WinPropTutorial Dry Gas, Wet Gas, Gas Condensate, Volatile Oil, Black Oil, and Heavy Oil 2011 Table of Contents Exercise 1 – Base Models of Five Different Fluid Types .........................3 Basic Setup and Dry Gas Fluid Model Creation ................................................................................3 Additional Exercises ..................................................................................................................... 19 Exercise 2 – Determination of MMP and MME ................................... 24 Addition of Injection Streams and Calculations ............................................................................. 24 Multi-Contact Miscibility Minimum Pressure Calculation ............................................................... 28 Exercise 3 – Creation of Raleigh Black Oil ........................................... 30 Setup of WinProp model with Plus Fraction Splitting ..................................................................... 30 Defining Calculations and Experimental Values ............................................................................. 32 Using Regression to Match WinProp model to Laboratory Results ................................................. 35 Matching Viscosity in WinProp to Laboratory Values ..................................................................... 38 Defining an IMEX Fluid Model Output ........................................................................................... 40 Exercise 4 – Heavy Oil Fluid Model .................................................... 44 Setup of WinProp model with Plus Fraction Splitting ..................................................................... 44 Matching of WinProp Model to Laboratory Results ....................................................................... 46 Matching of WinProp Model Viscosity to Laboratory Viscosity ...................................................... 49 Creating a STARS PVT Model from WinProp .................................................................................. 52 2|Page Exercise 1 – Base Models of Five Different Fluid Types The purpose of this exercise is to utilize WinProp to build 5 different types of fluid models. A general understanding of the interface and associated windows should be gained in the process of creating fluid models for Dry Gas, Wet Gas, Gas Condensate, Volatile Oil, and Black Oil cases. Basic Setup and Dry Gas Fluid Model Creation 1. Double click on the WinProp icon in the Launcher and open the WinProp interface. Please note that this course’s images and descriptions are based on WinProp version 2011.10 or newer. 2. Open the Titles/EOS/Units form and write “Dry Gas” in the Comment Line section and the Title Line 1 section. When inputting data for the other fluid models (Wet Gas, Gas Condensate, etc.) input the appropriate name for the model. Select PR 1978 as the equation of state to be used in characterizing the fluid model, select “Psia & deg F” as the units and Feed as "Mole". Figure 1: Title/EOS/Units Screen 3|Page 3. Go to Component Selection/Properties form and insert the library components in the following order: CO2, N2, C1, C2, C3, IC4, NC4, IC5, NC5, and FC6. To do this click on the Ins Lib button (Insert Library Component) and select the library components you wish to insert (select multiple components at a time by holding Shift or Control) then click on the right arrow to add the components (Figure 3), and click OK to finalize. If you need to inset a component you missed (Figure 4), select the component above where you want to inset the new component (Figure 5), and then use Ins Lib again to insert the new component directly under the current selection. (*Note: This feature is not working properly in Windows. It works only if you insert missing C2H6 when cursor is at CO2 location. It also works if you select one additional component). Figure 2: How to Insert Library Components 4|Page Figure 3: Selection of Components Figure 4: Component Definition Missing C2 Compound 5|Page Note on Order: The order of these components only matters in the input of compositions. + In all cases. Your component definition form should look like Figure 7 for Dry gas and Figure 8 in case of other fluid types. Click the New Row button.xls” under the REQUIRED DATA folder. In the Component Selection/Properties form select the last component on the list. Click OK to close the Form. Use the properties given in the file “Five Fluid Types Data. 6|Page . except “Dry Gas”. also characterize the C7 fraction with a single pseudocomponent by inserting a user defined component (Figure 6). specific gravity (SG) and molecular weight (MW).Figure 5: Select CH4 then use Ins Lib to insert the missing C2H6 Compound immediately below. and enter the information for component name. then click on the Ins Own button. In these examples the compositions will be copied from an Excel file in this order which implies that the order will be important. 4. Figure 6: Definition of C7+ Variable for Black Oil Fluid Type Figure 7: Example of Dry Gas Component Definition Screen 7|Page . The “secondary” corresponds to the injection fluid (if applicable). Open the Composition form and input the mole fractions of the primary composition as mentioned in the file “Five Fluid Types Data. (*Note: it is important that you enter a value of 0 for any components that are not present otherwise an empty space will cause the simulator to error.Figure 8: Example of Black Oil Component Definition Screen 5. The secondary stream concept will be covered in a later section.) Figure 9: Example of Black Oil Composition Form with compositions copy/pasted from excel file 8|Page .xls” (Figure 9). Figure 10: Example of Two-Phase Flash Calculation Form 7. Insert a Saturation Pressure form into the WinProp Interface to perform a saturation pressure calculation at the reservoir temperature.7 Psia and 60 deg F. The Two-phase Flash form should look like as shown in Figure 10. Open the newly inserted form by clicking on it and under the comments section type “Standard condition flash”. primary and secondary composition). We will be performing a flash at 14. The feed composition is subjected to mixed (i. Leave other calculation options as default.e. If any calculations need to be moved in a different order they must be copied/pasted by right clicking on the item and selecting “copy/paste after” respectively. Insert a Two-phase Flash form into the WinProp interface. 9|Page . Make sure that in doing this you have first selected the Composition form.6. It is important when adding new calculations to always click on the form you want to insert the calculation after/into. Also. 10 | P a g e . Open the form and type in “P-T envelope” under the comments section. Insert a Twophase Envelope form. Input the data as shown in Figure 12. We would also like to generate a pressure-temperature phase diagram. input the reservoir temperature and saturation pressure estimate as 180 ºF and 1000 Psia respectively (for Dry Gas). The input value of “Saturation Pressure Estimate” is used as an initial guess by WinProp during the iteration processes for calculating the actual saturation pressure. In the other cases insert the temperature as given in the Excel file but still use 1000 Psia. Open the Saturation Pressure Calculation form.8. Figure 11: Example of Two-Phase Saturation Pressure Form for Dry Gas 9. Under the comments type “Psat at reservoir temperature”. pressure step of 250 Psia and No. Input the reservoir pressure as 250 Psia. 11 | P a g e . of pressure steps as 12 for dry and wet gas cases. The reservoir temperature will also change depending on the case you are modeling.xls”. and 24 for gas condensate.Figure 12: Example of Two-Phase Envelope Construction for Dry Gas 10. pressure at the reservoir temperature using the 2phase flash calculation. as mentioned in the file “Five Fluid Types Data. This can be done by adding another Two-phase Flash calculation form. K-values. of temperature steps as 1. Type in the comments “Phase properties as a function of Pressure”. Input the reservoir temperature as 180 deg F (for Dry Gas). Create plots of phase properties vs. etc. temperature step as 0 and No. volatile oil and black oil. molecular weights. phase fractions. densities. Examples of properties which may be plotted are: Z-factors. 1 2 3 Case Dry Gas Wet gas Gas Condensate. Other cases will have differing temperatures 11.Figure 13: Example of Two-Phase Flash Calculation used in setting up Plots for Dry Gas. Volatile Oil & Black oil Plot Property Z compressibility factor Z compressibility factor Phase volume fraction. Z factor. K-values (y/x) 12 | P a g e . In the plot control tab of the two-phase calculation form select the properties depending on the case as follows: No. For all the oil cases. . Pres. and click OK (Figure 14). is 2000 psia and the Temp.xls”.12. add a single-stage separator calculation with separator pressure of 100 psia and separator temperature of 75 F. In order to do this add the Separator Calculation Insert Sep. is the same as in the file “Five Fluid Types Data. The final WinProp interface should look like Figure 15 for the Gaseous Cases. The oil cases will have a Separator Calculation added after the last Two-Phase Flash Calculation. (*Note this is to be done only for oil cases) Figure 14: Example of Separator Form for Black Oil 13. Click anywhere inside the table to allow you to click the button labeled Under Sat. make sure Pres. for the specific fluid type. 13 | P a g e . 15. and ‘blackoil. Repeat Steps 1 to 14 and build a dat file for other types of fluid and save them as ‘wetgas. 14 | P a g e . Save the WinProp file as ‘drygas. ‘volatileoil. ‘gascondensate.dat’ files respectively and then run.dat’. After running these jobs analyze the Simulation Results for the different cases.dat’.Figure 15: WinProp interface for modeling Dry Gas case 14. These are demonstrated in Figure 16 to 24.dat’ and Run it.dat’. Figure 16: 2-Phase P-T diagram for Dry Gas case Figure 17: Vapor Z factor for Dry gas case 15 | P a g e . Figure 18: 2-Phase P-T diagram for Wet Gas case Figure 19: Vapor Z factor for wet gas case 16 | P a g e . Figure 20: 2-Phase P-T diagram for Gas condensate case Figure 21: Phase volume fractions and Z factors for gas condensate 17 | P a g e . Figure 22: K value for gas condensate case Figure 23: 2-Phase P-T diagram for Volatile oil case 18 | P a g e . Figure 24: 2-Phase P-T diagram for Black oil case Additional Exercises For the black oil data case. 19 | P a g e . Go back to the Volume Shift tab again and click on Zero Volume Shift and save as 'blackoil1_volshift set to zero. These can be found at the bottom of the output file which can be opened in a text editor.dat' file. open Component Selection/Properties and click on Calculate Volume Shift button then save as 'blackoil1_volshift correlation value. To set volume shift to correlations. investigate the effect on the simulated separator calculation induced by changing the following parameters: Apply the volume shift correlations Set the hydrocarbon binary interaction parameters to zero Reduce the C7+ Pc by 20% 1.dat' file (Figure 25). Run both data files and compare the results of the Separator calculations. 10 Separator output with Volshift set to correlation value: Oil FVF = vol of saturated oil at 2861.0 deg F per vol of stock tank oil at STC(4) = 1.0 deg F per vol of stock tank oil at STC(4) = 1.145 API gravity of stock tank oil at STC(4) = 24.111 API gravity of stock tank oil at STC(4) = 58.Figure 25: Calculate volume shift values The Separator Calculations should look like to the following outputs: Separator output with Volshift set to zero: Oil FVF = vol of saturated oil at 2861.76 20 | P a g e .95 psia and 170.95 psia and 170. 2. tab (Figure 26) and click on “HC-HC Groups / Apply value to multiple non HC-HC pairs…”. Save as 'blackoil1_int_coeff_zero.dat' and Run the model. It should appear as follows: Oil FVF = vol of saturated oil at 2014. Coef.16 Figure 26: Int. Open ‘blackoil.115 API gravity of stock tank oil at STC(4) = 58. Check on HC-HC and change Exponent value to zero (Figure 27).47 psia and 170. Do this by clicking on Component Selection/Properties. click on the Int. Coef.0 deg F per vol of stock tank oil at STC(4)= 1. Tab under Component Selection 21 | P a g e .dat’ again and set hydrocarbon binary interaction parameter to zero. and press OK. Observe the result from the Separator calculation in the output file. Save as 'blackoil1_int_coeff_reduce_Pc. Setting HC-HC Exponent to Zero 3.dat' and Run it.103 API gravity of stock tank oil at STC(4) = 104.36 click Apply Change (Figure 28). Change the Critical Pressure of the heaviest component to see its effects.81 22 | P a g e . It should appear as follows: Oil FVF = vol of saturated oil at 1589.Figure 27: Step 17. in Component Selection/Properties change the Pc value of C7+ to 12. Observe the result from the Separator calculation in the output file.0 deg F per vol of stock tank oil at STC(4) = 1. To reduce the C7+ Pc by 20%.51 psia and 170. 36 atm 23 | P a g e .Figure 28: Changing the C7+ Component's Pc to 12. Figure 29: Exercise 2 Starting Parameters from Exercise 1 Black Oil Data 24 | P a g e .Exercise 2 – Determination of MMP and MME The purpose of this exercise is to utilize WinProp to determine the Minimum Miscibility Pressure (MMP) and Minimum Miscibility Enrichment (MME) for a rich gas injection into a reservoir. and Saturation Pressure (Figure 29). Addition of Injection Streams and Calculations 1.dat’ and Delete all of the calculations EXCEPT the Title/EOS/Units. Composition. Component Selection/Properties. Open the black oil data set from Exercise 1 ‘blackoil. This can lead to a decrease in viscosity and interfacial tension which can increase mobility. This is generally related to enhanced oil recovery techniques such as CO2 flooding where a gas is injected at a pressure sufficient to become miscible with the native hydrocarbon. To do this.3 C3 25.8 N2 1. Rename the form to be "Black Oil + N2" then hit OK (Figure 30).0 NC4 9. These will include the following compositions: Pure N2 Pure CO2 Dry gas (from Exercise 1) A rich gas stream with the composition (in mole %): CO2 1.6 C1 33. begin by opening the existing Composition Form. Under the second column labeled “Secondary” enter 100.3 NC5 0.00 into the box relating to N2.2 IC5 2.4 IC4 3.3 2.1 C2 23.A variety of secondary injection streams will be added in order to determine their interactions with the native hydrocarbons. Figure 30: Addition of N2 Secondary Stream to Composition 25 | P a g e . 00 for CO2 and 0. 5. Repeat the Copy/Paste and set the forms up for Dry Gas (which you get the properties of from the “Five Fluid Types Data.00 for N2. Copy and Paste the new Component and 2-Phase Envelope Forms in the Menu so that you have two sets of them. Save this file as ‘blackoil_richgas_MMP_MME. In the second set change the Secondary stream to 100. The required forms and their arrangement of the calculation options in WinProp interface should look as shown in Figure 31 for this Exercise.dat’.3. Next add a 2-Phase Envelope calculation and Name it "N2 Injection”. 4. Rename the Component form and 2-Phase form.xls” excel file) and Rich Gas. Figure 31: Addition of solvents in black oil 26 | P a g e . Implement a multi-contact miscibility (MCM) calculation to determine the MMP for pure rich gas injection.6. Figure 32: Input data for calculation of MMP Figure 33: Rich gas (make-up gas) composition for calculation of MMP 27 | P a g e . Insert a Multiple Contacts calculation form by clicking on the Calculations drop down menu and going down to Multiple Contacts. Input the data shown in Figures 32 and 33. In the composition form the starting point for the make-up gas fraction is from 50%. Figure 34: Input data for calculation of MME calculation 28 | P a g e .OUT file CALCULATIONS AT TEMPERATURE = 170. Insert a new Multiple Contacts form and input the following parameters.Analyze the output file for results of single contact miscibility and multi-contact miscibility pressures and mole fraction of make-up gas: SUMMARY OF MULTIPLE CONTACT MISCIBILITY in *.10000E+01 MULTIPLE CONTACT MISCIBILITY ACHIEVED AT PRESSURE = 0.48250E+04 psia MAKE UP GAS MOLE FRACTION = 0. 1.37250E+04 psia MAKE UP GAS MOLE FRACTION = 0. Notice that in this case only one pressure value is used at which the miscibility is desired.CONDENSING GAS DRIVE Multi-Contact Miscibility Minimum Pressure Calculation Run a multi-contact miscibility calculation to determine the minimum amount of rich gas necessary to add to the dry gas to achieve miscibility at 4500 psi (MME calculation).000 deg F ______________________________________________ FIRST CONTACT MISCIBILITY ACHIEVED AT PRESSURE 0.10000E+01 BY BACKWARD CONTACTS . 45000E+04 psia MAKE UP GAS MOLE FRACTION = 0.Figure 35: Rich gas (make-up gas) composition for calculation of MME Analyze the output file for results of single contact miscibility and multi-contact miscibility pressures and mole fraction of make-up gas: SUMMARY OF RICH GAS MME CALCULATIONS AT TEMPERATURE = 170.90000E+00 psia BY BACKWARD CONTACTS .45000E+04 psia MULTIPLE CONTACT MISCIBILITY ACHIEVED AT PRESSURE = 0.000 deg F FIRST CONTACT MISCIBILITY PRESSURE (FCM) IS GREATER THAN 0.CONDENSING GAS DRIVE 29 | P a g e . 3. In the Titles/EOS/Units form insert a title: “Plus fraction characterization” and select PR (1978). 2. Separator Tests. N2. Figure 36: Black oil composition for Raleigh oil 30 | P a g e . and C1-C6 (DON'T ADD C7+) Under the Composition form add the compositions as given in the file: “Raleigh black oil-data1. This will be done on a new WinProp model. and feed as moles. In the Component Selection/Properties form add the following library components: CO2.Exercise 3 – Creation of Raleigh Black Oil The purpose of this exercise is to utilize WinProp in building a Black Oil fluid model. This exercise will introduce the concept of Plus Fraction Splitting of components and the tuning of component values and Equation of State to match laboratory experiments such as Constant Composition Expansion (CCE). and Differential Liberation (DL). Initialize WinProp through CMG launcher. Psia & deg F.xls”. Setup of WinProp model with Plus Fraction Splitting 1. Figure 38: Plus fraction splitting for Raleigh Oil Sample 1 Tab 31 | P a g e . 4 Pseudocomponents. On the General Tab specify Gamma distribution function.2891. Figure 37: Plus fraction splitting for Raleigh Oil General Tab 5. To add and split the C7+ fraction into pseudo-components select Composition then click Characterization|Plus Fraction Splitting. Make sure alpha is equal to 1. the first single carbon number in plus fraction as 7. SG+ as 0. Lumping Method as Gaussian Quadrature.4.8150. and leave the other properties as default. and Z+ (mole fraction of C7+ fraction) as 0. Go to Sample 1 Tab and input the MW+ as 190. Add Saturation Pressure. Differential liberation and separator test. Defining Calculations and Experimental Values 1. Input the experimental data given in the file “Raleigh black oil-data1.6. from another WinProp dataset by copy/pasting). Constant Composition Expansion. Figure 39: WinProp Forms Inserted in Step 7 32 | P a g e . You will now notice that 4 hypothetical pseudo components have been added in the components form. use the data given in the file “Raleigh black oil-data1. After running the data set. use the Update component properties in the File menu and delete Plus Fraction Splitting. (You can also input all above forms. and Differential Liberation forms in sequence. Separator. Save the data set as ‘raleigh oil_plus fraction splitting. In order to match the CCE. Save the dataset as ‘raleigh oil.xls”.dat’.dat’ and Run it.xls” (Figures 39-44). Figure 40: Saturation Pressure Form with Data from Excel File Figure 41: Constant Composition Expansion Form with Values for Pressure and Exp. ROV Copy/Pasted from Excel 33 | P a g e . Figure 42: Separator Form Populated with data from Excel file Figure 43: Experimental Tab of Separator Form Populated with Data from Excel file 34 | P a g e . Select Pc and Tc for the Heaviest Component.dat’ and Run it once to validate your model and check for errors in the input data. Select Differential Liberation then click on Regression Start on the top menu to place Regression Parameters after everything else. In the Component Selection/Properties form. click the “Calculate Volume Shift” Button and hit Apply Change to calculate the volume shifts using correlation values. Save your model as ‘raleigh oil_experimental data.Figure 44: Differential Liberation Pressure Levels Tab with Excel Data (entire excel table can be copied and pasted directly into this) 2. For all of the C7+ pseudocomponents and C1 select the volume shifts (Figure 45). Using Regression to Match WinProp model to Laboratory Results 3. In Regression Parameters go to the Component Properties tab. 35 | P a g e . Figure 46: Interaction Coefficients tab setting Hydrocarbon Interaction Coefficient Exponent 36 | P a g e .0E-06 in Regression Controls tab (Figure 47).Figure 45: Component Properties for experimental data matching In the Interactions Coefficients tab. select the hydrocarbon interaction coefficient exponent (Figure 46). Set the convergence tolerance to 1. Figure 47: Regression Control tab displaying where to change the Convergence tolerance 4. Figure 48: WinProp Calculations Layout including Regression Parameters 37 | P a g e . Do this for both Constant Composition Expansion and Saturation Pressure as well. Your window should now look like Figure 48. and then click on Regression Parameters and Paste into Reg-Block. Select Separator and Delete/Cut then click on Regression Parameters and Paste into Reg-Block. Run and check for errors in the output file. Select Differential Liberation and Delete/Cut. 0 in the Saturation Pressure form.0. Try setting the weight for the API gravity to 5. temporarily exclude the Saturation Pressure.5. After completing the match to the PVT data. you may have to change the lower and upper bounds of the regression parameters depending on whether these bounds are reached during the regression. Constant Composition Expansion and Separator calculations from the data set by right-clicking on each option and select Exclude from the pop-up menu (Figure 50). Re-run the regression. 10. 7. Adjust the weight of some key experimental data points. In this case the following bounds were used: Figure 49: Variable bounds used during the regression Analyze the *.dat’ in preparation for viscosity matching. and in the Differential Liberation form set the API gravity at STD conditions to 0. 38 | P a g e . 6.0 in the Separator -> Experimental Data tab.out file and refer to the Summary of Regression Results for comparison of the experimental versus calculated values. Matching Viscosity in WinProp to Laboratory Values 1. For viscosity matching. Update component properties and Save the file under a new name as ‘raleigh oil_experimental data_vis. In some cases. 0.Figure 50: WinProp Calculations with Exclusions as per Step 15 2. Figure 51: Differential Liberation with Weighting Factors of everything except Viscosity set to 0 39 | P a g e . and all other weights to 0. In Differential Liberation set the weight for the viscosity data to 1.0 (Figure 51). Select Regression Parameters and Delete/Cut. After completing the match to the viscosity data. In Regression Parameters remove all previously selected parameters from the Component Properties and Interaction Coefficients tab.dat’ in preparation for generating the IMEX PVT table. Check for errors in the output file. On the Viscosity Parameters tab select C1 and the C7+ pseudo components as regression variables (Figure 52). Run the data set. Now select the bottommost calculation form and Add After -> Simulator PVT -> Black Oil PVT Data (Figure 53). Defining an IMEX Fluid Model Output 1. Update component properties and Save the file under a new name ‘raleigh oil_Blackoil PVT. Figure 52: Viscosity Regression Parameters for C1 and C7+ Pseudo-Components 4.3. Constant Composition Expansion and Separator options should still be on the side bar. right-click on each and choose Include from the pop-up menu. 40 | P a g e . The Saturation Pressure. Enter mole fractions of 0.3 for the swelling data (Figure 55). 0.1. enter the saturation pressure data.2. desired pressure levels and the separator data (Figure 54). In Black Oil PVT Data.Figure 53: WinProp Calculations Layout for Step 19 2. Figure 54: Black oil PVT export for IMEX Saturation Pressure Tab Inputs 41 | P a g e . and 0. Figure 55: Pressure levels for back oil PVT Figure 56: Water properties for back oil PVT 42 | P a g e . Run the data set and check the output file.dat file in Textpad Search for the keyword JSAT-SWEL Make sure that the numbers on the line directly below are only integers (it should be 2 instead of 2. 43 | P a g e .3.0) Save the file and run the data set again. and then select “Use solution gas composition…” for the swelling fluid specification on the Gas Properties tab. Leave the Oil Properties controls at the defaults. The messages should be cleared. If you see the following messages in the output file: Then do the following: Open the *. 4. Open WinProp through CMG launcher. such models will be used in STARS for thermal applications. Open the Composition form and add the composition for C1 as given in the file “Heavy Oil for STARS-Data1. and feed as moles.08223). The first single carbon number in plus fraction should be 6. Setup of WinProp model with Plus Fraction Splitting 1. Figure 57: Plus Fraction Splitting for Heavy Oil 44 | P a g e . 2. In the Component Selection/Properties add the library component C1. In the Titles/EOS/Units form insert a title: “Fluid Model for STARS” and select PR (1978). Because of this thermal properties may play a larger role than observed in Black-Oil fluid models (such as Exercise 3). insert a Plus fraction Splitting form in the WinProp interface after the Composition form. Commonly. 3. The laboratory has supplied a C6+ component which now needs to be split into pseudocomponents.Exercise 4 – Heavy Oil Fluid Model The purpose of this exercise is to utilize WinProp in building a Heavy Oil Model. In order to split the C6+ fractions. Specify the number of Pseudo-components to 4 and select Gamma. (The mole fraction of C1 is 0. and Lee-Kesler (Figure 57). including matching laboratory data. Gaussian Quadrature. such as Plus Fraction Splitting. This fluid model will be created by incorporating similar techniques implemented in Exercise 3.xls”. kPa & deg C. as well as some new concepts. input SG+ as 0.5. 45 | P a g e . Figure 58: Plus fraction splitting for Heavy Oil 6. Update component properties and Save the data set as ‘S2-regression psat. In the Sample 1 tab. After running the data set. You will now notice that 4 hypothetical pseudo components have been added in the components form. Save the dataset as ‘S1-char.dat’ and Run it.989 and the global mole fractions and molecular weights for liquid component as given in the file “Heavy Oil for STARS-Data. Add a Saturation Pressure form (Figure 59).dat’.xls” (Figure 58). 1.Figure 59: Saturation Pressure Calculation added per Step 6 Matching of WinProp Model to Laboratory Results Due to splitting the component into 4 pseudocomponents a regression/tuning must be performed to match the WinProp model to the experimental data. Update component properties and Save the data set as ‘S3-lumping. Then select Saturation Pressure and Delete/Cut and click Regression Parameters and Paste into Reg-Block.dat’. 2. than add a Component Lumping form and lump the last three heavy components by highlighting all three then selecting the bottom-most component. Delete Plus Faction Splitting. After running the dataset. The Component Lumping form should look like Figure 60. On the Regression Parameters form. Run the dataset. The first experimental value to match is the Saturation Pressure. select Pc and Tc for the heaviest pseudocomponent. Delete Regression Parameters. In the Interactions Coefficients tab select the hydrocarbon interaction coefficient exponent. and then add Regression Parameters below Composition. 46 | P a g e . Then select Saturation Pressure and Delete/Cut and click Regression Parameters and Paste into Reg-Block. GOR and API data from “Heavy Oil for STARS-Data1. reservoir temperature. Run the dataset. Delete Component Lumping and add Regression Parameters.xls” (Figures 61-63). Select Regression Parameters and Add into Reg-Block -> Lab -> Separator. Figure 61: Saturation Pressure Form Populated with Excel Values 47 | P a g e .dat’. Update component properties and Save the data set as ‘S4-regression.Figure 60: Component Lumping form for Heavy Oil 3. After running the dataset. Enter saturation pressure. 4. Figure 62: Separator Form Populated with values from Excel File Figure 63: Separator Form Experimental Tab Populated with Excel Values 48 | P a g e . 1. Update component properties and Save the data set as ‘S5-regression_visc. Insert 2 Two Phase Flash forms to input experimental viscosity data (Figures 65 and 66) Figure 65: Two-Phase Flash Calculations for viscosity data of Heavy Oil (10 deg) 49 | P a g e . shift for the 2 Heaviest components. After running the dataset.5. Check for match in regression summary. In Regression Parameters under the Component Properties tab select Pc and Tc for the Heaviest component. and Vol. Figure 64: Regression Parameters Set per Step 11 Matching of WinProp Model Viscosity to Laboratory Viscosity We will repeat the regression to match Viscosity at 10 deg C (Figures 65 and 66) and 100 deg C (Figures 67 and 68) as given in “Heavy Oil for STARS-Data.xls”.dat’. Run the dataset. Figure 66: Two-Phase Flash Experimental Data viscosity of Heavy Oil (10 deg) Figure 67: Two-Phase Flash Calculations viscosity data of Heavy Oil (100 deg) 50 | P a g e . You may have to change variable bounds to improve the match.dat’. Viscosity Parameters tab. (Figure 69). select all check boxes. When an acceptable match has been found Update component properties and Save the data set as ‘S6-STARS PVT. In Regression Parameters. After running the dataset. In Component Selection/Properties on the Viscosity tab. Run the dataset. set viscosity model type to Pedersen Corresponding State Model and the corresponding states model to Modified Pedersen (1987). 51 | P a g e . check for a match.Figure 68: Two-Phase Flash Experimental Data viscosity of Heavy Oil (100 deg) 2. 2. upper pressure at 5500 kPa and number of steps as 10. Type tab select “Basic STARS PVT Data”. on the Calc. 52 | P a g e . On the first CMG STARS PVT Data form. Set lower pressure at 500 kPa. Delete Regression Parameters then insert 2 CMG STARS PVT Data forms from the Simulator PVT drop down menu. Generate a Component liquid viscosity table from 10 C to 360 C with 8 steps and use the WinProp viscosity model (Figure 70). Then on the Basic PVT tab enter the initial reservoir conditions (3200 kPa and 12 C) as the reference conditions.Figure 69: Viscosity Component Definition Tab showing changes to Modified Pedersen Creating a STARS PVT Model from WinProp 1. Entering a minimum K-value threshold of 1. of temperature steps.” On the K-Value tab enter 500 kPa for both the Pressure and Pressure Step and 11 for the No. 53 | P a g e . 50 C for Temperature Step. This option sets any KValue less than this threshold to 0. On the second CMG STARS PVT Data form.Figure 70: STARS PVT Data Generator with Initial Reservoir Conditions 3.0E-06 will improve STARS numerical stability without materially affecting the simulation results (Figure 71). on the Calc. of pressure steps. and 8 for No. Type tab select “Gas-Liquid Kvalue Tables. Also enter 10 C for Temperature. 54 | P a g e . The information obtained is now capable of being imported to a STARS dataset and Ran.Figure 71: STARS PVT Data Generator K-Value Data Entries 4. Save the dataset under a new name and Run it.
Comments
Report "PBM and PVT Creation Using WinProp Tutorial"