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INSTITUTE OF PETROLEUM ENGINEERING RESERVOIR MANAGEMENT THERMODYNAMICS THERMODYNAMICS AND PHASE BEHAVIOR – W6104
Term Project Final Report ZAKARIYA YOUSEF ABU GRIN St.Num: 451369 3/2/2015
Ref: Gyulay, 1967
In this project, full PVT data is given to be simulated using EOS model in PVT Package IPM software. The full composition was grouped into 30 components then lumped to 6. The phase envelope has not been affected by reducing the components number for Psat matched matched by BIC’s models, while large changes are noted for Psat matched by Tc-Pc- AF models. Afterwards, Psat matched by BIC’s models showed superior match with lab data (CCE and DLE). Final tuning has been achieved for lab data including separator test with a maximum AAE≅5%. In these tunings, suitable weighting factors were allocated, volume shift was also implemented to enhance initial EOS results and density calculations. Pseudo components properties were used as re gression parameters in a small range (0.9-1.1).
Term Project March 2, 2015
Contents 1. 2.
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Introduction ............................ .......................................... ............................ ............................ ............................ ............................. ............................. ............................ ..........................2 ............2 Task (a) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. ......................3 .......3 2.1 Composition Composition Input.................. Input................................ ............................ ............................ ............................. ............................. ............................ ............................ ...................3 .....3 2.2 Grouping Grouping ........................... .......................................... ............................. ............................ ............................ ............................ ............................ ............................ ........................5 ..........5 2.3 Entering Lab Saturation Pressure, Density and Tuning .................................................................7 3. Task (b) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. .................... .....10 4. Task (c) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. .................... .....12 3. Task (d) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. .................... .....14 5. Task (e) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. .................... .....16 6. Task (f) ........................... ......................................... ............................ ............................ ............................ ............................ ............................ ............................ ............................. .................... .....19 7. References.. References................ ............................ ............................ ............................ ............................ ............................ ............................ ............................ ............................. ........................... ............22 8. Appendix Appendix A ............................ .......................................... ............................ ............................ ............................ ............................ ............................ ............................ ........................... .............23 9. Appendix Appendix B ............................ .......................................... ............................ ............................ ............................ ............................ ............................ ............................ ........................... .............24
Figures Figure 1: Adding components to the database. ................................................................................................3 Figure 2: Entering the composition as table. ...................................................................................................3 Figure 3: Entering pseudo component Mw......................................................................................................4 Figure 4: Entering pseudo component properties. ...........................................................................................4 Figure 5:Calculating Psat and API using EOS. ...............................................................................................5 Figure 6:Grouping approach. ...........................................................................................................................6 Figure 7: Grouping heavy components. ........... .......... ........... .......... ........... .......... .......... ........... .......... ........... ..6 Figure 8: Entering lab data – data – Psat............................. .......................................... ............................ ............................ ............................ ............................. ............................ ................7 ...7 Figure 9: Regression for matching Psat. ..........................................................................................................7 Figure 10: Choosing EOS regression parameters for pseudo components. .....................................................8 Figure 11: Regression tab options. ..................................................................................................................8 Figure 12: Matching Psat using BIC’s pseudo components. ........................... .......................................... ............................. ............................ ...................9 .....9 Figure 13: Matching density density separately using Vsh. .......... ........... .......... .......... ........... .......... ........... .......... ......9 Figure 14: 30 components composition phase behavior for different matched P sat models. ............... ......... 10 Figure 15: Lumping the original composition to 6 components. components. ........... .......... ........... .......... ........... .......... .... 10 Figure 16: 6 component lumped composition phase behavior for different matched P sat models. ........... .... 11 Figure 17: Naming fluid models. ................................................................................................................... 11 Figure 18: 30 component and lumped composition phase behavior for different matched Psat models. ...... 12 Figure 19: Entering CCE lab data. ................................................................................................................. 12 Figure 20: Entering CCE lab data points for EOS calculations. .......... ........... .......... ........... .......... ........... ..... 13 Figure 21: The difference between the experimental results and EOS model. ................ ........... .......... ......... 13 Figure 22: Entering DLE lab data. ................................................................................................................. 14 Figure 23: Entering DLE lab data points for EOS calculations ......... ........... .......... ........... .......... ........... ....... 14 Figure 24: The difference between DLE lab data and and EOS results. ................ ........... .......... ........... .......... .... 16 Figure 25: Entering SEP temperature and pressure. ........... .......... ........... .......... ........... .......... ........... .......... .. 16 Figure 26: EOS separator results. ........... .......... ........... .......... ........... .......... ........... .......... ........... .......... ......... 17 Figure 27: Entering separator separator test data. ........... .......... ........... .......... ........... .......... .......... ........... .......... ........... 17 Figure 28: Export data window. ........... ........... .......... ........... .......... ........... .......... .......... ........... .......... ........... 19 Figure 29: Export data option. ....................................................................................................................... 19
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Term Project March 2, 2015
2. Task (a) 2.1 Composition Input 1.
Some components are not included in the database such as Benzene, Toluene. A new database “user database” is needed for such task in PVTP. Database in the main bar menu is simply used to create and edit the database. The most important data is entered manually in this table as shown next graph.
Figure 1: Adding components to the database.
2.
Open “ ” or Data >> Enter composition as table to enter the composition as reported in the spreadsheet, then Verify button is used to link the components with the database. Finally, Enter Composition is pressed.
Figure 2: Entering the composition as table.
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Term Project March 2, 2015 As more information is required, another window is opened, reference data represents sampling conditions and C+ (Pseudo component) Mw are entered.
Figure 3: Entering pseudo component Mw.
Pseudo Props button is pressed to enter C+ data “Mw, SG, Tb”. Calc Values is used to calculate C+ properties using its Mw and SG. Auto Match is pressed to match EOS density at standard condition, with empirical correlations (Standing-Katz or Costald) that are proven to be reliable references, using pseudo component properties, Change button can be used for more options. Store then Use Original Pseudo Props from store . Advanced button is used for splitting techniques.
Figure 4: Entering pseudo component properties.
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Term Project March 2, 2015
Exit and Save button is pressed for the two windows to save data and close. This composition saved as wellstream (1).
3.
Some properties can be calculated by EOS such as Psat and API° using “ ” or Data >> View Properties, windows for Quick Calc and Oil Properties buttons are shown below. For this 30 component composition, Psat =1201 psia at 122 deg F, and API°= 73.8048.
Figure 5:Calculating Psat and API using EOS.
2.2 Grouping 1. Since just 30 components are required in this task, some heavy component will be lumped using 1 Whitson method as following:
= [1 + 3.3 log( − )] → = [1 + 3.3 log(30 − 14)] = 5 ⁄ 580 ⁄ = ( ) → = 190( ) → = 190(3.0526) ⁄ 190
Group#, i 1 2 3 4 5
Upper Mi 238 297 371 464 580
Components in Group C14 C17 C18 C21 C22 C26 C27 C29 C30+ C30+
This method is used to represent the C7+ fraction of a mixture, which should contain more than C20+, into few pseudo components.
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Term Project March 2, 2015
2. Grouping technique can be done in PVTP using “ is pressed.
” or Data >> Grouping, and then Group button
Figure 6:Grouping approach.
Another window will pop-up, all components are added as a single component group excluding the components that were chosen to be in groups, which will be grouped in 5 multi-component groups as indicated. Then click OK and Exit and Save.
Figure 7: Grouping heavy components.
3. After applying grouping, the properties changed slightly. Psat= 1207 psi and API°= 72.7164. This composition saved as wellstream (2).
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Term Project March 2, 2015
2.3 Entering Lab Saturation Pressure, Density and Tuning 1. Lab data can be entered using “ ” or Data >> Enter Lab Data . The reported saturation pressure at Tres (psat= 1650 psia and Dsat = 0.765 gm/cc at 50° C = 122 F) is entered as shown below. Since it is recommended to give 40 weighting factor to Psat, note that saturation pressure has been given a high weighting factor due to its significant important in any tuning process.
Figure 8: Entering lab data – Psat. 2 Note: EOS usually predicts saturation pressure with ± 10% error . Since heaviest pseudo component properties are the least reliable data, it will be used as tuning parameters. For better EOS initial prediction, Volume Shift is impl emented. All pure component properties will be excluded from tuning.
2. Tuning or Regression process can be done in PVTP using “ ” or Data >> Regression. Several models are available; all models may result matching although the second one is not recommended. After choosing the suitable type, Regress button is pressed.
Figure 9: Regression for matching Psat.
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Term Project March 2, 2015 Regress window will open for matching properties selection and options. For better EOS initial prediction, Volume Shift is implemented.
Figure 10: Choosing EOS regression parameters for pseudo components.
Change button can be used to choose some important options. In regression tab, pure component can be excluded from tuning. However, pure component will not be chosen. Multipliers limit can also be entered for BICs and properties used in tuning. Since small tuning is recommended small range is used (0.9 – 1.1).
Figure 11: Regression tab options.
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Term Project March 2, 2015 Since it is usually recommended to choose the most effective and the least number of parameters, EOS parameters will be tested separately. Firstly, saturation pressure was matched by just BIC’s for pseudo component from group 2 till C30+ and saved as wellstream (3).
Figure 12: Matching Psat using BIC’s pseudo components.
Secondly, for C30+ pseudo component, OmegaA alone was enough to match saturation pressure with small limit change (0.9 – 1.1), the same effect with Tc. Unfortunately, the phase behavior was misleading while th OmegaB and Pc have a moderate effect. Finally, the most suitable choice is to choose the 4 model and regress Psat using Tc Pc AF multipliers for pseudo component from group 2 till C30+ and saved as wellstream (4). For both saved choices density was matched separately using C30+ Vsh.
Figure 13: Matching density separately using Vsh.
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Term Project March 2, 2015 This table illustrates the chosen parameters which give matched results and proper phase behavior. WellStream
Comp Num
1 2 3 4
42 30 30 30
Saturation Pressure Density Psat, psi Matched by for Dsat, gm/cc Matched by 1200.8 1207 1650 BIC's G2 to C30+ 0.765 Vsh 1650 Mult Tc Pc AF G2 to C30+ 0.765 Vsh
for C30+ C30+
APIº 46.1704 45.3823 37.3983 40.2461
3. Phase envelope is drawn for both matched composition wellstream 3 and 4. Note the intersect between the two phase behaviors was exactly at saturation pressure, which indicate several matching choices for Psat, but the most suitable one that can match the other lab data more accurate,
Figure 14: 30 components composition phase behavior for different matched Psat models.
3. Task (b) 1.
Lumping the composition to 6 components can be obtained from the original fluid description. Using Data >> Lumping|Delumping for IPM. Lumping window will open then Lump stream, components are chosen for each lumped group. Lump is pressed then To Stream to apply the lumping process.
Figure 15: Lumping the original composition to 6 components.
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Term Project March 2, 2015 The components were lumped as following: Group.Num 1 2 3 4 5 6
2.
Components in Group N2+C1 CO2+C2 C3+iC4+nC4 iC5+nC5+C6+Methylcyclopenta+Benzene+Cyclohexane C7+Methylcyclohexa+Toluene+C8+Ethylbenzene+M-&P-Xyl+C10→C17 C18+C19+C20+C21+C22+C23+C24+C25+C26+C27+C28+C29+C30+
This lumped fluid has been matched throughout the last pseudo component (Group 6) by two ways, the first using BIC’s (by the value 0.1779144 between group 1 and 6) and the second using Tc, Pc AF. As mentioned before density is matched separately using Vsh for the last pseudo component. Next figure shows the different between the two options.
Figure 16: 6 component lumped composition phase behavior for different matched Psat models.
3.
Since more than one fluid may be confused with the current PVTP file, the fluids are renamed using “
” by described names as following:
Figure 17: Naming fluid models.
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Term Project March 2, 2015
4.
P-T Phase behavior diagram can be obtained using “ ” or Calculation >> Phase Envelope. Fluids can be chosen from the left side menu, and then Calc is pressed. Set Test Pts. button is used to add the saturation pressure in the diagram. After choosing the required fluids, Expand button is pressed.
Figure 18: 30 component and lumped composition phase behavior for different matched Psat models.
Although all fluid models match the bubble point at 1650 psi, different phase envelopes were generated, except the ones which were matched using BIC’s. Hence, reducing the components number does not have an effect on the phase envelope for saturation pre ssure matched by BIC’s, while big change may exist for the saturation pressure matched by Tc, Pc, and AF.
4. Task (c) 1.
All experiment data can be entered using “ ” or Data >> Enter Lab Data , CCE for the Psat matched fluids are chosen. Enter temperature and pressure with relative volume. It is not necessary to enter the temperature for each point because CCE is isothermal experiment. OK is pressed.
Figure 19: Entering CCE lab data.
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Term Project March 2, 2015 Note: Semi medium weighting factor (around 5) has been introduced for CCE volume relation as recommended in different PVT textbooks. Weighting factor allocation can be done by selecting the cell (single weighting factor) or all cells (globule weighting factor) for data (relative volume) in the previews window and press Set Weighting. Data will appear with different colure (Blue).
2.
After adding lab data, CCE experiment can be simulated by EOS using “ ” or Calculation >> Constant Composition Expansion. To simulate CCE experiment exactly at the same lab data points User Selected option is chosen. Here the data is entered in each 10 rows, in this case just the first 2 columns is used. Required fluid models are also chosen. Then Calc is pressed.
Figure 20: Entering CCE lab data points for EOS calculations.
Another window will open to show the results after Calc is pressed again. Lab data (observation data) and calculated data (simulated data by EOS) can be compared using plot button. Relative volume relation is chosen from variables in the main bar menu in the plot window.
Figure 21: The difference between the experimental results and EOS model.
CCE data is matched without any regression for both 6 components fluid models (AAE=0.51% for 6 Comp matched by BIC’s and 0.36% for 6 Comp matched by Tc, Pc, AF) , which indicates the reliability of both lab data and the used EOS models. 13
Term Project March 2, 2015
3. Task (d)
1.
DLE data is also entered using “ ”. Enter temperature, pressure, solution GOR “Rsd”, oil FVF “Bod”, Oil density, and oil viscosity “μo”. It is not necessary to enter the temperature for each point because DLE is isothermal experiment. OK is pressed.
Figure 22: Entering DLE lab data.
Note: Medium weighting factor (5) has been introduced for density, from 1 to 3 for GORd and Bod, and 1 for viscosity as recommended in different PVT textbooks (Ali Danesh 1, Whitson3). Oil density was excluded from regression, because it is matched using just CCE.
Oil Viscosity at DLE pressure points were enterpolated.
2.
After adding lab data, DLE experiment can be simulated by EOS using “ ” or Calculation >> Differential Expansion. To simulate DLE experiment exactly at the same lab data points, User Selected option is chosen. Required fluid models are also chosen. Then Calc is pressed twice.
Figure 23: Entering DLE lab data points for EOS calculations
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Term Project March 2, 2015 Another window will open to show the results after Calc is pressed again. Lab data (observation data) and calculated data (simulated data by EOS) can be compared by calculating AAE%. Initial results were not bad, slight tuning is needed to match GOR. Both fluid models have shown near results. AAE % - 6Comp Matched by BIC's
AAE % - 6Comp Matched by Tc, Pc, AF
Points Gas Oil Ratio Oil FVF Oil Density Z Factor (Vapour) n ABS. Error ABS. Error ABS. Error ABS. Error
Points Gas Oil Ratio Oil FVF Oil Density Z Factor (Vapour) n ABS. Error ABS. Error ABS. Error ABS. Error
1 2 3 4 5 6 Sum Error%
3.
0.0976 0.0925 0.1579 0.2675 0.4397
0.0226 0.0219 0.0327 0.0379 0.0334 0.0203
0.0001 0.0004 0.0113 0.0174 0.0133 0.0063
0.0021 0.0087 0.0073 0.0065 0.0081
1.0553 21.11%
0.1688 2.81%
0.0488 0.81%
0.0327 0.65%
1 2 3 4 5 6 Sum Error%
0.1034 0.0968 0.1590 0.2636 0.4298
0.0341 0.0317 0.0403 0.0438 0.0385 0.0252
0.0001 0.0014 0.0072 0.0114 0.0062 0.0014
0.0034 0.0096 0.0079 0.0070 0.0085
1.0527 21.05%
0.2136 3.56%
0.0276 0.46%
0.0363 0.73%
Since tuning is required, DLE and CCE data is matched again using the weighting factors as mentioned before. Oil density and viscosity are matched separately using Vsh and Vcrit respectively. In this tuning, EOS parameters just for pseudo components were used in a small range limit (0.9-1.1). st
For the 1 model (6 Comp Psat matched by BIC’s), lab data was matched accurately using Tc, Pc, AF and BIC (1st model in regression) for the last two pseudo components. Then Oil density at saturation pressure from CCE is matched separately using the last pseudo component Vsh (without including DLE oil density). For DLE, AAE% was as following: AAE % - 6Comp Matched by BIC's Points n
Gas Oil Ratio Oil FVF Oil Density Z Factor (Vapour) Oil Viscosity ABS. Error ABS. Error ABS. Error ABS. Error ABS. Error
1 2 3 4 5 6 Sum Error%
0.0002 0.0287 0.0082 0.0010 0.0016
0.0029 0.0019 0.0112 0.0188 0.0165 0.0188
0.0000 0.0004 0.0115 0.0179 0.0135 0.0027
0.0225 0.0202 0.0146 0.0130 0.0188
0.0015 0.0038 0.0028 0.0084 0.0086 0.0150
0.0398 0.80%
0.0701 1.17%
0.0460 0.77%
0.0891 1.78%
0.0403 0.67%
Since other different methods are available for viscosity calculation, Little Kennedy was chosen instead of Pederson to enhance viscosity calculations to low AAE (0.67% instead of 4.09%). While CCE is kept matched (AAE=0.62%). nd
While for the 2 model (6Comp Psat matched by mult Tc,Pc,AF), lab data were matched using multiplier Tc, Pc, AF for the two last pseudo component with low weighting factor for GOR. Density and viscosity were matched by the last pseudo components using Vsh and Vcrit respectively. Little Kennedy correlation was chosen for viscosity. AAE % - 6Comp Matched by Tc, Pc, AF Points n 1 2 3 4 5 6 Sum Error%
Gas Oil Ratio Oil FVF Oil Density Z Factor (Vapour) Oil Viscosity ABS. Error ABS. Error ABS. Error ABS. Error ABS. Error 0.0934 0.0881 0.1518 0.2511 0.4051
0.0297 0.0283 0.0378 0.0416 0.0366 0.0244
0.0001 0.0007 0.0084 0.0129 0.0078 0.0002
0.0077 0.0117 0.0090 0.0079 0.0099
0.0010 0.0036 0.0005 0.0051 0.0052 0.0082
0.9894 19.79%
0.1982 3.30%
0.0301 0.50%
0.0462 0.92%
0.0236 0.39%
Since the 1st model is more accurate, this model will be chosen. Hence matching saturation pressure using BIC’s for pseudo component is recommended as a first tuning step. 15
Term Project March 2, 2015
4.
First model shows accurate results comparing with lab results. These plots show the difference between lab data and EOS results.
Figure 24: The difference between DLE lab data and EOS results.
5. Task (e) 1.
Separator test can be simulated using EOS by “ ” or Calculation >> Separator to calculate separator GOR (RsSb) and BoSb at each separator stage. Enter temperature and pressure values and press Calc.
Figure 25: Entering SEP temperature and pressure.
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Term Project March 2, 2015 2.
Another window appears to show the results, press Calc. Repeat the last steps for the other stations to see the different from lab data and EOS results.
Figure 26: EOS separator results.
3.
4.
Lab data shows the optimum separator condition at 233-15 psi and 40-27 Cº respectively, while EOS model shows the second separator stage as the optimum condition at 160-15 psi and 40-27 Cº. However, lab data should always be used as reference guide line. AAE% for all experiment shows that RsSb needs to be matched. In this final matching, oil FVF and oil density in separator test will be excluded because they are already matched in DLE. AAE % - 6Comp Matched by BIC's Points n 1 2 3 4 5
DLE Gas Oi l Rati o A BS . E rr or
5.
CCE
Oi l De ns ity Z F acto r ( Vap our ) Oi l V is co si ty
A BS . E rr or A BS . E rr or 0.0000 0.0004 0.0115 0.0179 0.0135
A BS . E rr or
0.0002 0.0287 0.0082 0.0010 0.0016
0.0029 0.0019 0.0112 0.0188 0.0165 0.0188
0.0027
0.0188
0.0398 0.80%
0.0701 1.17%
0.0460 0.77%
0.0891 1.78%
6 Sum Error%
O il F VF
0.0225 0.0202 0.0146 0.0130
A BS . E rr or 0.0015 0.0038 0.0028 0.0084 0.0086
Separator test
Re l. Vo l
Rs Sb
BoS b
A BS . E rr or
A BS . E rr or
A BS . E rr or
O il De ns A BS . E rr or
-
-
-
-
0.0150
-
-
-
-
0.0403 0.67%
0.0927 0.62%
-
-
8.19%
0.83%
1.07%
Separator data is also entered using “ ”. Enter separator temperature, pressure, solution GOR “RsSb”, oil FVF “BoSb”, Oil and gas density. OK is pressed. Note that oil FVF and oil density are excluded from tuning (Bo is matched throughout DLE and oil density throughout CCE).
Figure 27: Entering separator test data.
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Term Project March 2, 2015 6.
Separator data with CCE and DLE were matched together, using Original Tc, Pc, AF and Vsh for the last two pseudo component (with no limit). The viscosity is matched separately by Vcrit for just the last pseudo component. AAE% was accepted for all simulated results. Next table shows the results: AAE % - 6Comp Psat Matched by BIC's DLE
Points
Gas Oi l Rati o
n
ABS. Error
Oi l FV F
CCE
Oi l De nsi ty Z F actor ( Vapour) Oi l V is cos ity
ABS. Error ABS. Error
ABS. Error
Separator test
Re l. Vol
ABS. Error ABS. Error
Rs Sb
BoSb
Oi l De ns
ABS. Error
ABS. Error
ABS. Error
1
0.0031
0.0046
0.0103
0.0034
-
-
-
-
2
0.0362
0.0040
0.0118
0.0349
0.0024
-
-
-
-
3
0.0258
0.0162
0.0021
0.0258
0.0048
-
-
-
-
4
0.0372
0.0231
0.0030
0.0176
0.0085
-
-
-
-
5
0.0687
0.0203
0.0023
0.0155
0.0067
-
-
-
-
0.0212
0.0182
0.0227
0.0145
-
-
-
-
Sum
0.1710
0.0894
0.0478
0.1166
0.0403
0.1002
-
-
-
Error%
3.42%
1.49%
0.80%
2.33%
0.67%
0.67%
6
7.
4.98%
0.95%
The solution gas-oil ratio and FVF data can be adjusted to the separator as following:
Adjustment of the Differential Liberation Data to Separator Condition t Te mp s e T deg F
Pressure psia
Rel.Vol -
Core ction factor
Adjuste d Oil FVF Test Gas Oil Ratio (bbl/STB) (sm3/sm3)
Adjusted Gas Oil Ratio (sm3/sm3)
Test Total FVF (bbl/STB)
T 220
-
Vrel (CCE) farc
BoSb (bbl/STB)
Bo = Vrel x BoSb (bbl/STB)
-
Rs = RsSb Rs = Optimum Sep GOR
-
Pb
9000 5000 4000 3500 3000 2500 2000 1900 1800 1700 1650
1.101 1.126 1.134 1.139 1.144 1.150 1.155 1.157 1.158 1.159 1.160
-
T 220
-
Pb
1660 1200 700 300 100 15
b P > P t a a t a d E C C
b P < P t a a t a d E L D
BoSb RsSb BoDb RsDb
*
0.949354 0.970672 0.977887 0.981907 0.986251 0.990966 0.996109 0.997195 0.998302 0.99943 1
1.16 1.16 1.16 1.16 1.16 1.16 1.16 1.16 1.16 1.16 1.16
Bo D ( DLE) S od = B oD/ Bo Db Bo = S od x Bo Sb (bbl/STB) frac (bbl/STB) 1.16959 1.13539 1.09698 1.06581 1.04826 1. 01989
1 0.970758984 0.937918416 0.911268051 0.896262793 0. 87200643
54.6 54.6 54.6 54.6 54.6 54.6 54.6 54.6 54.6 54.6 54.6
Rs D ( DLE) (sm3/sm3)
1.160 1.126 1.088 1.057 1.040 1.000
Bt1 = Bo = Vrel x BoSb (bbl/STB)
-
54.6 40 23 10 3 0
1.17 1.31 1.78 3.41 9.35 65.17
bubble-point oil formation volume factor from the separator test, bbl of the bubble-point oil/STB (=1.474) bubble-point solution gas-oil ratio from the separator test, scf/STB (=768) differential relative oil volume factor at the bubblepoint pressure pb, psia, bbl/STB (=1.6) solution gas-oil at the bubble-point pressure as measured by the differential liberation test, scf/STB (=854) Red values are manually adjusted at atmospheric pressure. Bo=1 and Rs = 0.
1.18
70
1.16
60
B t2 = Bt D * Bo Sb / Bo Db Bt = BtD * 1.16 / 1.16959
9000 5000 4000 3500 3000 2500 2000 1900 1800 1700 1650
0.949354 0.970672 0.977887 0.981907 0.986251 0.990966 0.996109 0.997195 0.998302 0.99943 1
1500 1. 02994 1250 1.10418
1.160 1.303 1.761 3.383 9.278 64.639
1000 500
1.22874 1.93731
1.101 1.126 1.134 1.139 1.144 1.150 1.155 1.157 1.158 1.159 1.160 1. 195 B gD 1.281 cu ft/SCF
Bt 3= B o+( BgD /5. 615) (Rs b- Rs )*5. 61 (bbl/STB)
1.425 0 2.247 0.011796 0.021398 0.052288 0.16045 1.07258
1.160 1.303 1.761 3.383 9.278 59.511
Bt1 equal to Bo, which is calculated from CCE data and separator test data at Press below and above Pb Bt2 is calculated using DLE data and SEP data at Press below Pb (Corrected Bt) Bt3 is calculated using the adjusted DLE for SEP data at Press below Pb The differential shrinkage factor.
Bt1 Bt2 Bt3 Sod
Gas Oil Ratio
Total Formation Volume Factor 3.00 BtD=BoD+(BgD/5.615)(RsDb-RsD)*5.61 Adjusted Total FVF (CCE&DLE) Calculated Total FVF using just (CCE)
2.80 2.60
1.14 ) 3 m s / 3 m s (
1.12
, o B
Separator Test Data 54.6 (sm3/sm3) 1.16 (bbl/STB)
Pressure Vrel (CCE) Bt1 = Vrel * BoSb psia farc (bbl/STB)
1.101 1.126 1.134 1.139 1.144 1.150 1.155 1.157 1.158 1.159 1.160
Bt D=Bo D+( BgD/ 5. 615) (Rs Db -Rs D) *5. 61 (bbl/STB)
59.866 44.7286 28.1028 14.9786 8.0484 0
RsSb BoSb
Adjusted Total FVF (CCE&DLE) Calculated Total FVF using just (CCE) (bbl/STB)
R s = Rs Sb - ( Rs Db -R sD) (Bo Sb /Bo Db ) Rs = 54.6 - ( 59.86 - RsD ) ( 1.16 / 1.169 )
Oil Formation Volume Factor
B T S / B R
2.59%
1.1 1.08
, R O G
1.06 1.04
BoD (DLE)
1.02
50
2.40
40
B T S / B R , t B
30
2000
4000 Pressure, psi
6000
8000
10
10000
1.80
RsD (DLE)
1.40
Adjusted Gas Oil Ratio
1.20
0 0
2.00
1.60
20
Adjusted Oil FVF
1
2.20
1.00 0
200
400
600
800
1000
Pressure, psi
1200
1400
1600
1800
0
2000
4000
6000
8000
Pressure, psi
The adjustment were applied to EOS results (CCE and CVD) using both RsSb and BoSb, which obtained in optimum separator test condition. Input data in this spreadsheet is indicated in yellow.
18
10000
Term Project March 2, 2015 8.
Comparing the corrected Bo and Rs with the results from the Separator Corrected Differential Depletion Data (Lab), acceptable AAE% was found. Separator corrected Differential Depletion data Gas /Oil
Gas/ Oi l
Pressure Pressure Ratio (Lab) Ratio (EOS)
Format ion Volume
Format ion Volume
Correct ed
Rs
Factor (Lab)
Factor (EOS)
Bo
(bbl/stb) or (bbl/stb)
ABS. Error
(sm3/sm3) (sm3/sm3) ABS. Error (bbl/stb) or (bbl/stb)
(psi a)
Bar
5003.80 4003.04 3495.41
345 241
3002.28
207
2494.65 2001.52 1899.99
172
1798.47 1653.43 1203.81
124
696.18 304.58
48
101.53 AAE% :
Correct ed
54.6 54.6 54.6
54.6 54.6 54.6
0 0 0
1.131 1.139 1.142
54.6
54.6
0
1.146
1.144
0.00172
54.6 54.6 54.6
54.6 54.6 54.6
0 0 0
1.15 1.155 1.156
1.150 1.155 1.157
0.00036 0.00041 0.00065
54.6 54.6 37.8
54.6 54.6 39.7
0 0.0 0.05
1.158 1.16 1.125
1.158 1.16 1.126
0.00004 0.00000 0.00115
21
22.1 9.3
23.0 10.3
0.04 0.10
1.101 1.077
1.088 1.057
0.01217 0.01819
7
2.3
3.3
0.43
1.056
1.040
0.01533
276
138 131 114 83
4.80%
1.126 1.134 1.139
0.00446 0.00411 0.00258
0.47%
6. Task (f) 1.
Generating a compositional PVT data file for the ECLIPSE 300 reservoir simulator can be done from the main menu. File >> Export. Another window will appear, the export file type number 8 is chosen. Ok is pressed.
Figure 28: Export data window.
2.
Export data options window allowing to choose the units of export. Field unit is chosen
Figure 29: Export data option.
19
Term Project March 2, 2015 3.
PVO file was generated for E300 for 6 component matched model in a field unit:
-- Petroleum Experts - PVTp Export File ---- Export File Signature -- #PetexECL300 -- Export File Version -- #2 -- 2 has increased accuracy (no of decimal places) of output values -- UNITS --FIELD -- !!!!!!!!!!!!!!!!!! PVT FILE DETAILS !!!!!!!!!!!!!! -- PVT FILE NAME : 5_Term Project(C30+)AllMatched.pvi -- STREAM : 6Comp-Matched by BIC's -- Exported :Mon Mar 02 22:29:26 2015 -- !!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!! - NCOMPS 6/ EOS PR / -- Peng Robinson correction PRCORR -- Standard temperature and pressure in Deg F and PSIA STCOND 60.0200 14.6960 / -- Component names CNAMES N2C1 CO2C2 C3IC4NC4 IC5NC5C6METHY++ C7METHYLCYCLO++ C18C19C20C21C++ / -- Critical temperatures Deg R TCRIT 3.42921198e+002 5.49415125e+002 7.45389757e+002 9.24647325e+002 9.94765154e+002 1.82550301e+003 / -- Critical pressures PSIA PCRIT 6.72718384e+002 7.17500488e+002 5.52807129e+002 5.06895630e+002 4.02294067e+002 1.38930161e+002 / -- Critical volumes FT3/LBMOLE VCRIT 1.58868933e+000 2.35359621e+000 4.02083254e+000 5.32031965e+000 1.02359457e+001 2.24441814e+001 / -- Reservoir 3-Parameter EoS Shift Coefficients SSHIFT -1.53999999e-001 -1.00199997e-001 -7.05393329e-002 -2.17463728e-002 5.63572347e-001 -8.10160860e-003 / -- Critical volumes for LBC Viscosities FT3/LBMOLE VCRITVIS 1.58868933e+000 2.35359621e+000 4.02083254e+000 5.32031965e+000 1.02359457e+001 2.24441814e+001 / -- Acentric factors ACF 1.10554304e-002 1.02514647e-001 1.89455450e-001 2.54017651e-001 3.91309820e-002 1.18171144e+000 / -- Molecular Weights MW 1.60636978e+001 3.04492054e+001 5.64661255e+001 8.22998123e+001 1.49269562e+002 3.81107819e+002 / -- fluid sample composition ZI 3.15100789e-001 6.80842445e-003 4.66116450e-002 1.05275896e-001 3.80357166e-001 1.45846080e-001 / -- Boiling point temperatures Deg R TBOIL 2.00758135e+002 3.32736406e+002 4.76812227e+002 6.07030382e+002 8.28216082e+002 1.23133962e+003 / -- Reference temperatures Deg R TREF 5.19690000e+002 5.19690000e+002 5.19690000e+002 5.19690000e+002 5.19690000e+002 5.19690000e+002 / -- Reference densities LB/FT3 DREF 2.62205992e+001 2.99663993e+001 1.56075000e+001 2.49720004e+001 3.17144410e+001 3.51480914e+001 / -- Parachors (Dynes/cm) PARACHOR 6.99809952e+001 1.14071129e+002 1.89919632e+002 2.61760895e+002 4.52601807e+002 9.56223389e+002 / BIC -- Binary Interaction Coefficients 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 1.35247087e-001 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 / -- Reservoir temperature in Deg F RTEMP 122 /
20
Term Project March 2, 2015 4.
Another PVO file was generated for E300 for 6 component matched model in a metric unit:
-- Petroleum Experts - PVTp Export File ---- Export File Signature -- #PetexECL300 -- Export File Version -- #2 -- 2 has increased accuracy (no of decimal places) of output values -- UNITS --METRIC -- !!!!!!!!!!!!!!!!!! PVT FILE DETAILS !!!!!!!!!!!!!! -- PVT FILE NAME : 5_Term Project(C30+)AllMatched.pvi -- STREAM : 6Comp-Matched by BIC's -- Exported :Mon Mar 02 22:36:57 2015 -- !!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!!! - NCOMPS 6/ EOS PR / -- Peng Robinson correction PRCORR -- Standard temperature and pressure in Deg C and BARSA STCOND 15.5667 1.0133 / -- Component names CNAMES N2C1 CO2C2 C3IC4NC4 IC5NC5C6METHY++ C7METHYLCYCLO++ C18C19C20C21C++ / -- Critical temperatures deg K TCRIT 1.90511777e+002 3.05230625e+002 4.14105421e+002 5.13692958e+002 5.52647308e+002 1.01416834e+003 / -- Critical pressures BARSA PCRIT 4.63835114e+001 4.94712095e+001 3.81157055e+001 3.49501364e+001 2.77379241e+001 9.57914763e+000 / -- Critical volumes VCRIT 9.91813983e-002 1.46934305e-001 2.51019369e-001 3.32145960e-001 6.39027019e-001 1.40118351e+000 / -- Reservoir 3-Parameter EoS Shift Coefficients SSHIFT -1.53999999e-001 -1.00199997e-001 -7.05393329e-002 -2.17463728e-002 5.63572347e-001 -8.10160860e-003 / -- Critical volumes for LBC Viscosities VCRITVIS 9.91813983e-002 1.46934305e-001 2.51019369e-001 3.32145960e-001 6.39027019e-001 1.40118351e+000 / -- Acentric factors ACF 1.10554304e-002 1.02514647e-001 1.89455450e-001 2.54017651e-001 3.91309820e-002 1.18171144e+000 / -- Molecular Weights MW 1.60636978e+001 3.04492054e+001 5.64661255e+001 8.22998123e+001 1.49269562e+002 3.81107819e+002 / -- fluid sample composition ZI 3.15100789e-001 6.80842445e-003 4.66116450e-002 1.05275896e-001 3.80357166e-001 1.45846080e-001 / -- Boiling point temperatures deg K TBOIL 1.11532297e+002 1.84853559e+002 2.64895682e+002 3.37239101e+002 4.60120046e+002 6.84077565e+002 / -- Reference temperatures deg K TREF 2.88716667e+002 2.88716667e+002 2.88716667e+002 2.88716667e+002 2.88716667e+002 2.88716667e+002 / -- Reference densities KG/M3 DREF 4.19999987e+002 4.79999989e+002 2.50000000e+002 4.00000006e+002 5.08000016e+002 5.63000023e+002 / -- Parachors (Dynes/cm) PARACHOR 6.99809952e+001 1.14071129e+002 1.89919632e+002 2.61760895e+002 4.52601807e+002 9.56223389e+002 / BIC -- Binary Interaction Coefficients 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 1.35247087e-001 0.00000000e+000 0.00000000e+000 0.00000000e+000 0.00000000e+000 / -- Reference temperatures Deg C RTEMP 50 /
21
Term Project March 2, 2015
7. References 1
Ali Danesh: “PVT and Phase Behavior of Petroleum Reservoir Fluids,” Elsevier (2003). Whitson, C.H.: “PHASE BEHAVIOR, Ch.4: Equation-of-State Calculations,” SPEJ (2000). 3 Whitson, C.H.: “Characterizing Hydrocarbon Plus Fractions,” SPEJ (August 1983) 683; Trans., AIME, 275. 2
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