CN113012763B - Crude oil oxidation reaction kinetic model building method based on four-group components - Google Patents
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- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 96
- 239000010779 crude oil Substances 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 30
- 230000003647 oxidation Effects 0.000 claims abstract description 44
- 238000006243 chemical reaction Methods 0.000 claims abstract description 33
- 238000002474 experimental method Methods 0.000 claims abstract description 24
- 238000004088 simulation Methods 0.000 claims abstract description 24
- 239000003921 oil Substances 0.000 claims abstract description 16
- 239000012530 fluid Substances 0.000 claims abstract description 5
- 238000000646 scanning calorimetry Methods 0.000 claims abstract description 4
- 239000000571 coke Substances 0.000 claims description 14
- 229930195734 saturated hydrocarbon Natural products 0.000 claims description 9
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 7
- 239000000084 colloidal system Substances 0.000 claims description 6
- 238000002347 injection Methods 0.000 claims description 6
- 239000007924 injection Substances 0.000 claims description 6
- 229920005989 resin Polymers 0.000 claims description 6
- 239000011347 resin Substances 0.000 claims description 6
- 230000004913 activation Effects 0.000 claims description 5
- 241000233805 Phoenix Species 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 description 8
- 238000002485 combustion reaction Methods 0.000 description 5
- 230000001186 cumulative effect Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 4
- 239000010426 asphalt Substances 0.000 description 3
- 238000011065 in-situ storage Methods 0.000 description 3
- 230000035699 permeability Effects 0.000 description 3
- 238000009835 boiling Methods 0.000 description 2
- 238000004364 calculation method Methods 0.000 description 2
- 238000005336 cracking Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 238000004227 thermal cracking Methods 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 230000010718 Oxidation Activity Effects 0.000 description 1
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- 230000006872 improvement Effects 0.000 description 1
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- 238000006213 oxygenation reaction Methods 0.000 description 1
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- G16C10/00—Computational theoretical chemistry, i.e. ICT specially adapted for theoretical aspects of quantum chemistry, molecular mechanics, molecular dynamics or the like
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- G—PHYSICS
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- G16C—COMPUTATIONAL CHEMISTRY; CHEMOINFORMATICS; COMPUTATIONAL MATERIALS SCIENCE
- G16C20/00—Chemoinformatics, i.e. ICT specially adapted for the handling of physicochemical or structural data of chemical particles, elements, compounds or mixtures
- G16C20/10—Analysis or design of chemical reactions, syntheses or processes
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- G—PHYSICS
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- G16C—COMPUTATIONAL CHEMISTRY; CHEMOINFORMATICS; COMPUTATIONAL MATERIALS SCIENCE
- G16C20/00—Chemoinformatics, i.e. ICT specially adapted for the handling of physicochemical or structural data of chemical particles, elements, compounds or mixtures
- G16C20/90—Programming languages; Computing architectures; Database systems; Data warehousing
Abstract
The invention discloses a method for establishing a crude oil oxidation reaction kinetic model based on four-group components, which comprises the following steps of: step 1: defining four groups of components of crude oil by using CMG oil reservoir numerical simulation software, defining state parameters of each component, and establishing a crude oil fluid model; step 2: determining an oxidation reaction equation; and step 3: determining the kinetic parameters and enthalpy of the oxidation reaction, and assigning the kinetic parameters and enthalpy of the oxidation reaction to the oxidation reaction equation determined in the step 2; and 4, step 4: simulating the model established in the step 3, and comparing the simulation result with the result obtained by adopting a high Pressure Difference Scanning Calorimetry (PDSC) experiment; and 5: if the simulation result reaches the set precision, ending the simulation to obtain a required oxidation reaction kinetic model; if the simulation result does not reach the set precision, adjusting the kinetic parameters of the oxidation reaction and returning to the step 4; the invention defines the four groups of components of the crude oil, considers the reaction process of the low-temperature oxidation stage and the reaction process of the high-temperature oxidation stage, and has more accurate simulation result.
Description
Technical Field
The invention relates to the technical field of oil and gas field development, in particular to a method for establishing a crude oil oxidation reaction kinetic model based on four-group components.
Background
The thick oil in-situ fire flooding is an efficient thermal method enhanced oil recovery technology, and the success of the technology mainly lies in a series of complex oxidation reactions of air and crude oil. The oxidation reaction mode can be largely classified into low-temperature oxidation, fuel deposition, and high-temperature oxidation. The heat released during the oxidation phase of the crude oil is of great significance to the success of the ignition of the oil reservoir.
At present, the oxidation heat release condition of crude oil is mainly researched by indoor experimental means (a differential scanning calorimeter, an adiabatic acceleration calorimeter and a combustion tube). However, the composition of crude oil is quite complex, which limits the knowledge of the exothermic heat of oxidation of crude oil. The scholars then split the crude oil from a "pseudo-composition" perspective. Belgrave et al (Belgrave J D M, Moore R G, Ursenbach M G, et al. A comprehensive improvement to in-situ combustion modeling [ J ]. SPE Advanced Technology Series 1993,1(1):98-107.) have provided a more comprehensive oxidation reaction kinetic model (including low temperature oxidation, thermal cracking and high temperature oxidation) that was widely used to simulate indoor experimental results and the mine field fire flooding process. In their model, oil samples are divided into two components, maltene and asphaltene. Jia et al (Jia N, Moore R G, Mehta S A, et al. kinetic modeling of thermal cracking and low temperature oxidation reactions [ J. Journal of Canadian Petroleum Technology,2006,45(9):21-28.) further classify the maltenes into a low reactivity component and a high reactivity component, which are difficult to embed into numerical simulation models because detailed information is not provided for both components. In view of the oxidation activity of the four-group components, Sequera et al (Sequera B, Moore R G, Mehta S A, et al.numerical simulation of in-situ synthesis expressed under low temperature conditions [ J ]. Journal of Canadian Petroleum Technology,2010,49(1):55-64.) further proposed a low temperature oxidation reaction model of the four-group components by improving the reaction model of Jia et al; in this model, both aromatics and gums can be oxidized to intermediates in the low temperature oxidation temperature range.
At present, no air injection full-temperature domain crude oil oxidation reaction model based on four-family components exists, and the crude oil oxidation exothermic process is difficult to predict.
Disclosure of Invention
Aiming at the problems in the prior art, the invention provides a method for establishing a crude oil oxidation reaction kinetic model based on four-group components, which can successfully simulate the oxidation exothermic behavior of crude oil in the temperature rise process.
The technical scheme adopted by the invention is as follows:
a method for establishing a crude oil oxidation reaction kinetic model based on four-group components comprises the following steps:
step 1: defining four groups of components of crude oil by using CMG oil reservoir numerical simulation software, defining state parameters of each component, and establishing a crude oil fluid model;
step 2: determining an oxidation reaction equation;
and step 3: determining the kinetic parameters and enthalpy of the oxidation reaction, and assigning the kinetic parameters and enthalpy of the oxidation reaction to the oxidation reaction equation determined in the step 2;
and 4, step 4: simulating the model established in the step 3, and comparing the simulation result with the result obtained by adopting a high Pressure Difference Scanning Calorimetry (PDSC) experiment;
and 5: if the simulation result reaches the set precision, ending the simulation to obtain a required oxidation reaction kinetic model; and if the simulation result does not reach the set precision, adjusting the kinetic parameters of the oxidation reaction and returning to the step 4.
Further, the four-family component of the crude oil in the step 1 comprises saturated hydrocarbon, aromatic hydrocarbon, colloid and asphaltene.
Further, in the step 1, the state parameters (including critical temperature, critical pressure, boiling point, etc.) of each component are determined by fitting the crude oil density and viscosity temperature curves.
Further, the oxidation reaction equation in the step 2 includes a low-temperature oxidation stage reaction equation and a high-temperature oxidation stage reaction equation; the reaction equation of the low-temperature oxidation stage is as follows:
Saturates+39.4713O2→24.25CO2+30.06H2O
Aromatics+4.79O2→0.3716Asphaltenes
Resins+6.01O2→0.5963Asphaltenes
Asphaltenes+12.8078O2→2.01Saturates+80coke+6.48gas+0.1CO2
the reaction equation in the high-temperature oxidation stage is as follows:
coke+1.125O2→0.75CO2+0.25CO+0.5H2O
wherein, satrates is saturated hydrocarbon, aromatic hydrocarbon, Resins is colloid, Asphalenes is asphaltene, and coke is coke.
Further, the oxidation kinetic parameters adjusted in the step 5 include temperature-rising oxidation activation energy and frequency factor.
Further, the oxidation reaction kinetic parameters in the step 3 are obtained by calculation according to an equal conversion rate method.
Further, the thermal break of oxidation reaction is obtained by fitting a curve obtained by a PDSC experiment.
Further, the PDSC experiment in step 4 was performed using a DSC204HP Phoenix thermal analyzer.
Further, the PDSC experiment in the step 4 is carried out by establishing a model simulation through a STAR module in CMG software, the PDSC experiment is simulated by a three-dimensional Cartesian coordinate system, and three grids from left to right sequentially represent an injection well, an oil reservoir and a production well; the crude oil in the middle grid reacts with air.
The invention has the beneficial effects that:
(1) the invention provides a method for establishing an air injection full-temperature-domain crude oil oxidation dynamic reaction model based on four-group components, which can be used for simulating the oxidation heat release characteristics of crude oil in indoor experiments and the fire flooding process of a mine site.
(2) The invention defines the four groups of components of the crude oil, considers the reaction process of the low-temperature oxidation stage and the reaction process of the high-temperature oxidation stage, and has more accurate simulation result and higher simulation calculation efficiency.
Drawings
FIG. 1 is a schematic flow chart of the method of the present invention.
FIG. 2 is a graph of the PDSC of thickened oil using three ramp rates in accordance with the present invention.
FIG. 3 is a PDSC experimental model established by simulation software CMG according to the present invention.
FIG. 4 is a gas-liquid relative permeability curve obtained from a PDSC simulation experiment according to the present invention.
FIG. 5 is a graph comparing the experimental result and the fitting result of the cumulative reaction heat with the temperature increase rate of 5 deg.C/min in the example of the present invention.
FIG. 6 is a graph comparing the experimental result and the fitting result of the cumulative reaction heat with the temperature increase rate of 10 deg.C/min in the example of the present invention.
FIG. 7 is a graph comparing the experimental results and the fitting results of the cumulative reaction heat with a temperature rise rate of 15 deg.C/min in the examples of the present invention.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
As shown in FIG. 1, a method for establishing a dynamic model of oxidation reaction of crude oil based on four groups of components comprises the following steps:
step 1: defining four groups of components of crude oil by using a WinProp module in CMG oil reservoir numerical simulation software, defining state parameters of each component, and establishing a crude oil fluid model;
the state parameters of each simulated component are provided for the numerical model by fitting the crude oil density and the viscosity temperature curve, so that the provided state parameters of each simulated component can accurately represent the characteristics of the experimental oil sample. The state parameters of each component comprise critical temperature, critical pressure, boiling point and the like.
Step 2: determining an oxidation reaction equation;
the reaction model of the crude oil in the low-temperature oxidation stage comprises the following steps:
oxidation of saturated hydrocarbons
Saturates+39.4713O2→24.25CO2+30.06H2O (1)
Oxidation of aromatic hydrocarbons
Aromatics+4.79O2→0.3716Asphaltenes (2)
Oxidation of gums
Resins+6.01O2→0.5963Asphaltenes (3)
Considering the reaction (4) of the oxygenation of asphaltenes to form an oxidised bitumen product and the cracking of the oxidised bitumen to form saturated hydrocarbons, coke, gas and CO2Reaction (5) of (1).
Asphaltenes+12.8078O2→Oxidized Asphaltenes (4)
Cracking of oxidized bitumen to produce saturated hydrocarbons, coke, gas and CO2The reaction of (1): wherein the gas is light hydrocarbon of C4-C12, and the mass density and molecular weight of the coke are respectively 1.4g/cm3And 13 g/mol.
Oxidized Asphaltenes→2.01Saturates+80coke+6.48gas+0.1CO2 (5)
The formula (4) and the formula (5) may be further combined into the formula (6).
Asphaltenes+12.8078O2→2.01Saturates+80coke+6.48gas+0.1CO2 (6)
The above formulas 1, 2, 3 and 6 represent reaction models of saturated hydrocarbons, aromatic hydrocarbons, colloids and asphaltenes, respectively, in a low-temperature oxidation stage.
Since the crude oil sample used in the PDSC experiments was very small (about 0.5mg) and the temperature-rising oxidation was carried out under dynamic air flow, the gases released during the reaction were able to leave the reaction chamber quickly. Thus, the high temperature oxidation reactions observed in PDSCs are primarily coke combustion. The gas phase combustion is partly neglected and the high temperature oxidation mode given comprises only the coke combustion reaction:
coke+1.125O2→0.75CO2+0.25CO+0.5H2O (7)
in the formula: saturrates, Aromatics, Resins, Asphalenes denote Saturates, Aromatics, gums and Asphaltenes, respectively. Oxidized Asphaltenes represent Oxidized Asphaltenes and Coke represents Coke.
And step 3: determining the kinetic parameters and enthalpy of the oxidation reaction, and assigning the kinetic parameters and enthalpy of the oxidation reaction to the oxidation reaction equation determined in the step 2;
the temperature rise oxidation activation energy and frequency factor of crude oil and four-family components are obtained by an equal conversion method (such as Friedman and DAEM). The enthalpies of saturated hydrocarbons, aromatic hydrocarbons, colloids and asphaltenes at the low-temperature oxidation stage (reaction enthalpies determined by PDSC experimental curve fitting) and kinetic parameters (temperature-rising oxidation activation energy and frequency factor) obtained by the DAEM method are assigned to equations 1, 2, 3 and 6 respectively. The enthalpy of the crude oil at the high-temperature oxidation stage and kinetic parameters obtained by the DAEM method (the DAEM method is used in the present invention, but not limited thereto) are assigned to equation 7.
And 4, step 4: simulating the model established in the step 3, and comparing the simulation result with the result obtained by adopting a high Pressure Difference Scanning Calorimetry (PDSC) experiment;
PDSC experiments:
a DSC204HP Phoenix thermal analyzer is adopted to study the pressurized temperature rise oxidation characteristics of the thickened oil and the four-group components thereof.
The method comprises the following steps:
1) accurately weighing 0.5mg of sample in a crucible;
2) pressurizing the inside of the instrument;
3) setting the air flow rate to be 30ml/min and the experiment temperature range to be 30-600 ℃;
4) three heating rates of 5 ℃/min, 10 ℃/min and 15 ℃/min are selected for experiments.
Experiments for all samples were repeated in at least two sets to verify the accuracy and reproducibility of the data, with temperature errors of less than ± 1 ℃. The PDSC curves (pressure 5MPa) for the thickened oils were obtained at three temperature rise rates (5, 10 and 15 ℃/min) as shown in FIG. 1.
The PDSC experimental model can also be established by using a STARS module in commercial numerical simulation software CMG. As shown in fig. 2, the PDSC experiment was simulated by a three-dimensional cartesian coordinate system (3 × 1 × 1 grid). From left to right, the three grids represent, in order, an injection well, a reservoir, and a production well. The grid sizes are all 0.25cm × 0.25cm × 0.25cm, and the crude oil in the middle grid reacts with air.
The relevant conditions were consistent with the conditions of the PDSC experiments, and the grid representing the PDSC reaction chamber was given a constant heat source in order to achieve a constant rate of temperature rise in the CMG simulator. In order to eliminate the influence of the internal energy exchange, heat conduction and reaction heat release of the fluid on the temperature of the mesh, the specific heat of the mesh is set to a large value. Different heating rates are obtained by adjusting the heating source.
To facilitate gas phase flow, the model permeability was set to 10000X 10-3 μm2(ii) a The gas-liquid relative permeability curve was set to allow only the gas phase to flow (as shown in fig. 3) in consideration of the fact that the oil phase could not flow in the crucible during the experiment.
And 5: if the simulation result reaches the set precision, ending the simulation to obtain a required oxidation reaction kinetic model; and if the simulation result does not reach the set precision, adjusting the kinetic parameters of the oxidation reaction and returning to the step 4. And comparing and analyzing the simulation result and the experiment result, and enabling the fitting result to be close to the experiment result by continuously adjusting the kinetic parameters of each reaction (the kinetic parameters adjusted in the invention are temperature-rise oxidation activation energy and frequency factors, and other kinetic parameters are not adjusted).
Examples
The model established by the invention is adopted to obtain the cumulative reaction heat fitting results of different heating rates (5 ℃/min, 10 ℃/min and 15 ℃/min), and the comparison schematic diagram of the cumulative reaction heat fitting results and the experimental results is shown in fig. 5, fig. 6 and fig. 7.
The simulated curve is relatively close to the curve obtained by the experiment, which shows that the oxidation reaction kinetic model established by the invention can successfully simulate the oxidation exothermic behavior of the heavy oil in the temperature rising process.
The invention discloses an air injection full-temperature-domain crude oil oxidation reaction model (from a low-temperature oxidation region to a high-temperature oxidation region) based on four-group components, which can accurately predict the heat release of the crude oil oxidation reaction.
Claims (8)
1. A method for establishing a crude oil oxidation reaction kinetic model based on four-group components is characterized by comprising the following steps:
step 1: defining four groups of components of crude oil by using CMG oil reservoir numerical simulation software, defining state parameters of each component, and establishing a crude oil fluid model;
step 2: determining an oxidation reaction equation; the oxidation reaction equation comprises a low-temperature oxidation stage reaction equation and a high-temperature oxidation stage reaction equation; the reaction equation of the low-temperature oxidation stage is as follows:
Saturates+39.4713O2→24.25CO2+30.06H2O
Aromatics+4.79O2→0.3716Asphaltenes
Resins+6.01O2→0.5963Asphaltenes
Asphaltenes+12.8078O2→2.01Saturates+80coke+6.48gas+0.1CO2
the reaction equation in the high-temperature oxidation stage is as follows:
coke+1.125O2→0.75CO2+0.25CO+0.5H2O
wherein, the satrates is saturated hydrocarbon, the aromatic hydrocarbon, the Resins is colloid, the Asphalenes is asphaltene, and the coke is coke;
and step 3: determining the kinetic parameters and enthalpy of the oxidation reaction, and assigning the parameters and enthalpy to the oxidation reaction equation determined in the step 2;
and 4, step 4: simulating the model established in the step 3, and comparing the simulation result with the result obtained by adopting a high Pressure Difference Scanning Calorimetry (PDSC) experiment;
and 5: if the simulation result reaches the set precision, ending the simulation to obtain a required oxidation reaction kinetic model; and if the simulation result does not reach the set precision, adjusting the kinetic parameters of the oxidation reaction and returning to the step 4.
2. The method for modeling the kinetics of oxidation reaction of crude oil based on four components as claimed in claim 1, wherein the four components of crude oil in step 1 include saturated hydrocarbons, aromatic hydrocarbons, colloids and asphaltenes.
3. The method for building a kinetic model of oxidation reaction of crude oil based on four components as claimed in claim 1, wherein the state parameters of each component are determined by fitting the density and viscosity temperature curves of crude oil in step 1.
4. The method of claim 1, wherein the oxidation kinetics parameters adjusted in step 5 comprise elevated temperature oxidation activation energy and frequency factor.
5. The method for modeling the oxidation reaction kinetics of crude oil based on four components as claimed in claim 1, wherein the oxidation reaction kinetics parameters in step 3 are calculated according to the equal conversion method.
6. The method of claim 1, wherein the enthalpy of oxidation reaction is obtained by curve fitting through PDSC experiments.
7. The method for establishing the kinetic model of the oxidation reaction of crude oil based on four group components in claim 1, wherein the PDSC experiment in the step 4 is performed by using a DSC204HP Phoenix thermal analyzer.
8. The method for modeling the kinetics of the oxidation reaction of crude oil based on four families of components according to claim 1, wherein the PDSC experiment in the step 4 is performed by modeling and simulating a STAR module in CMG software, the PDSC experiment is simulated by a three-dimensional Cartesian coordinate system, and three grids from left to right represent an injection well, an oil reservoir and a production well in sequence; the crude oil in the middle grid reacts with air.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106029610A (en) * | 2014-02-25 | 2016-10-12 | 沙特基础工业公司 | Process and installation for the conversion of crude oil to petrochemicals having improved ethylene and btx yield |
| CN106459780A (en) * | 2014-05-05 | 2017-02-22 | 沙特阿拉伯石油公司 | Demulsification and extraction of biochemicals from crude and its fractions using water and subcritical/supercritical carbon dioxide as proton pump with ph tuning without precipitating oil components |
| CN111927441A (en) * | 2019-05-13 | 2020-11-13 | 中国石油天然气股份有限公司 | Oil-water transition zone crude oil component simulation method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| GB2368848B (en) * | 2000-09-21 | 2002-11-27 | Ciba Sc Holding Ag | Lubricants with 5-tert.-butyl-hydroxy-3-methylphenyl substituted fatty acid esters |
| JP5483329B2 (en) * | 2009-12-24 | 2014-05-07 | Ｊｘ日鉱日石エネルギー株式会社 | Cylinder lubricating oil composition for crosshead type diesel engine |
| JP5689239B2 (en) * | 2010-02-03 | 2015-03-25 | 昭和シェル石油株式会社 | Gasoline engine and diesel engine oil |
| CN108902356A (en) * | 2018-07-26 | 2018-11-30 | 广州利众生物科技有限公司 | A kind of linseed oil, flaxseed gum vegetable fat powder and preparation method thereof |
| CN112305201A (en) * | 2019-07-15 | 2021-02-02 | 中国石油化工股份有限公司 | Method for predicting reservoir crude oil density by utilizing family components |
| CN110761761B (en) * | 2019-11-28 | 2021-08-06 | 中国海洋石油集团有限公司 | Method for reducing emulsification risk of thick oil in steam huff and puff process |
| CN111091244B (en) * | 2019-12-16 | 2023-02-03 | 武汉材料保护研究所有限公司 | Engine lubricating oil change period prediction method |
| CN111126685B (en) * | 2019-12-16 | 2023-02-03 | 武汉材料保护研究所有限公司 | Method for establishing engine lubricating oil quality prediction model |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106029610A (en) * | 2014-02-25 | 2016-10-12 | 沙特基础工业公司 | Process and installation for the conversion of crude oil to petrochemicals having improved ethylene and btx yield |
| CN106459780A (en) * | 2014-05-05 | 2017-02-22 | 沙特阿拉伯石油公司 | Demulsification and extraction of biochemicals from crude and its fractions using water and subcritical/supercritical carbon dioxide as proton pump with ph tuning without precipitating oil components |
| CN111927441A (en) * | 2019-05-13 | 2020-11-13 | 中国石油天然气股份有限公司 | Oil-water transition zone crude oil component simulation method |
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