilar values e lists and values of BIPs and other parametres which can influence results have similar values 101 Standard versions include a complete set of thermodynamic models additional models are available in extended versions Regular Properties
103. om Properties editor define the composition models BIPs for mixtures 2 enter the discharging temperature pressure flow model outlet pressure 3 click on button Calculate Solution the procedure calculates the required area and the outlet temperature for critical and two phase flow you may utilize the procedure to verify the results from a different software in applications as fluids in critical area two phases flow etc The same page includes a procedure to compare the results from HEM Homogeneous Equilibrium and different Non Equilibrium models for a specified pressure in a range of inlet vapor qualities Please follow fhese steps to compare two models 1 from Properties editor define the composition models BIPs for mixtures 2 enter the pressure model and parameter 3 click on button Compare Models 19 You can compare the results of HEM model against another model at specified inlet pressure pout set at a fraction of pin to evaluate the critical flow 20 Stream f 21 Model to compare 2 HNE 3 HNE DS 4 NHNE 22 Model parameter 23 Pin Compare models 24 25 26 Compare HEM Homogeneous Equilibrium and Non Equilibrium Models 27 18000 Quality HEM HNE 28 180004 s 0 00025 10413 333 16796 976 29 z 14000 0 00062 10407 7 16772 9 30 12000 4 0 00156 10391 2 16713 2 31 s 100004 e 0 00391 10349 16565 1 32 E
104. ompressor xls A B G D B F G H J K E M N 1 Single polytropic stage design and rating for gas and gas liquid flow INSTRUCTION Esi Stream Rate From Properties editor define the composition for the specified stream 4 Pin in this page enter pressures temperatures flow with proper units and method to ES Tin then click on Rate button to estimate the polytropic efficiency head and power e Pout EA Tout Result Esd Flow spec mass flow 2 volumetric flow at inlet condition Eg Flow 10 Method Huntington 4 Polytropic solution with phase equilibria 11 zy Efficiency 13 Head 14 Power 15 INSTRUCTION 16 Stream Design From Properties editor define the composition for the specified stream ae Pin in this page enter pressures temperature efficiency flow with proper units and m 18 Tin then click on Design button to estimate the outlet temperature head and power e Pout a Efficiency 0 1 Result ei Flow spec 1 mass flow 2 volumetric flow at inlet condition E2 Flow Esi Method 1 1 Huntington 3 Polytropic solution with phase equilibria 24 Ed _26 Tout E Head 28 Power the page contains two sections the first permits to calculate the polytropic efficiency of a single compression stage given the inlet temperature and pressure The second section allows to estimate the discharging temperature given inlet temperatu
105. ondenser and reboiler and the related specifications the procedure allows different specifications including molar fractions and recovery of a component in top or bottom stage Notes In Stream Editor Config gt Units you can define all the units for this project in Stream Editor Config gt Setti gs you can define mass units or molar units for flows in Stream Editor 33 Once the column has been defined it is suggested to verify the input data for inconsistent specifications if you are sure that all is Ok run the solver button Solve Column Solve Colurnn Results a numerical solution was found please verify the results Error mass and energy balance 8 342E 16 Zeboiler duty 399 71527 kW Dondenser duty 312 58773 kW tage temperatures pressures liquid and vapor flows in kmol h T K P Pa a LIQUID C2H6 OGH8 CIH10 CIH10 CHU VAPOI Bottom product 361 66 530000 29 7485 0 359E 08 0 543766 1031683 18858 Top product 263 16811 500000 29 7485 4 833105 17 98915 4 455996 2 460342 0 RR 1 50 263 168511 500000 29 7485 4 633105 17 99915 4 455998 2 460342 2 87E 23 3 6E 49 285 80306 5005122 28 7518 0 974546 1310682 8 221982 644845 8 8E 22 59 497 48 294045396 5012245 28 35777 0 51557 9397879 9311468 9152849 97E 21 58 50 47 297 45470 501836 7 28 15443 0 450963 7 683638 9 23552 10 78431 9 02E 20 58 106 46 296 99289 502449 28 042684 0 435465 6 971584 6626632 1160696 7 66E 19 57 9031 45 299 74269 503061 2 27 973465 0 429428 6 673339
106. one or by electronic media for a period of 60 days after delivery of the product How to contact Prode you can contact Prode by phone web page or email the details are available at http www prode com How to obtain technical support we welcome your comments or suggestions about our program On request we will also provide information on the internal methods used While the program has been tested carefully to ensure proper operation it still may be possible for an unusual situation to result in an error We will have a much greater chance of fixing or assisting with errors and problems if they are provided to us in a form that is repeatable In reporting a problem to us the following information should be given e customer reference e the version of the software e a copy of the procedure you are running and if possible the input data e a detailed description of what you were doing Sequence of operations when the problem occurred any additional information you think may describe the problem Introduction Prode Properties includes a comprehensive collection of procedures to solve problems such as e Physical Properties Data e Heat Material Balance e Process Simulation e Process Control Equipment Design Separations e Instrument Design And more Technical features overview Entirely written in C from the origin Properties for Windows different versions for Android Linux etc are available is released in
107. op product distillate btm_h int stream for bottom product fnr int number of feeds fstr int vector fnr with the feeding streams fpos int vector fnr with feeds positions 1 stgnr snr int number of side streams sstr int vector snr with the list of side streams spos int vector snr with side streams positions 1 stgnr sft int vector snr with specified flow type GAS_PHASE LIQ_PHASE see Codes used in Prode library sflow double vector snr with the specified on each side stream side product to feed flow ratio vnr int number of variables to solve vtype int vector vnr with type of variable seebelow vrv double vector vnr with calculated values for variable ptype int vector pnr with type of specification see below piv int vector pnr with integer values as the position of components in the list prv double vector pnr with values of the specifications to solve flows double vector with calculated values for vapor liquid flows in all stages dimension nrphases nrc stgnr when a condenser is present the reflux is the liquid flow on top stage Codes for variables reboiler 1 total condenser 2 partial condenser 3 Codes for specifications reflux ratio product to feed ratio molar fract bottom to feed ratio molar fract component molar fract in top product component molar fract in bottom product component recovery in top product component recovery in bottom
108. ponent liquid flows in each stage 34 next example shows how to calculate the hydrate formation curve temperature and pressure for a given mixture From Excel menu File gt open in Excel folder in Prode Properties installation select the file hydrate xls IMPORTANT in order to calculate phase equilibria with hydrates you must include in stream one or more fomers plus water when solving multiphase equilibria Prode Properties considers SI SII and SH structures In Properties Editor select stream 6 Test Hydrate in both selectors of first and second window the 6 Test Hydrate stream includes a predefined composition C1 0 905 C2 0 05 C3 0 02 CO2 0 02 H2O 0 005 CH40 0 Prode Properties Editor g xi Stream Select edit stream 6 Test Hydrate Test Hydrate Saves Components Operating Conditions K Pa a kg s BIPs Config Chemicals Feed and Operation 6 Test Hydrate kais i i K alee FA m T IMPORTANT when solving phase equilibria with solids and hydrates to avoid large errors make sure to have the same model selected for vapor liquid solid and hydrate you can set inspect models from models tab in Properties Editor Base version allows two alternatives 1 CPA PR for vapor and liquid SP CPA for solid HYD CPA for hydrate 2 PR Extended PRX for vapor and liquid plus SP P
109. problems in chemical engineering and to achieve tight control over the calculations A non inclusive list would include Thermodynamic calcs flash operations enthalpy entropy volume energy unit operations Streams data access and calcs set and retrieve operating conditions critical and transport properties calcs e Chemicals library access retrieve data from chemicals file e Error messages management of errors messages Methods for thermodynamic calc s Prode Properties includes a complete set of methods for solving all the standard flash operations with specified final temperature or pressure and entropy or enthalpy or volume or energy basis phase fraction with temperature or pressure basis plus mixers dividers gas liquid phase separation operations etc integer result setOp integer stream double t double p Given a stream operating pressure and temperature performs an isothermal flash and sets operating conditions integer result setSOp integer stream Given a stream performs an isothermal flash at user defined standard conditions double t PfPF integer stream double p double pf int state int n Given a stream the pressure phase fraction range 0 1 state gas liquid solid and position n calculates and returns the nth n 1 5 equilibrium temperature along the specified phase fraction line double p PfTF integer stream double t double pf int state int n Given a stream the temperature
110. product NORWOOD Notes When passing returning paramenters the first element in vectors is the element 0 Main variables 1 vnr are when specified reboiler and condenser partial or total each variable of type defined in vtype requires a suitable specification in ptype piv prv usually for reboiler the specification is the product to feed ratio and for a condenser the reflux ratio but specifications based on component s fractions on top and bottom products are permitted in these cases specify in piv the position of selected component in the list and in prv the value of the fraction required Secondary variables are side streams 1 snr each side stream defined in sstr spos requires in sflow a specification for the side product to total feed flow ratio 76 The column is modeled with thermodynamics and options defined for the first feed in the list Initialization in most cases the procedure doesn t require to initialize values when required set the variable init to 1 and define the proper initial values in vectors stgt and flows note that in a sequence of similar operations for example when controlling the operating point of a column it may result useful to reintroduce the calculated values as starting point for the new calculus Examples Column with 8 stages 1 feed stage 4 pressure reboiler 12 5 Bar pressure top 12 Bar efficiency 1 dH 0 csep 1 stgnr 8 init 0 stgp 0 12 5 stgp 7 12 stgef 0
111. r gt if not libisloaded ppp hfile C Program Files Prode MATLAB ppp h J loadlibrary ppp dll hfile end libfunctions ppp this command will load Prode Properties in memory and print the list of methods avaliable you may wish to modify C Program Files Prode MATLAB ppp h to reflect your installation s settings Functions in library ppp AFOpen CompLD Divi EStrLss PSep StrGIc StrLV StrST getAji getPatm putMod AFSave CompLV EStrFMH EStrLV PfPF StrGICp StrLVE StrSv getcc getSUMS putN AOpen CompMp EStrFML EStrLVE PfTF StrGJT StrLf StrSvd getCNr getT putZ ASave CompMw EStrGC EStrLf SPF StrGMw StrMDt StrTc getCi getUMC setAc BFsave CompN EStrGCp EStrPf STF StrGS StrMw StrTcm getCj getUMN setErrFlag BPF CompNb EStrGCv EStrs StrAc StrGss StrN Strvv getErrFlag getUMS setKM BPLine CompPc EStrGD EStrSCp StrCBp StrGV StrPc StrVvd getFCNr getW setMFg BRegr CompRg EStrGIC EStrSD StrcBt StrGVE StrPcm StrZv getFPNr getWm setMH CompAc CompSC EStrGJT EStrstT StrCPnr StrH StrPf StrlnFv getGij getxX setMS CompCID CompSD EStrGMw EStrZv StrCTp StrHC StrPt StrinFvd getGji getY setMV CompDm CompSG EStrGss ErrMsg StrcTt StrHv StrPts StrlnFvdv getKji getz setMw CompF CompSL EStrGV GSep StrCopy StrHvd Strs UMAU getMBPNr inits setOM CompGC CompSs EStrGVE HPF StrFMH StrLc StrSCp UMCR getMCNr isSDef setOp CompGV CompST EStrH HPFORM StrFML StrLCp StrsD UMCS getMFg loadsB setPc CompGf CompSf EStrHC HTF StrFv StrLCv StrSGH UMRAU getMH putAji sets CompH
112. r 10 Prode Properties Editor xi Strearn Operating Select editstean I Save Components Operating Conditions K Pa a kg s Models BIPs Config Chemicals Feed and Operation 1 Test Case 1 1 BIPS Specifications 200 K 37 bar a 1 kg s Licence Specifications OUT 1 72 bar a kV On second page Composition we define the composition 0 982 Methane 0 018 CO2 Prode Properties Editor E Stream Operating Components Models BIPs Config CARBON DIOXIDE Sort by first name Molar fract 0 1 7 Chemicals 4 BIPs Add Remove Licence Clear l Component Molar fract 0 1 METHANE 0 982 CARBON DIOXIDE Oo On third page Models we select the predefined package Soave Redlich Kwong Extended the extended models available in Prode Properties include parameters calculated data regression for best fitting of vapor pressure enthalpy and liquid volume of pure fluids Prode Properties Editor x Stream Operating Predefined packages 1 Soave Redlick Kwang standai_ Soave Redlick Kwong Extended Components 1 Redlick Kwong standar Models AS fedlick Kwong Extend BIPs 3 Peng Robinson Standard 4 Peng Robinson Extended Confia Piae ii a S ES AA in fourth page BIPS click on button Get BIPs from database
113. ra NTa aE Kaa TEE N aOR ada aiaa lates 91 Methods for accessing data editing WINdOWS oroni essensa a Re A Minders 91 Methods to load save ArChIVES 5 4 25 S2cccsceteagaategesscaeiseee cedeadinsstseeesscaesdeqee aaseiiedaesanesisecetsstces cies sansa cusecaia sce d aiesiedadestseuseietsazsteasoleaes 91 Methods for accessing defining the Units Of measurement ee eee cent eeeeneeeeeeeeeeeeaeeteeaeeeteaaeeeeeaeeeseaeeeseaeeeseneeeesenteeeeneeesenaeees 92 Additional Meto dS a bh eels eal eee daca Ledet Sed eed as aE ie ids PRL bad aids A ced 92 Application example Skirius e eats E ee ie Adee ee ene deca ee eed 93 How to define directly a stream without accessing the Properties Editor eee eeeeeeenneeeeeeeeeeeeeeenaeeeeeaeeesaeeeseeeeeneneeennaeeees 94 How to save and restore streams toy froma file ves stzceesccedtesas sche teeeacdegee sates sascnenntoeeaussecavaucedsncatctsbeneesenseteve caged diaa eiaha 95 Error IMOSSAGCS en eapi aey aaa stat N ANETA SAE IAL AO A a ced Lea EE EEEa EU TURS EAE E E EA EE A 96 Calculation Dasi Ssma ea R NE E O a ea E ie 97 Gimitsin thermodynamic Cale S seyss oeiee e aa E EOE cteacsadasnagascheauenzelaniqesadecccerasubeqaiess acceessdaededadesndguendatsapaceesseenss 97 Chemical S File fOnmmal tic iresi ga eae eiae aea A E a E E E a E A E a aiea 98 Sources of dala inma a a aa a a a a aa E Ea a ar E a LOM le 101 Comparing Prode Properties results against those of different process simulators eceeeee
114. rature and initial value from which to start integration for entropy and enthalpy from Properties Editor in setting s page these values are stored in archive and restored when program starts In addition it is possible to modify these value by code with the following methods akwWNhM integer res setHB integer mod double t double val given a code to identify the procedure see the table with codes the temperature and initial value sets base value for enthalpy integer res setSB integer mod double t double val given a code to identify the procedure see the table with codes the temperature and initial value sets base value for entropy Table of codes to specify the different base values in setHB and setSB reference methods setHB setSB Code Procedure 1 initial values specified by user values of t and val 2 initial values are enthalpy of formation or entropy of formation and temperature 25 C 89 Methods to set access stream s names In Prode Properties streams have several properties including a label name which could match for example the name of a line in your project you can easily set access these labels through a series of methods VARIANT str MSirN integer stream given a integer that identifies a stream method returns a string identifying that stream this is the Microsoft specific method char str StrN integer stream given a integer that identifies a stream m
115. re and pressure outlet pressure and polytropic efficiency Notice that Prode Properties includes a specific methof for solving a polytropic stage with phase equilibria this method permits to simulate both single phase vapor and mixed vapor liquid processes The mixture Methane 0 999 n Butane 0 001 predefined stream 2 at 10 Bar a shows a dew point of 187 5 K by setting a inlet temperature of 180 K we specify vapor liquid as inlet condition the standard method can simulate only gas streams however the Polytropic solution with phase equilibria method allows to solve this case 29 A_ E coo E E P Ca fy PE 1 Single polytropic stage design and rating for gas and gas liquid flow Ea INSTRUCTION Ess Stream Rate From Properties editor define the composition for the specified stream 4 Pin in this page enter pressures temperatures flow with proper units and method to Eaa Tin then click on Rate button to estimate the polytropic efficiency head and power 6 Pout ea Tout Result Us Flow spec 1 mass flow 2 volumetric flow at inlet condition Esi Flow kg s 10 Method 2 2 Huntington 4 Polytropic solution with phase equilibria 11 2 Efficiency 13 Head 14 Power EE INSTRUCTION 16 Stream Design From Properties editor define the composition for the specified stream mz Pin in this page enter pressures temperature efficiency flow with proper units and m 18 Tin then cl
116. re can model compression and expansion units such as centrifugal compressors expansion turbines etc the procedure returns calculated temperature options 1 3 calculated efficiency options 2 4 models available 1 given initial condition pout and polytropic efficiency calculates outlet condition R A Huntington Evaluation of Polytropic calculation Methods for Turoomachinery Performance method applicable to gas phase only given initial condition pout and tout calculates polytropic efficiency R A Huntington Evaluation of Polytropic calculation Methods for Turbomachinery Performance method applicable to gas phase only given initial condition pout and polytropic efficiency calculates outlet condition R Paron Polytropic solution with phase equilibria method applicable to gas and mixed gas liquid phases given initial condition pout and tout calculates polytropic efficiency R Paron Polytropic solution with phase equilibria method applicable to gas and mixed gas liquid phases NM w A additional models available from Prode 79 Methods for relief valves design rating This unit models a relief valve with different methods double area ISPF int stream double pout int model double param Parameters stream int inlet stream pout double outlet pressure model int model see below codes 1 4 param double correction parameter see below the range of values the proc
117. rmamide Perfluorohexane Perfluoromethylcyclohexane Methyl acrylate Methylsilane Diethylsilane Heptamethyltrisiloxane Heptamethyldisiloxane 1 3 Dimethyldisiloxane 1 1 3 3 Tetramethyldisiloxane Octamethylcyclotetrasiloxane N methylpyrrolidone Trichlorofluoromethane Tetrachloro 1 2 difluoroethane Dichlorofluoromethane 1 Chloro 1 2 2 2 tetrafluoroethane 1 2 Dichlorotetrafluoroethane Chlorodifluoromethane Chlorotrifluoromethane Dichlorodifluoromethane Acetamid N Methylacetamid N Ethylacetamid N N Dimethylacetamid N N methylethylacetamid N N Diethylacetamid 2 Ethoxyethanol 2 Ethoxy 1 propanol Dimethylsulfide Diethylsulfide Diisopropylsulfide Morpholine C4H4S Thiophene C4H3S C4H2S 2 Methylthiophene 2 3 Dimethylthiophene 104
118. rs to set one or more options call setOM passing as value a integer with the sum decimal values of all required options Table of codes to specify the different states reference methods setMP PfTF PfTF StrFv StrFvd Code State 0 Vapor phase 1 Liquid phase 2 Solid phase 3 Hydrate phase Table of codes to specify the different models reference methods setMP getMP Caution Some models may not be available and or the codes may change in different_versions contact Prode for details Code Model 1 Regular 11 Pitzer 21 Hayden O Connell 31 Wilson 32 NRTL 33 Uniquac 40 Unifac 50 Soave Redlich_Kwong VDW 51 Soave Redlich_Kwong Extended VDW 60 Peng Robinson VDW 61 Peng Robinson Extended VDW 62 Peng Robinson Wilson WS 63 Peng Robinson UNIQUAC WS 64 Peng Robinson NRTL WS 65 Peng Robinson UNIFAC WS 66 Peng Robinson Wilson MHV2 67 Peng Robinson UNIQUAC MHV2 68 Peng Robinson NRTL MHV2 69 Peng Robinson NRTL LCVM 70 BWR 71 BWRS 75 Lee Kesler 76 Lee Kesler Plocker 80 Solid Pure based on Peng Robinson Extended 81 Solid Pure based on CPA Peng Robinson 82 Solid Pure Regular solid pressure 83 Solid Solution based on Peng Robinson Extended 85 Hydrate based on CPA Peng Robinson 86 Hydrate based on Peng Robinson Extended 87 Hydrate based on CPA Electrolyte 90 PC SAFT 95 CPA Soave Redlich Kwong 96 CPA Peng Robinson 97 CPA E
119. rst component in the chemical s file Microsoft NET VB see the samples provided with Prode Properties for additional information e include properties vba to instruct the compiler about the methods available in Prode Properties and access the methods CompName MCompN 1 Microsoft Excel Microsoft Excel supports macros and VBA language for defining procedures both of these can be used to access the functions in Prode Properties see the samples provided with Prode Properties for additional information e include properties vba to instruct Microsoft Excel about the methods available in Prode Properties and access the methods CompName MCompN 1 64 Translate resources to different languages A large part of the resources are stored in the file res lan see the paragraph Data files folder for additional information about how to locate the file The file res lan is a text file easily editable by the user Example in English language N2_NAME Nitrogen in French language N2_NAME Azote in Italian language N2_NAME Azoto IMPORTANT When editing a string take care to modify only the parts enclosed within the braces composed by special characters as for example Microsoft Applications and Strings Prode Properties utilizes the standard API calling convention for Microsoft Windows applications This assures that almost all Windows compatible applications which support DLLs will also suppo
120. rt Prode Properties There are however some exceptions in passing strings arrays of characters since Microsoft utilizes proprietary data formats Prode Properties includes Microsoft specific methods in addition to the standard methods supporting the ANSI C standard Microsoft specific methods are compatible with almost all Microsoft applications Define models compatibility with old verions Prode Properties includes many methods for defining via software the thermodynamic models and the related options see the paragraph Methods to set access different options for additional information and do not alter modify the data structures 65 Units of measurement Prode Properties allows to define via software the units of measurement there are methods for defining the units and methods for retrieving codes and strings see paragraph Methods for accessing defining the units of measurement and the samples provided with the package for additional information in Prode Properties to reference a unit must use a numeric code QUANTITY Pressure abs Pressure rel Temperature abs Temperature rel Calorific Value weight Calorific Value molar Power Entropy Streams Heat Capacity weight Heat Capacity molar Flow mass basis Flow gas mass basis Density weight Density molar Specific Volume weight Specific Volume molar Thermal Conductivity Viscosity dynamic Surface Tension Lenght Area
121. s Fraction 0 1 d in Stfream gt Models dialog we define SRK VDW select in predefined packages for both gas and liquid e we set Multiphase equilibria to Multiphase vapor liquid and Multiphase initialization to Standard tests Prode Properties Editor xi FE A rs Licence Multiphase vapor liquid f then we can edit BIPs we can input data or load from database IMPORTANT when accessing the library from an external program you must define the proper settings in stream s options for multiphase flash operation 13 Prode Properties Editor me SC Prode Properties Editor Notice that once saved the dialog shows the feed composition of the stream Now you can define access diferent streams as the program remembers your data for stream 2 MPORTANT before to leave the application remember to save all data into the archive otherways your changes will be lost_read the paragraph Working with archives save and load data default settings for additional information 14 From the dialog Stream gt Operating you can calculate a isothermal multiphase flash select stream 2 as feed then T P VLL isothermal Vapor Liquid Liquid enter 187 K as temperature and 40 atm g as pressure this is the example provided by Michelsen in Calculation of multiphase equilibrium then click on Compute the procedure will calculate two liquid ph
122. s Liquid density correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Liquid viscosity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Liquid thermal conductivity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Liquid heat capacity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Solid vapor pressure correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Solid density correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters 99 Solid thermal conductivity correlation type of equation unit for property unit for temperature low temperature limit high temperature limit A E 5 parameters Solid heat capacity correlation type of equation unit for property unit for temperature low temperature limit igh temperature limit A E 5 parameters 100 Sources of data Data in chemical data file come from several sources including e Dechema Chemistry Data ser text books e DIPPR data c
123. s the stream B5 is the outlet pressure B4 the required entropy equal to inlet entropy being a isentropic process and 0 0 as estimated final temperature SOMMA vy X v amp SPF 2 B5 B4 0 A rc tC _1 Inlet Pressure 1000000 Pa 2 Inlet Temperature 203 K 3 Inlet Enthalpy 5397 561779 Kw 4 Inlet Entropy Kw 5 Outlet Pressure 2000000 Pa 6 Isentropic Outlet Temperature SPF 2 B5 B4 0 IK _f Outlet Isentropic Enthalpy 5471 336367 Kw 8 Adiabatic Efficiency 0 75 9 Outlet Enthalpy 5495 927896 Kw 10 Mechanical Efficiency 0 98 11 Estimated Absorbed Power 100 373588 Kw 12 Estimated Outlet Temperature 253 9183245 K to calculate the outlet enthalpy enter in cell B7 EstrH 2 B6 B5 and in cell B9 enter B3 B7 B3 B8 to calculate the final enthapy with the adiabatic efficiency specified in cell B7 to estimate the absorbed power in cell B11 enter B9 B3 B10 Since we know the enthalpy and pressure at outlet conditions we can calculate the temperature with HPF method HPF 2 B5 B9 0 where 2 is the stream B4 is the outlet pressure B8 B6 represents the heat duty the difference from initial conditions calculated in cell B6 and 0 0 the estimated final temperature 29 SOMMA vy X v amp HPF 2 B5 B9 0 A la Sea Cc 1 Inlet Pressure 1000000 Pa 2 Inlet Temperature 203 K 3 Inlet Enthalpy 5397 561779 Kw A Inlet Entropy 59 74773903 Kw 5 Outlet Pressure 2000000 Pa 6 Isentropic Ou
124. solid liquid equilibria include in X column the measured liquid molar fraction of component 1 in liquid phase and in Y column the measured solid molar fraction of component 1 finally enter the temperature and the pressure for that point Example of measured VLE data for Methanol Water VLE data for Methanol Water at 735 mmHg Point VLE VLE VLE VLE VLE VLE VLE VLE X 1 0 008400 0 025800 0 068000 0 137000 0 240000 0 480000 0 572000 0 741000 Y 1 0 103000 0 227000 0 391000 0 568000 0 680000 0 790000 0 820000 0 906000 Temperature C 96 5 92 3 87 5 80 1 75 9 70 6 68 7 66 4 57 Pressure mmHg 735 735 735 735 735 735 735 735 Enter the measured data select the models to regress in this case Wilson for liquid phase and regulat ideal for vapor phase Prode Properties Editor x E Stream E Contig REGULAR tit E a WMLSON O o j pi Do not accept calc X Y outside 0 1 range gt vata Regress measured VLE LLE data points X B Licence 0 15000 15000 0 103 73 0 227 73 lo 391 735 0137 lo s6a EX C735 mmHGa 024 loss i759 c 735 mmHG a 048 lo 73 706 S 735 mmHG a 0 572 To 82 687 C 735 mmHG a 0741 lo S06 664 735 mmHG a Selecting the button Calculate the procedure calculates the best fitting parameters shows the calculatd results and the relative errors Prode Properties Editor x gt Stream E Config
125. ssure specifications they return the temperature at which the calculated value of enthalpy or entropy equals the specified value These methods permit to solve many problems for example model heat exchangers where you know inlet and outlet pressures and heat duty simulate valves where you know inlet and outlet pressures usually valves are modeled as adiabatic processes dh 0 simulate pipelines where you know inlet and outlet pressures and heat exchanged with surrounding environment model pumps and compressors when you know inlet and outlet pressures Supposing we wish to simulate a process to cool down the mixture already examined in previous examples Methane 0 7 Carbon Dioxide 0 15 Hydrogen Sulfide 0 15 with Soave Redlick Kwong model from the point A in retrograde region and near the dew line 89 Bar a and 246 K to the point B located close to the critical point 225 00 230 00 235 00 240 00 245 00 250 00 255 00 260 00 89 00 87 00 85 00 83 00 81 00 79 00 77 00 this example can represent a good test for evaluating the stability and reliability of convergence in retrograde region 23 select stream 1 verify the list of components and molar fractions C1 0 7 CO2 0 15 H2S 0 15 the models for vapor and liquid fugacity SRK VDW and the values for BIPs Prode Properties Editor x with these values the calculated p t for critical point are 79 117 B
126. st Hydrate 0 00489785 0 0686959 0 0212596 0 0159116 0 00379904 0 890334 0 you may decide to adopt methanol as inhibitor to avoid the formation of hydrates IMPORTANT depending from models BIPs for liquid solid equilibria water methanol may have limited ranges of application for the predefined BIPs included in Prode Properties PRX model the allowed range for the fraction methanol water is 0 0 0 4 to keep the errors in calculated freezing point depression below 1 5 2 K in the range 210 273 15 K if you wish to inject more methanol make sure to recalculate the liquid solid BIPs with the utility available in Prode Properties for the details see the paragraph Regress VLE LLE SLE data 36 In this example we will consider a methanol fraction of 0 002 equivalent to 0 002 0 005 0 4 the maximum allowed In component s tab edit methanol fraction and methane fraction so that resulting composition will be C1 0 903 C2 0 05 C3 0 02 CO2 0 02 H20 0 005 CH40 0 002 in the Operating tab click on Save button to store the new composition then solve the TP VLSH operation to find the predicted hydrate formation pressure in this case we test 277 K 50 Bar a without finding hydrate formation Prode Properties Editor Se N 37 As alternative to solve the multiphase flash operations you can calculate the hydrate formation curve directly
127. stream pressure and temperature performs an isothermal flash and returns the specific heat capacity constant pressure liquid phase double cv EStrLCv integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the specific heat capacity constant volume liquid phase double c ESirGIC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the isothermal compressibility in gas phase double c ESirLIC integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the the isothermal compressibility in liquid phase double ss StrMSS integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns returns the speed of sound gas liquid as calculated with HEM model for mixed phases double ss EStrGSS integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the speed of sound in gas phase double ss EStrLSS integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the speed of sound in liquid phase 83 double jt EStrGJT integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the Joule Thomson coefficient for gas p
128. t NET VB C applications IMPORTANT Microsoft NET support files are located in the directory Prode NET Prode Properties can be easily included as unmanaged code in every Microsoft NET application for compiling the sample code provided with Prode Properties a recent version of Microsoft Visual Studio is required From Microsoft Visual Studio compiler menu File gt Open gt Project Solution in NET folder in Prode Properties installation select the file vba sln File Edt View Project Bukid Debug Tools Test window Heb Open Project x Object name Juba sh Objects of type aut Proyect Fas sin dew vew epeo bp gt C Add to Solution Clore Solution then from menu Build select Build Solution Note if desired you can edit the settings from Project gt vba Properties g vba Microsoft Visual Studio Fle Edt View Project Buld Debug Data Tools Test Window Help j Output Build sta 4 ion Debug Any CPU vba gt C Progra failed O skipped 42 As next step you can test the application from Visual Studio menu Debug gt Start Debugging then once the application is running 1 click on the button Prode Properties editor to access the editor define the streams and units of measurement 2 define a suitable temperature and pressure with proper units 3 click on button Compute Properties to print the properties Microsoft Visual Studia ShowPUM Text t isothermal f res setOp 3t I res
129. ta default settings Load and save archives Archives are files which contain the data required by Prode Properties to work with stream s and units of measurement when you open an archive the stream s data and units are loaded when you choose to save an archive these data are stored in a file in this way you can work with many different projetcs Prode Properties includes several methods to save and load data as archives The default settings When Prode Properties starts it loads data from the archive named def ppp so if you wish to use your own list of streams units etc just save your preferred settings under the name def ppp Properties editor Prode Properties includes Properties editor from the editor you have access to Streams edit operating conditions flow compositions models BIPs for all streams Config edit all units of measurement and settings e Chemicals edit all chemical s data regress data add new chemicals BIPs edit BIPs regress data add new BIPs How to activate the Properties editor call one of the methods edS stream edSS remember that in Prode Properties each stream is referenced with a code integer value in the range 1 max number of streams Use the right method Use edSS if you wish to start editing the first stream but access all streams Use edS stream if you would like to choose which stream to edit From Microsoft VB Call edSS Call edS 8 start editing stream nr
130. the molecular weight for liquid phase double If EStrLf integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns liquid fraction molar basis in stream double pf ESirPf integer stream integer state double t double p given a stream state gas liquid solid pressure and temperature performs an isothermal flash and returns the phase fraction molar basis in specified state double zv ESirZv integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the relevant compressibility factor gas phase double h EStrH integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the enthalpy gas liquid phase double v ESirV integer stream double t double p given a stream pressure and temperature performs an isothermal flash and returns the specific volume as sum of specific volumes of all phases double cp EStrGCp integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the specific heat capacity constant pressure gas phase double cv EStrGCv integer stream double t double p given the stream pressure and temperature performs an isothermal flash and returns the specific heat capacity constant volume gas phase double cp EStrLCp integer stream double t double p given the
131. the outlet enthalpy as outlet enthalpy for the isentropic process enthalpy at inlet conditions outlet enthalpy enthalpy at inlet conditions adiabatic efficiency d calculate the outlet temperature at given outlet enthalpy The specifications are mass flow 1 Kg s fluid Methane 0 999 n Butane 0 001 this is the Test case 2 to compress from 10 Bar a 203 K to 20 Bar a we assume 0 75 as adibatic efficiency and 0 98 as mechanical efficiency In Excel we define the inlet conditions with macro EStrH which forces a isothermal flash at specified pressure and temperature EStrH 2 B2 B1 where 2 is the stream B2 is the inlet temperature and B1 is the inlet pressure SOMMA X v amp EstrH 2 B2 B1 A es ee 1_ Inlet Pressure rf 4000000 Pa 2 Inlet Temperature PF 20K Ea Inlet Enthalpy EstrH 2 B2 B1 kw 4 Inlet Entropy 59 74773903 Kw 5 Outlet Pressure 2000000 Pa 6 lsentropic Outlet Temperature 243 4167696 K 7 Outlet Isentropic Enthalpy 5471 336367 Kw 8 Adiabatic Efficiency 0 75 9 Outlet Enthalpy 5495 927896 Kw 10 Mechanical Efficiency 0 98 11 Estimated Absorbed Power 100 373588 Kw 12 Estimated Outlet Temperature 253 9183242 K in cell B4 we calculate the initial entropy as EstrS 2 B2 B1 to calculate the outlet temperature for the isentropic process in celll B6 we enter SPF 2 B5 B4 0 where 2 i
132. the results Prode Properties Editor ay Stream Operating Model for vapor phase Components Model for liquid phase Models BIPs l Config measured VLE LLE SLE data points 4 Chemicals Standard basic search BIPs i j Accept calc X Y outside 0 1 range Data l Models Licence high limit Calculate BIP 1 0 594397 0 999 0 999 BIP 2 0 158481 0 999 0 999 Clear BIP 3 0 0187911 0 999 0 999 BIP 4 0 482164 0 998 0 999 _seve_ BIP S jo jo 0 x4 0 9432 i zos 0 9999 259 65 k zos 0 9999 242 95 K 0728 0 9999 233 45 kmj xosa os999 217 95 n xllos7e7s os999 257 65 k_ zioscsss fo sss99 248 85 K Pressure X calc Error bar g 0 947416 0 446967 bar g 0 893741 0 695423 bar g 0 786932 1 63347 0 734414 0 881037 bar g 0 64541 0 688046 bar g 0 884411 0 872674 bar g 0 817208 1 41201 of gt cot _ elolololfololfo 60 Then click on Save button to move calculated values on Data tab in Data dialog select SLE BIPs as database and click on Save button to store data you may use File button to store permanently data in bips dat file Prode Properties Editor x Stream Operating Components Models BIPs l
133. the samples provided with the software Properties includes a procedure for solving staged columns the column is modeled with stgnr equilibrium stages column may include a condenser and a rebolier stage numbering is bottom up the bottom stage reboiler if specified is number one and the top stage condenser if specified is number stgnr There may be one or more feeds a feed is modeled by entering liquid on the specified stage and vapor portion to the stage above with exception of top stage There may be one or more side streams Heat added removed on each stage can be specified Efficiency parameter on each stage can be specified integer res DCOL int csep int stgnr int init double stgt double stgp double stgef double stgdH int prod_h int btm_h int fnr int fstr int fpos int snr int sstr int spos int sft double sflow int vnr double vrv int vtype int ptype int piv double prv double flows Parameters csep int column type 1 VLE 2 VLLE 3 LLE some features available in extended versions stgnr int number of stages init int O for automatic initialization 1 temperatures and flows are defined by user stgt double stgp double stgef double stgdH double vector stgnr with stage temperatures vector stgnr with specified stage pressures vector stgnr with specified stage efficiency permitted range 0 1 1 vector stgnr with specified dH heat added removed prod_h int stream for t
134. theProperties Editor The functions for accessing components in Prode Properties require the component code this code may vary in different versions of chemical file to convert the ID to the component code utilize the method CompCID and ComplID to convert from code to ID this example shows how to access data with ID code Dim code As Long ID As Long Pc As Double ID 74840 CAS code for Ethane but the user may define his own list of values code CompCID ID get the code Pc CompPc code and the critical pressure 93 How to define directly a stream without accessing the Properties Editor Prode Properties includes methods to access read and write each different value in a stream making it possible for the user to create procedure to define edit update directly each value without going through the Properties editor Following list presents the methods for accessing all items operating pressure operating temperature flow vector getMCNr elements with components codes vector getMCNr elements Z vector mole basis getZ thermodynamic model and related options vector getMBPNr elements of Ci vector getMBPNr elements of Cj vector getMBPNr elements of BIP matrix read the value set the value getP getT getW getCC getMP getCi getCj getBIP When defining a stream one must follow these steps e call initS method to clear all stream s data definedata c
135. timate method solves the flash operation entropy basis and returns final temperature double p STF integer stream double t double s double ep Given a stream final temperature the required final entropy see the method StrS for the definition and a estimated value for final pressure or 0 for automatic estimate method solves the flash operation entropy basis and returns final pressure double t VPF integer stream double p double v double et Given a stream final pressure the required specific volume see the method StrV for the definition and a estimated value for final temperature or 0 for automatic estimate method solves the flash operation volume basis and returns final temperature double p VTF integer stream double t double v double ep Given a stream final temperature the required specific volume see the method StrV for the definition and a estimated value for final pressure or 0 for automatic estimate method solves the flash operation volume basis and returns final pressure integer result HVF integer stream double h double v double et double ep Given a stream the required final enthalpy see the method StrH for the definition the required final specific volume see the method SirV for the definition and estimated values for final temperature and pressure or O for automatic estimate method solves the flash operation 67 integer result SVF integer stream double s doubl
136. tlet Temperature 243 4167696 K T Outlet lsentropic Enthalpy 5471 336367 Kw 8 Adiabatic Efficiency 0 75 9 Outlet Enthalpy Kw 1H Mechanical Efficiency 0 98 11 Estimated Absorbed Power 100 373588 Kw ENE Outlet Temperature HPF 2 B5 B9 0 IK Now if we wish to evaluate the performance at different conditions we can modify the inlet conditions for example setting 2500000 Pa a as outlet pressure and changing the value in cell B1 or cell B2 to force a recalc BS X fe 2500000 A a C _1_ Inlet Pressure 1000000 Pa 2 _ Inlet Temperature 203 K 3 Inlet Enthalpy 5397 561779 Kw 4 nlet Entropy 59 74773903 Kw 5 Outlet Pressure 2500000 Pa 6 Isentropic Outlet Temperature 257 9890919 K 7 Outlet Isentropic Enthalpy 5497 900368 Kw 8 Adiabatic Efficiency 0 75 9 Outlet Enthalpy 5531 346564 Kw 10 Mechanical Efficiency 0 98 11 Estimated Absorbed Power 136 5150868 Kw 12 Estimated Outlet Temperature 272 0167586 K In a similar way you can define a procedure to model a polytropic process 30 Next example shows how to simulate a compression stage as polytropic process where the inlet stream can be vapor or vapor liquid mixed comparing the results of different methods see the paragraph Methods for solving a Polytropic operation for additional information We use a predefined Excel page as interface to Prode Properties From Excel menu File gt open in Excel folder in Prode Properties installation select the file c
137. tor 59 Regress SLE Water Methanol and test the calculated freezing point depression This example will show how to estimate BIPs for different models from available SLE equilibrium points SLE data for Water Methanol atm pressure First component is Water second component Methanol X1 is the water fraction in liquid phase while Y1 is solid fraction always 0 9999 for a model based on pure fluid Point X1 Y1 Temperature K Pressure Bar g SLE 0 9432 0 9999 266 85 0 SLE 0 9 0 9999 259 65 0 SLE 0 87676 0 9999 257 65 0 SLE 0 80583 0 9999 246 85 0 SLE 0 8 0 9999 242 95 0 SLE 0 728 0 9999 233 45 0 SLE 0 641 0 9999 217 95 0 SLE 0 636 0 9999 214 95 0 SLE 0 6 0 9999 208 15 0 as first step in BIPs gt Data page you must select the components in this example methanol and water Prode Properties Editor xj Stream Operating Components Models BIPs l Config l Chemicals BIPs Regress Models Licence Min temp in data set 217 95 K Max temp in data set 266 85 K Min press in data set 101327 Paa Max press in data set 101327 Pa a X Y data fitting error 0 358844 K12 0 349532 K12 T 0 309601 K12 T2 0 16291 L12 0 528678 then in BIPs gt Regress page select models CPA PR for vapor CPA PR for liquid SP CPA for solid options enter all data points and click on Calculate button to get
138. tor 2 additional models on request 78 Methods for fluid flow problems simulation of single phase two phases multiphase flow on circular pipes int res PIPE int stream int model double diam double rough double length double dHeight double dHeat Parameters stream int inlet stream model int model for fluid flow and phase equilibria see below diam double pipe internal diameter rough double parameter defining relative pipe roughness length double lenght of this segment dHeight double height difference inlet outlet dHeat double heat added removed Codes for models Beggs amp Brill Hazen Williams AGA 1 additional models on request Methods for Hydrates phase equilibria methods for calculating hydrate formation pressure or temperature double p HPFORM int stream double t int method double t HTFORM int stream double p int method Parameters stream int inlet stream t double operating temperature or operating pressure method int 1 include SI SII SH 2 Sl 3 SIl Methods for solving a Polytropic operation Polytropic stage compression and expansion double val PSPF int stream double pout int model double param Parameters stream int inlet stream pout double outlet pressure model int model see below codes 1 4 param double for model 1 and 3 specified polytropic efficiency range 0 1 for model 2 and 4 measured outlet temperature the procedu
139. tuation is to provide a status flag that can be interrogated and used by the users at convenient points in the sequence setErrFlag integer state given a Boolean state sets the error flag to TRUE or FALSE The flag should be cleared state FALSE before each sequence of calculations and tested method getErrFlag after the calcs If this is done then a flag state of TRUE indicates that an error has occurred somewhere in the calculation sequence integer res getErrFlag a value of TRUE means that an error has been found please note that PROPERTIES doesn t clear the error flag state You should clear the error flag via setErrFlag before each sequence of calc s defErrMsg integer state a value TRUE for variable state sets on the Microsoft Windows Dialog Box and a message will appear every time an error is discovered A value FALSE sets off the dialog box no messages of error VARIANT str MErrMsg Returns the last error message generated this is the Microsoft specific method char str ErrMsg Returns the last error message generated this is the ANSI C compatible method Methods for accessing data editing windows Prode Properties includes two predefined methods for activating Properties editor integer res edS nteger stream given a integer that identifies a stream method activates the Properties Editor on the specified stream integer res edSS this method activates the Properties Editor on first str
140. ulated according GERG report ISO 18453 CPASRK Properties calculated as Q Qphys Qass where Qphys is derived from Soave Redlich Kwong model and Qass is the association term G M Kontogeorgis E Voutsas Yakoumis D P Tassios 1996 The model includes for each fluid 5 2 ass parameters calculated to fit the set of experimental data saturation pressures densities latent heats available in DIPPR or DECHEMA pure fluid data collections CPAPR Properties calculated as Q Qphys Qass where Qphys is derived from Peng Robinson model and Qass is the association term G M Kontogeorgis E Voutsas Yakoumis D P Tassios 1996 The model includes for each fluid 5 2 ass parameters calculated to fit the set of experimental data saturation pressures densities latent heats available in DIPPR or DECHEMA pure fluid data collections SPM Solid Pure Model solid phase treated as single component solid fugacity derived from liquid fugacity calculated according selected model SSM Solid Solution Model solid phase treated as homogeneous solution solid fugacity derived from liquid fugacity calculated according selected model Steam tables IAPWS 1995 Water steam properties calculated according IAPWS 1995 formulation for the thermodynamic properties of Water for general and scientific use issued by the International Association for the Properties of Water and Steam Hydrates Multiphase equilibria fugacities calculated according
141. ultiphase at specified temperature and pressure T P VLS vapor liquid solid multiphase at specified temperature and pressure T P VLSH vapor liquid solid hydrate multiphase at specified temperature and pressure LF P equilibrium temperature at specified liquid phase fraction and pressure LF T equilibrium pressure at specified liquid phase fraction and temperature H P VL equilibrium temperature two phases at specified pressure and enthalpy H P VLL equilibrium temperature vapor liquid liquid multiphase at specified pressure and enthalpy H P VLS equilibrium temperature vapor liquid solid multiphase at specified pressure and enthalpy H P VLSH equilibrium temperature vapor liquid solid hydrate multiphase at specified pressure and enthalpy S P VL equilibrium temperature two phases at specified pressure and entropy S P VLL equilibrium temperature vapor liquid liquid multiphase at specified pressure and entropy S P VLS equilibrium temperature vapor liquid solid multiphase at specified pressure and entropy S P VLSH equilibrium temperature vapor liquid solid hydrate multiphase at specified pressure and entropy V P VL equilibrium temperature two phases at specified pressure and specific volume V P VLL equilibrium temperature vapor liquid liquid multiphase at specified pressure and specific volume V P VLS equilibrium temperature vapor liquid solid multiphase at specified pressure and specific vo
142. units of measurement and Prode Properties will calculate the value of Idensities and iquid fraction accordingly in this way is very easy with Excel to solve many different problems leaving to Prode Properties the task to calculate all properties for pure fluids and mixtures 12 Next example permits to calculate the phase fractions and compositions in multiphase equilibria to show the result in Excel we ll use a predefined Excel page from Excel menu File gt open in Excel folder in Prode Properties installation select the file multiphase xls and click Ok to load the file We need to define a new mixture a from Properties menu select Edit Properties b in Stream gt Operating dialog we select the stream number 2 and define the name Mlxture 2 Prode Properties Editor xj J Stream Components Select fedit stream 2 Operating Condtions K wi Midure 2 E Contig amp Chemicals Feed and Operation 1 Test Case 1 EN iin Specifications 288 15 K 101327 Paa 1 kgs Specifications OUT Paa KY j Phase Not present Not present Not present Not present Mol traction 0 lo lo 0 0 0 c then we select t Stream gt Components dialog and define a composition of two components with following molar fractions Methane 0 9 n Hexane 0 1 Prode Properties Editor d xi EF Stream Operating n HEXANE Sort by first name BPs Molar fractions 3 Config 4 Chemicals BIP
143. urns the total stream entropy gas phase double s StrSGS integer stream given a stream returns the specific unit weight entropy gas phase double s StrLS integer stream given a stream returns the total stream entropy liquid phase double s StrSS integer stream given a stream returns the total stream entropy solid phase double s StrSLS integer stream given a stream returns the specific unit weight entropy liquid phase double s StrSSS integer stream given a stream returns the specific unit weight entropy solid phase double s StrS integer stream given a stream returns the total stream entropy gas liquid solid phases integer res setWm integer stream double W given a stream and flow mass basis sets the flow double w getWm integer stream given a stream returns the flow specified for that stream double hc StrHC integer stream given a stream returns the calculated net heat of combustion gas phase double fl StrFML integer stream given a stream returns the calculated flammability lean limit gas phase double fl StrFMH integer stream given a stream returns the calculated flammability rich limit gas phase double d StrLD integer stream given a stream returns the calculated liquid density at operating conditions double d SitrGD integer stream given a stream returns the calculated gas density at operating conditions double tc StrLC integer stream

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