Enhanced Solubility and Miscibility of CO2-Oil Mixture in the Presence of Propane under Reservoir Conditions to Improve Recovery Efficiency
Abstract
:1. Introduction
2. Experimental
2.1. Materials
2.1.1. Viscosity of Trembley Oil
2.1.2. Density of Trembley Oil
2.2. Experimental Setup
2.3. Experimental Procedure
3. Mathematical Formulations
3.1. Oil Characterization
- A constant Watson factor Kw [32] is assumed based on the molecular weight and specific gravity of the oil sample:
- Specific gravity for each SCN [33] can be calculated according to the Kw:
- The boiling temperature is calculated by using the Soreide [34] correlation, which is a function of and
- Then, the critical properties and acentric factor of SCN are estimated by the Kesler [35] correlations, which are the function of .
- Acentric factor [36] can be calculated from as well:If ,If ,where , , , , , , , .
- Molecular weight of C42+ can be estimated from its known mass fraction and the number of moles:
3.2. Lumping
3.3. PR EOS Model
PR EOS
3.4. MMP
- Start with initial equations at the initial pressure and given temperature:
- To obtain a set of intersecting tie lines, the following equations are applied:
- Increase the pressure slightly. Equations (28) and (29) are solved again using the solution for the previous pressure;
- Repeat Step #c until one of the tie lines shrinks to a point at which condition is fulfilled for the nth tie line if
4. Results and Discussions
4.1. PVT Equipment Validation
4.2. Characterization of Trembley Oil
4.3. Validation of the Developed BIP Correlations
4.4. Saturation Pressure and Solubility
4.5. Viscosity of the Gas-Saturated Oil at High Pressures
4.6. Miscibility between Gas and Oil
5. Conclusions
- (1)
- Under reservoir conditions, the saturation pressures of the C3H8-oil mixture, CO2-oil mixture, and C3H8-CO2-oil mixture have been experimentally and theoretically determined. It has been found that the saturation pressure increases with the temperature, as well as with the amount of C3H8, CO2, or CO2-C3H8 gas mixture in the oil;
- (2)
- The saturation pressures are successfully predicted by using the well-developed PR EOS model, together with two newly developed BIP correlations with an overall AARD of 2.39%, where three pseudo-component lumping schemes are applied;
- (3)
- The correlations of Trembley oil’s viscosity and density have been successfully generated for temperatures ranging from 20 °C to 75 °C. The measured viscosity and saturation pressure data confirm that the presence of C3H8 in the CO2 stream can enhance oil-recovery performance by achieving miscibility at lower pressures and delaying gas-breakthrough time, ultimately leading to more CO2 being stored in the reservoir;
- (4)
- The enhancement in miscibility through C3H8 addition can effectively delay gas breakthrough and increase incremental oil recovery compared to immiscible or near-miscible CO2 flooding, thus minimizing CO2 breakthrough and improving the overall EOR efficiency.
Author Contributions
Funding
Data Availability Statement
Conflicts of Interest
Nomenclature
a | Attraction parameter in the PR-EOS |
ac | Constant in the PR EOS |
b | Van der Waals volume, m3/kmol |
Kw | Watson factor, dimensionless |
T | Temperature, °C |
TbR | Normal boiling point at 1 atm, °R |
TC | Critical temperature, K |
Mi | Molecular weight of component i, g/mol |
m | Sample mass |
n | Number of moles |
P | Pressure, psi |
PC | Critical pressure, psi |
R | Universal gas constant |
SG | Specific gravity, dimensionless |
V | Original molar volume calculated by the PR EOS, m3/kmol |
VC | Critical molar volume, m3/kmol |
Calculated saturation pressure | |
Experimentally measured saturation pressure | |
wi | Mass fraction |
xi | Mole fraction of component i in the equilibrium liquid phase |
yi | Mole fraction of component i in the equilibrium gas phase |
zi | Mole fraction of the component i |
α | α function in the PR EOS |
β | Adjustable exponent defined in Equation (21) |
σ | Adjustable exponent defined in Equation (25) |
ρ | Density, g/cm3 |
μ | Viscosity, cP |
Binary interaction parameter (BIP) between ith and jth component. | |
ω | Acentric factor, dimensionless |
Fugacity coefficient of component i, dimensionless | |
Generic symbol for any property | |
Specific gravity, dimensionless | |
Specific gravity of component i, dimensionless |
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Feed # | Composition, mol% | Temperature, °C | ||
---|---|---|---|---|
C3H8 | CO2 | Trembley Oil | ||
1 | 34.62 | 0.0 | 65.38 | 25, 30, 40, 50 |
2 | 46.65 | 0.0 | 53.35 | 25, 30, 40, 50 |
3 | 60.08 | 0.0 | 39.92 | 25, 30, 40, 50 |
4 | 72.21 | 0.0 | 27.79 | 25, 30, 40, 50 |
5 | 0.0 | 29.29 | 70.71 | 25, 30, 40, 50 |
6 | 0.0 | 47.35 | 52.65 | 25, 30, 40, 50 |
7 | 0.0 | 60.39 | 39.61 | 25, 30, 40, 50 |
8 | 0.0 | 73.74 | 26.26 | 25, 30, 40, 50 |
9 | 13.03 | 46.04 | 40.57 | 25, 30, 40, 50 |
10 | 20.54 | 41.18 | 38.28 | 25, 30, 40, 50 |
11 | 14.34 | 51.05 | 34.61 | 25, 30, 40, 50 |
12 | 16.16 | 57.57 | 26.27 | 25, 30, 40, 50 |
Carbon No. | wt % | mol% | Carbon No. | wt% | mol% |
---|---|---|---|---|---|
C1 | 0.0000 | 0.0000 | C23 | 2.4646 | 1.7589 |
C2 | 0.0000 | 0.0000 | C24 | 2.4059 | 1.6459 |
C3 | 0.0000 | 0.0000 | C25 | 2.1876 | 1.4370 |
C4 | 0.0000 | 0.0000 | C26 | 2.0541 | 1.2977 |
C5 | 0.0000 | 0.0000 | C27 | 2.0280 | 1.2340 |
C6 | 0.5450 | 1.4653 | C28 | 1.8724 | 1.0989 |
C7 | 3.2287 | 7.4656 | C29 | 1.8359 | 1.0405 |
C8 | 3.9144 | 7.9396 | C30 | 1.9715 | 1.0802 |
C9 | 5.8007 | 10.4787 | C31 | 1.8066 | 0.9581 |
C10 | 4.5822 | 7.4615 | C32 | 1.4699 | 0.7553 |
C11 | 3.8471 | 5.7023 | C33 | 1.4436 | 0.7194 |
C12 | 3.3481 | 4.5539 | C34 | 1.2218 | 0.5910 |
C13 | 4.7586 | 5.9800 | C35 | 1.3866 | 0.6517 |
C14 | 4.6292 | 5.4060 | C36 | 0.9497 | 0.4340 |
C15 | 3.9684 | 4.3283 | C37 | 1.3118 | 0.5833 |
C16 | 3.5751 | 3.6578 | C38 | 1.1327 | 0.4905 |
C17 | 5.1290 | 4.9415 | C39 | 0.6638 | 0.2801 |
C18 | 4.1833 | 3.8083 | C40 | 0.8432 | 0.3469 |
C19 | 3.3873 | 2.9225 | C41 | 0.7403 | 0.2972 |
C20 | 2.4659 | 2.0220 | C42 | 0.8318 | 0.3260 |
C21 | 3.0100 | 2.3514 | C42+ | 6.8063 | 0.8485 |
C22 | 2.1989 | 1.6402 | Total | 100 | 100 |
Temperature (°C) | Reference Value (psi) | Continuous Method | Stepwise Method | ||
---|---|---|---|---|---|
Measured (psi) | Error (%) | Measured (psi) | Error (%) | ||
30 | 158.4 | 163.2 | 3.03 | 161.6 | 2.02 |
40 | 190.3 | 195.4 | 2.67 | 192.7 | 1.26 |
50 | 226.8 | 232.6 | 2.56 | 230.1 | 1.45 |
No. of PCs * | MW, g/mol | PC, atm | TC, K | γ | Tb, K | ω |
---|---|---|---|---|---|---|
1 | 234.667 | 17.008 | 753.715 | 0.863 | 573.479 | 0.114 |
2 | 150.212 | 23.711 | 641.937 | 0.794 | 459.751 | 0.212 |
490.845 | 14.631 | 869.390 | 0.954 | 687.960 | 0.636 | |
3 | 129.247 | 25.914 | 610.064 | 0.774 | 427.981 | 0.176 |
213.037 | 18.350 | 727.432 | 0.846 | 546.376 | 0.312 | |
580.628 | 13.101 | 910.548 | 0.982 | 728.647 | 0.739 | |
4 | 116.781 | 27.578 | 588.588 | 0.760 | 407.150 | 0.153 |
163.012 | 21.979 | 664.193 | 0.807 | 481.339 | 0.236 | |
231.871 | 17.262 | 748.773 | 0.860 | 568.598 | 0.337 | |
604.239 | 12.911 | 919.991 | 0.990 | 737.828 | 0.766 | |
5 | 116.782 | 27.579 | 588.589 | 0.761 | 407.517 | 0.153 |
163.013 | 21.980 | 664.193 | 0.808 | 481.773 | 0.237 | |
219.448 | 17.853 | 735.917 | 0.852 | 555.609 | 0.322 | |
296.820 | 14.796 | 808.874 | 0.899 | 632.341 | 0.408 | |
745.441 | 12.270 | 966.642 | 1.030 | 782.285 | 0.933 | |
6 | 107.672 | 28.999 | 571.533 | 0.750 | 390.998 | 0.136 |
134.178 | 25.045 | 619.963 | 0.780 | 437.200 | 0.186 | |
171.067 | 21.184 | 676.108 | 0.814 | 493.328 | 0.250 | |
219.447 | 17.852 | 735.916 | 0.852 | 555.108 | 0.322 | |
290.818 | 14.952 | 804.197 | 0.896 | 626.856 | 0.403 | |
718.796 | 12.343 | 958.868 | 1.022 | 774.496 | 0.901 |
Binary and Ternary Systems | Feed No. | No. of PCs | ||||||
---|---|---|---|---|---|---|---|---|
Temperature (°C) | 1 | 2 | 3 | 4 | 5 | 6 | ||
C3H8-oil | 1 | 25 | 1.99 | 1.21 | 1.32 | 1.47 | 1.22 | 1.31 |
2 | 30 | 2.21 | 1.30 | 1.48 | 1.52 | 1.25 | 1.34 | |
3 | 40 | 2.44 | 1.54 | 1.55 | 1.57 | 1.29 | 1.39 | |
4 | 50 | 2.68 | 1.41 | 1.54 | 1.63 | 1.33 | 1.44 | |
CO2-oil | 5 | 25 | 0.19 | 0.27 | 0.04 | 0.05 | 0.03 | 0.05 |
6 | 30 | 0.09 | 0.00 | 0.01 | 0.00 | 0.00 | 0.00 | |
7 | 40 | 0.92 | 0.06 | 0.10 | 0.11 | 0.08 | 0.12 | |
8 | 50 | 0.38 | 0.00 | 0.01 | 0.02 | 0.00 | 0.03 | |
C3H8-CO2-oil (β for C3H8-PC) | 9 | 25 | 1.60 | 1.36 | 1.36 | 1.36 | 1.22 | 1.36 |
10 | 30 | 1.69 | 1.30 | 1.40 | 1.42 | 1.28 | 1.39 | |
11 | 40 | 2.68 | 1.36 | 1.36 | 1.36 | 1.29 | 1.34 | |
12 | 50 | 1.72 | 1.36 | 1.37 | 1.36 | 1.33 | 1.20 | |
C3H8-CO2-oil (β for CO2-PC) | 9 | 25 | 0.22 | 0.01 | 0.01 | 0.01 | 0.03 | 0.01 |
10 | 30 | 0.31 | 0.01 | 0.02 | 0.04 | 0.03 | 0.06 | |
11 | 40 | 0.50 | 0.01 | 0.01 | 0.01 | 0.08 | 0.01 | |
12 | 50 | 0.34 | 0.01 | 0.02 | 0.01 | 0.00 | 0.01 |
System | μ (cP) |
---|---|
C3H8-oil (Feed #1) | 2.33 |
CO2-oil (Feed #8) | 3.03 |
C3H8-CO2-oil (Feed #12) | 1.89 |
Dead oil at 1600 psi | 9.50 |
Dead oil at room pressure | 9.49 |
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Du, X.; Li, X.; Thakur, G.C. Enhanced Solubility and Miscibility of CO2-Oil Mixture in the Presence of Propane under Reservoir Conditions to Improve Recovery Efficiency. Energies 2024, 17, 4790. https://doi.org/10.3390/en17194790
Du X, Li X, Thakur GC. Enhanced Solubility and Miscibility of CO2-Oil Mixture in the Presence of Propane under Reservoir Conditions to Improve Recovery Efficiency. Energies. 2024; 17(19):4790. https://doi.org/10.3390/en17194790
Chicago/Turabian StyleDu, Xuejia, Xiaoli Li, and Ganesh C. Thakur. 2024. "Enhanced Solubility and Miscibility of CO2-Oil Mixture in the Presence of Propane under Reservoir Conditions to Improve Recovery Efficiency" Energies 17, no. 19: 4790. https://doi.org/10.3390/en17194790