CN116411957A - Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis - Google Patents
Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis Download PDFInfo
- Publication number
- CN116411957A CN116411957A CN202111676356.3A CN202111676356A CN116411957A CN 116411957 A CN116411957 A CN 116411957A CN 202111676356 A CN202111676356 A CN 202111676356A CN 116411957 A CN116411957 A CN 116411957A
- Authority
- CN
- China
- Prior art keywords
- narrow
- oil
- crude oil
- reservoir
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000010779 crude oil Substances 0.000 title claims abstract description 196
- 238000000034 method Methods 0.000 title claims abstract description 109
- 238000002347 injection Methods 0.000 title claims abstract description 75
- 239000007924 injection Substances 0.000 title claims abstract description 75
- 238000011161 development Methods 0.000 title claims abstract description 73
- 238000004458 analytical method Methods 0.000 title claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 133
- 230000003647 oxidation Effects 0.000 claims abstract description 120
- 238000002156 mixing Methods 0.000 claims abstract description 30
- 239000000203 mixture Substances 0.000 claims abstract description 25
- 239000003921 oil Substances 0.000 claims description 225
- 238000004821 distillation Methods 0.000 claims description 82
- 230000008569 process Effects 0.000 claims description 48
- 238000002485 combustion reaction Methods 0.000 claims description 29
- 238000012360 testing method Methods 0.000 claims description 25
- 238000004088 simulation Methods 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 26
- 229910052760 oxygen Inorganic materials 0.000 description 26
- 239000001301 oxygen Substances 0.000 description 26
- 239000000571 coke Substances 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 15
- 230000000694 effects Effects 0.000 description 12
- 239000011148 porous material Substances 0.000 description 11
- 230000007246 mechanism Effects 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000011160 research Methods 0.000 description 6
- 239000004215 Carbon black (E152) Substances 0.000 description 5
- 230000010718 Oxidation Activity Effects 0.000 description 5
- 230000009286 beneficial effect Effects 0.000 description 5
- 229930195733 hydrocarbon Natural products 0.000 description 5
- 150000002430 hydrocarbons Chemical class 0.000 description 5
- 238000006213 oxygenation reaction Methods 0.000 description 5
- 230000009257 reactivity Effects 0.000 description 5
- 230000001133 acceleration Effects 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- 238000004364 calculation method Methods 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 239000000446 fuel Substances 0.000 description 4
- 239000000295 fuel oil Substances 0.000 description 4
- 238000000197 pyrolysis Methods 0.000 description 4
- 238000007872 degassing Methods 0.000 description 3
- 229930195734 saturated hydrocarbon Natural products 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- RZVAJINKPMORJF-UHFFFAOYSA-N Acetaminophen Chemical compound CC(=O)NC1=CC=C(O)C=C1 RZVAJINKPMORJF-UHFFFAOYSA-N 0.000 description 2
- -1 C20 hydrocarbon Chemical class 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 230000000704 physical effect Effects 0.000 description 2
- 230000001737 promoting effect Effects 0.000 description 2
- PLPFBVXTEJUIIT-UHFFFAOYSA-N 1,2-dimethylanthracene Chemical compound C1=CC=CC2=CC3=C(C)C(C)=CC=C3C=C21 PLPFBVXTEJUIIT-UHFFFAOYSA-N 0.000 description 1
- 230000002159 abnormal effect Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000003306 harvesting Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000013178 mathematical model Methods 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000012821 model calculation Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
Images
Classifications
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B49/00—Testing the nature of borehole walls; Formation testing; Methods or apparatus for obtaining samples of soil or well fluids, specially adapted to earth drilling or wells
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/166—Injecting a gaseous medium; Injecting a gaseous medium and a liquid medium
- E21B43/168—Injecting a gaseous medium
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N11/00—Investigating flow properties of materials, e.g. viscosity, plasticity; Analysing materials by determining flow properties
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N31/00—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods
-
- G—PHYSICS
- G01—MEASURING; TESTING
- G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
- G01N31/00—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods
- G01N31/005—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods investigating the presence of an element by oxidation
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B2200/00—Special features related to earth drilling for obtaining oil, gas or water
- E21B2200/20—Computer models or simulations, e.g. for reservoirs under production, drill bits
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A10/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE at coastal zones; at river basins
- Y02A10/40—Controlling or monitoring, e.g. of flood or hurricane; Forecasting, e.g. risk assessment or mapping
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Mining & Mineral Resources (AREA)
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Geology (AREA)
- Health & Medical Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Fluid Mechanics (AREA)
- Environmental & Geological Engineering (AREA)
- Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Biochemistry (AREA)
- General Health & Medical Sciences (AREA)
- General Physics & Mathematics (AREA)
- Immunology (AREA)
- Pathology (AREA)
- Molecular Biology (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a crude oil pseudo-component, an acquisition method thereof and an air injection development reservoir determination method based on crude oil component analysis. The first crude oil mimetic composition is formed by mixing narrow distillates having a negative temperature coefficient range for oxidation rate and fluidity at reservoir temperature in a narrow distillate group of the target crude oil. The second crude oil pseudo-component is formed by mixing narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and fluidity at reservoir temperature in the narrow distillates group of the target crude oil. The third crude oil pseudo component is formed by mixing narrow distillates having a negative temperature coefficient range of oxidation rate and no fluidity at reservoir temperature in the narrow distillates group of the target crude oil. The fourth crude oil pseudo-component is formed by mixing narrow distillates having no negative temperature coefficient interval of oxidation rate and no fluidity at reservoir temperature in the narrow distillate group of the target crude oil.
Description
Technical Field
The invention belongs to the technical field of thickened oil development, and particularly relates to a crude oil quasi-component acquisition method, a crude oil quasi-component and an air injection development reservoir layer determination method based on crude oil component analysis.
Background
In modeling analysis of crude oil air injection development, it is necessary to make clear what components are involved in what chemical reactions and what is generated after the reactions throughout the displacement process. Crude oil, however, is a complex mixture of numerous hydrocarbon and non-hydrocarbon compounds, and two major difficulties are encountered in determining its chemical composition: (1) The components are extremely complex, the relative molecular weight is from tens to thousands, the differences are very large, and the isomers are extremely large; (2) a plurality of mixed structural molecules are present. Meanwhile, each time a component and a reaction equation of the numerical model are added, the calculation time is increased in geometric progression.
The currently common crude oil component classification methods mainly comprise three types:
(1) Four component process (SARA process), which divides crude oil into four components, saturated hydrocarbons, aromatic hydrocarbons, gum, asphaltenes, where asphaltenes are the most polar non-hydrocarbon components of the crude oil that are the largest relative molecular weight, and gum is the larger non-hydrocarbon compound of the crude oil that is the next to asphaltenes in relative molecular weight and polarity.
(2) Fraction method-crude oil is divided according to boiling point, wherein the fraction oil with boiling point below 200 ℃ is called light fraction, the fraction oil with boiling point below 200 ℃ is called middle fraction, and the fraction oil with boiling point above 350 ℃ is called heavy fraction.
(3) Minimum model—crude oil is separated into heavy oil, light oil, coke.
In the four-component method, frequent conversion exists between colloid and asphaltene, which is difficult to realize in actual simulation, and in order to remedy the defect, the STARS software of the general thermal recovery simulation software-CMG company uses carbon number as a division basis to divide C33-C60 into asphalt, C20-C32 into colloid and aromatic hydrocarbon and C2-C19 into saturated hydrocarbon. The four-component method takes the carbon number as a component dividing unit, combines the advantages of the SARA model, and can clearly describe the oxidation reaction in the fireflood process.
Heretofore, the four-component method has not been applied to numerical simulation of air injection development. The main reason is that: first, the components divided in units of carbon number do not match the oxidation activity, and C10 and C36 should be incorporated into different pseudo-components according to the above four-component method, but they tend to be oxidized at the same temperature and pressure in the same low-temperature and high-temperature combustion mode, i.e., they should be incorporated into the same pseudo-components from the viewpoint of oxidation reaction; the paraffinic C20 hydrocarbon and the aromatic C20 hydrocarbon have the same carbon number, but the paraffinic hydrocarbon burns in a low temperature range, the aromatic hydrocarbon burns in a high temperature range, the oxidation activities are greatly different, and from the oxidation point of view, they should not be combined into the same pseudo-component as shown in FIG. 1; secondly, the reaction process and the oil extraction mechanism in the thermochemical flooding process cannot be intuitively and simply displayed, so that the research process is extremely complex; third, no consideration is given to the transition conditions from low-temperature oxidation to high-temperature oxidation.
Currently, the distillate method is not used in the mechanism analysis and numerical simulation research of air injection development.
The minimum model is the simplest and practical air injection development analysis model at present, but has serious disadvantages: first, the fuel is derived only from heavy oil cracking; secondly, the same heavy oil, the fire driving mechanism of saturated hydrocarbon and aromatic hydrocarbon is quite different, and the large error exists in the process of dividing crude oil by heavy oil, light oil and coke. In order to make up for the shortage of the minimum model for the consideration of the crude oil low-temperature oxidation mechanism, the component 1 of the fuel coke generated by the crude oil low-temperature oxidation is added in 2006. Although this improvement is helpful for understanding the mechanism of air injection development, the model is not widely used in the related mechanism and numerical simulation research because of the great ambiguity of the generation mechanism and oxidation mode of coke 1 in the research field.
The traditional method for dividing the components by taking the carbon number as the unit cannot be applied to oil deposit engineering and numerical simulation calculation or is difficult to apply to the oil deposit engineering and numerical simulation calculation, and the reaction process and the oil extraction mechanism in the development process of the crude oil injection air cannot be intuitively and simply displayed; only the low-temperature oxidation process and the high-temperature oxidation process are considered, the whole oxidation reaction process cannot be reflected, and therefore, a reservoir suitable for air injection development cannot be determined through analysis and construction of crude oil components. At present, no particularly suitable method is adopted to screen a reservoir suitable for air injection exploitation, so that a plurality of failure cases of air injection exploitation occur, and in addition, exploitation failures caused by inconsistent early simulation and on-site exploitation processes in thick oil air injection exploitation are also good at all.
Disclosure of Invention
The invention aims to provide a crude oil pseudo-component capable of effectively solving the problem of on-site crude oil extraction in air injection development and an acquisition method thereof.
It is another object of the present invention to provide an air injection development reservoir identification method that helps promote the smooth progress of in-situ air injection development.
In order to achieve the above object, in a first aspect, the present invention provides a crude oil mimetic composition, wherein the crude oil mimetic composition is formed by mixing, in a narrow-cut oil group of a target crude oil, individual narrow-cuts oils having a negative temperature coefficient interval of oxidation rate and fluidity at reservoir temperature.
In a preferred embodiment of the first aspect, the narrow-cut oil has a distillation range temperature range of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the first aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
In a preferred embodiment of the first aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at reservoir temperature; narrow distillates with a distillation range temperature greater than 200 ℃ do not have flowability at reservoir temperatures.
In a preferred embodiment of the first aspect, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; narrow distillates with a distillation range temperature greater than 300 ℃ do not have flowability at reservoir temperatures.
In a second aspect, the present invention provides a crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having no negative temperature coefficient of section for oxidation rate and fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
In a preferred embodiment of the second aspect, the narrow-cut oil has a distillation range temperature interval of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the second aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
In a preferred embodiment of the second aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at reservoir temperature; the narrow fraction oil with a distillation range temperature of 200 ℃ or higher has no fluidity at the reservoir temperature.
In a preferred embodiment of the second aspect, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; the narrow fraction oil having a distillation range temperature of 300 ℃ or higher does not have fluidity at the reservoir temperature.
In a preferred embodiment, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at reservoir temperature; the narrow fraction oil with a distillation range temperature of 200 ℃ or higher has no fluidity at the reservoir temperature.
In a preferred embodiment, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; the narrow fraction oil having a distillation range temperature of 300 ℃ or higher does not have fluidity at the reservoir temperature.
In a third aspect, the present invention provides a crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having a negative temperature coefficient range for oxidation rate and no fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
In a preferred embodiment of the third aspect, the narrow-cut oil has a distillation range temperature range of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the third aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
In a preferred embodiment of the third aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 200 ℃ do not have flowability at reservoir temperatures.
In a preferred embodiment of the third aspect, the narrow-cut oil having a distillation range temperature of 300 ℃ or less has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 300 ℃ do not have flowability at reservoir temperatures.
In a fourth aspect, the present invention provides a crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having no negative temperature coefficient of section for oxidation rate and no fluidity at reservoir temperature in a narrow distillate group of target crude oil.
In a preferred embodiment of the fourth aspect, the narrow-cut oil has a distillation range temperature interval of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the fourth aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
In a preferred embodiment of the fourth aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 200 ℃ do not have flowability at reservoir temperatures.
In a preferred embodiment of the fourth aspect, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 300 ℃ do not have flowability at reservoir temperatures.
In a fifth aspect, the present invention provides a method for obtaining a crude oil pseudo-component, wherein the method comprises:
obtaining a narrow fraction oil group of target crude oil;
carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval (namely NTC interval); carrying out mobility test on each narrow fraction oil in the narrow fraction oil group at the reservoir temperature to determine whether each narrow fraction oil has mobility at the reservoir temperature;
obtaining a target crude oil pseudo-component based on whether the oxidation rate of each narrow-cut oil of the target crude oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at reservoir temperature; wherein,,
mixing the narrow distillates having an oxidation rate having a negative temperature coefficient range and fluidity at reservoir temperature to form a target crude oil first pseudo-component;
mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that is mobile at reservoir temperatures to form a target crude oil second pseudo-component;
Mixing the narrow distillates having an oxidation rate with a negative temperature coefficient range and no fluidity at reservoir temperature to form a target crude third pseudo-component;
the narrow distillates, which do not have a negative temperature coefficient range for oxidation rate and which do not have fluidity at reservoir temperature, are mixed to form the target crude fourth pseudo-component.
In a preferred embodiment of the fifth aspect, the narrow-cut oil has a distillation range temperature interval of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the fifth aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at the reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
Among them, each of the narrow-cut oils having no fluidity at the reservoir temperature may be regarded as medium-heavy narrow-cut oil, and each of the narrow-cut oils having fluidity at the reservoir temperature may be regarded as light narrow-cut oil.
In a preferred embodiment of the fifth aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at the reservoir temperature; narrow distillates with a distillation range temperature of greater than 200 ℃ do not have flowability at reservoir temperatures.
In a preferred embodiment of the fifth aspect, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 300 ℃ do not have flowability at reservoir temperatures.
The traditional method for obtaining the quasi-components by taking the carbon number as a unit causes the abnormal complexity of the air injection development simulation research process, can not reflect the whole process of oxidation reaction, and can not be effectively applied to solve the problem of on-site crude oil exploitation.
In a sixth aspect, the present invention provides an air injection development reservoir determination method based on crude oil composition analysis, wherein the method comprises:
Obtaining a narrow fraction oil group of crude oil of a target reservoir;
carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval (namely NTC interval); carrying out mobility test on each narrow fraction oil in the narrow fraction oil group at the target reservoir temperature, and determining whether each narrow fraction oil has mobility at the target reservoir temperature;
determining a first, second, third and fourth pseudo-components of the target reservoir crude based on whether the oxidation rate of each narrow-cut oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at the target reservoir temperature; wherein the first crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate having negative temperature coefficient interval and fluidity at reservoir temperature, the second crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate not having negative temperature coefficient interval and fluidity at reservoir temperature, the third crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate having negative temperature coefficient interval and not fluidity at reservoir temperature, and the fourth crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate not having negative temperature coefficient interval and not fluidity at reservoir temperature;
When the target reservoir crude oil has a first mimetic component and/or a third mimetic component, the target reservoir is air-injected developed as an air-injected development reservoir.
In a preferred embodiment of the sixth aspect, the crude oil oxidation process is controlled during the air injection development process;
further, the control of the crude oil oxidation process is realized by controlling the combustion temperature to be in the optimal combustion temperature range; still further, the optimum combustion temperature is determined by:
injecting air under different combustion temperature conditions to develop a simulation experiment for a target reservoir;
determining the optimal combustion temperature according to the simulation experiment result;
further, the control method of the oxidation process is determined by performing simulation analysis on the roles of the pseudo components in the oxidation process, and comprises the following steps:
factors considered in the simulation analysis of the effect of the first pseudo-component on the progress of the oxidation reaction include: (1) when the pyrolysis temperature is reached by heating, the components are separated;
(2) because the reservoir is heated, when the oxygen intake is insufficient, coke is generated by low-temperature oxidation, pores are blocked, the subsequent oxygen is influenced to enter the pores, and when the reservoir is rich in oxygen and the temperature of the reservoir is not high, combustion is unfavorable;
(3) When the oxygen inlet amount is sufficient, the temperature is increased to a degree that the coke generated by the partial oxygenation reaction can be ignited and burnt;
(4) under the condition of proper temperature and oxygen inlet amount, the crude oil can be oxidized at high temperature as soon as possible, so that other crude oil with similar components at the periphery is driven to be oxidized at high temperature.
Further, factors considered in the simulation analysis of the effect of the second pseudo-component on the progress of the oxidation reaction include: (1) when the pyrolysis temperature is reached, the components are separated;
(2) because the reservoir is heated, when the oxygen intake is insufficient, coke is generated by low-temperature oxidation, pores are blocked, the subsequent oxygen is influenced to enter the pores, and when the reservoir is rich in oxygen and the temperature of the reservoir is not high, combustion is unfavorable;
(3) when the oxygen inlet amount is sufficient, the temperature is increased to a degree that the coke generated by the partial oxygenation reaction can be ignited and burnt;
further, factors considered in the simulation analysis of the effect of the third pseudo-component on the progress of the oxidation reaction include: (1) under the conditions of proper temperature and oxygen inlet amount, whether the crude oil enters high-temperature oxidation as soon as possible or not can be judged, so that other crude oil with similar components on the periphery is driven to generate high-temperature oxidation;
(2) because the reservoir is heated, when the oxygen intake is insufficient, coke is generated by low-temperature oxidation, pores are blocked, the subsequent oxygen is influenced to enter the pores, and when the reservoir is rich in oxygen and the temperature of the reservoir is not high, combustion is unfavorable;
(3) When the oxygen inlet amount is sufficient, the temperature is increased to a degree that the coke generated by the partial oxygenation reaction can be ignited and burnt;
further, factors considered in the simulation analysis of the effect of the fourth pseudo-component on the progress of the oxidation reaction include: (1) under the condition of proper temperature and oxygen feeding amount, the crude oil with the intended components is oxidized at high temperature;
(2) because the reservoir is heated, when the oxygen intake is insufficient, coke is generated by low-temperature oxidation, pores are blocked, the subsequent oxygen is influenced to enter the pores, and when the reservoir is rich in oxygen and the temperature of the reservoir is not high, combustion is unfavorable;
(3) when the oxygen inlet amount is sufficient, the temperature is increased to a degree that the coke generated by the partial oxygenation reaction can be ignited and burnt;
in a preferred embodiment of the sixth aspect, the narrow-cut oil has a distillation range temperature interval of 25 ℃;
for example, the narrow distillate group includes distillate oil with a distillation range of 100 ℃ or more and less than 125 ℃, distillate oil with a distillation range of 125 ℃ or more and less than 150 ℃, distillate oil with a distillation range of 150 ℃ or more and less than 175 ℃, distillate oil with a distillation range of 175 ℃ or more and less than 200 ℃, and distillate oil with a distillation range of 200 ℃ or more and less than 225 ℃; further, the narrow cut oil group includes cut oil of a distillation range of less than 100 ℃.
In a preferred embodiment of the sixth aspect, the narrow-cut oil having a viscosity of not more than 500 mPa-s has flowability at the reservoir temperature, and the narrow-cut oil having a viscosity of more than 500 mPa-s does not have flowability.
In a preferred embodiment of the sixth aspect, the narrow-cut oil having a distillation range temperature of 200 ℃ or less has fluidity at the reservoir temperature; narrow distillates with a distillation range temperature of greater than 200 ℃ do not have flowability at reservoir temperatures.
In a preferred embodiment of the sixth aspect, the narrow-cut oil having a distillation range temperature below 300 ℃ has fluidity at reservoir temperature; narrow distillates with a distillation range temperature of greater than 300 ℃ do not have flowability at reservoir temperatures.
The inventor searches the oxidation dynamics characteristics of crude oil and distillate oil thereof by carrying out oxidation dynamics characteristic experiments on the crude oil and distillate oil thereof which are collected from different areas and have different viscosities, and discovers that the crude oil and distillate oil thereof sometimes have a Negative Temperature Coefficient (NTC) oxidation process between low-temperature oxidation and high-temperature oxidation, and the oxidation reaction rate of fuel is reduced along with the increase of temperature in a certain negative temperature coefficient oxidation process interval, so that phenomena such as ignition delay and the like are caused, but the interval of the negative temperature coefficient oxidation process is an interval with oxidation reaction activity, and the oxidation activity is helpful for promoting the exploitation process of the crude oil, so that air injection development is better realized. Further, the process is properly controlled, and the increase of the crude oil exploitation yield can be realized.
Currently, the success rate of the implemented fireflood development (i.e., air injection development) project is low, one of the reasons being the complexity of the fireflood process itself, which involves a series of chemical reactions, three-phase complex migration processes, and various reaction phenomena, and there is a lack of in-depth knowledge of how the combustion process proceeds in the reservoir. The inventor of the invention is based on the research on crude oil narrow-fraction oil, and discovers that in the air injection development, NTC interval is not a disadvantageous factor but is an interval with active oxidation activity, and the existence of the narrow-fraction oil with NTC interval can have great beneficial influence on the whole reaction process of the air injection development of crude oil, promote the smooth progress of the air injection development, and greatly improve the success rate of the air injection development. The NTC interval in the negative temperature coefficient oxidation progression reaction between low temperature oxidation and high temperature oxidation is a key parameter characterizing crude oil oxidation activity. Based on this, the inventors propose the technical solution claimed by the present invention.
According to the technical scheme provided by the invention, the crude oil pseudo-component is constructed according to the flowability and whether the Negative Temperature Coefficient (NTC) interval between the low-temperature oxidation process and the high-temperature oxidation process exists, so that the pseudo-component combined with the NTC is obtained, the low-temperature, high-temperature and negative temperature coefficient oxidation process can be well reflected, and the whole oxidation reaction process can be well reflected. In addition, the invention has few types of the quasi-components formed in the technical scheme, is convenient for further researching the matching conditions of the crude oil with different quasi-components and the oxidation process to obtain the matching conditions with fewer relation parameters, is beneficial to simplifying the mathematical model for simulating and researching the on-site crude oil, obtains the required accurate conditions and control parameters, and realizes the smooth completion of air injection exploitation.
In the technical scheme provided by the invention, four pseudo-components capable of representing main oxidation reaction properties of crude oil in thermochemical flooding development are obtained based on crude oil of complex mixture. The respective pseudo-components can respectively and correspondingly simulate the performances in three oxidation processes of low temperature, negative temperature coefficient and high temperature in the development of thermochemical flooding:
(1) The four pseudo-components can simulate the low-temperature and high-temperature oxidation process, including coke formation due to low-temperature oxidation when the reservoir is heated and the oxygen intake is insufficient, pore blocking and subsequent oxygen entering into the pores are affected; when the temperature of the oxygen-enriched reservoir is not high, the combustion is unfavorable; when the oxygen intake is sufficient, the temperature is increased to a degree that the coke generated by the partial oxygenation reaction can be ignited and burned.
(2) The pseudo-component with NTC interval can simulate how to better utilize the oxidation process of negative temperature coefficient, for example, under the action of the additive, what temperature and oxygen inlet amount can make the component promote the coke, the coke and the heavy fraction remained around to enter high-temperature oxidation as soon as possible, and drive the crude oil of other pseudo-components around to generate high-temperature oxidation;
(3) The pseudo-composition without NTC interval and without fluidity can simulate the conditions of entering high temperature oxidation, i.e. what temperature and oxygen intake make this part of the oil undergo high temperature oxidation.
(4) The light components can also simulate thermal pyrolysis, i.e., the situation where the light components come out when heated to pyrolysis temperatures.
Furthermore, the existence of the quasi-component with the NTC interval can promote the full reaction process of the air injection development of crude oil, promote the smooth proceeding of the air injection development of gas drive, and greatly improve the success rate of the air injection development.
According to the technical scheme of the method for determining the air injection development reservoir based on the crude oil component analysis, the air injection development reservoir can be further screened based on whether crude oil contains the pseudo-component in the NTC interval, and the reservoir containing the crude oil with the pseudo-component in the NTC interval is selected as the air injection development reservoir for air injection development. In the air injection development process of the target reservoir, the mode that the simulated components with NTC intervals in the crude oil are beneficial to enabling the crude oil in the reservoir to smoothly enter a high-temperature combustion state greatly improves the on-site crude oil production amount, and the successful air injection development can be well guaranteed.
In short, the crude oil pseudo-component obtained by the crude oil pseudo-component obtaining method provided by the invention is beneficial to analyzing and exploring the influence of crude oil physical properties, oil reservoir physical properties, pore blocking, oxygen enrichment and fuel and gas amount on the development effect of injected air; when the method is applied to numerical simulation analysis of air injection development, the model calculation can be simplified, and the problems of overlong numerical simulation time, poor calculation stability and the like are avoided; the method can be effectively used for solving the problem of on-site crude oil extraction in air injection development. The method for determining the air injection development reservoir based on the crude oil component analysis is beneficial to promoting on-site air injection development to be carried out smoothly.
Drawings
FIG. 1 shows the thermal reaction characteristics of C20 carborane and dimethyl anthracene at 4.1 MPa.
Detailed Description
In order to make the objects, technical solutions and advantages of the embodiments of the present invention more clear, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention. It will be apparent that the described embodiments are some, but not all, embodiments of the invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to fall within the scope of the invention.
Example 1
The embodiment provides a crude oil quasi-component acquisition method and a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component acquired by the method.
The method for obtaining the crude oil pseudo-component in the embodiment comprises the following steps:
1) Collecting 1# crude oil (with the ground degassing oil viscosity of 540 mPa.s), and distilling the 1# crude oil to obtain a narrow fraction oil group of the 1# crude oil;
the distillation range temperature of each narrow fraction oil in the narrow fraction oil group is shown in Table 1;
2) Carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval (namely NTC interval); carrying out a flowability test at a reservoir temperature on each narrow-fraction oil in the narrow-fraction oil group to determine whether each narrow-fraction oil has flowability at the reservoir temperature (the narrow-fraction oil with the viscosity of not more than 500 mPas has flowability at the reservoir temperature, and the narrow-fraction oil with the viscosity of more than 500 mPas does not have flowability);
Wherein, the oxidation kinetics test adopts a rapid compressor to test the narrow fraction;
the results are shown in Table 1;
table 1 1 results of oxidation kinetics test of crude oil narrow cut with fast compressor
Wherein the equivalence ratio refers to the ratio of the amounts of air and the narrow-cut oil material;
the narrow distillates 1, 2, 3 and 4 have fluidity at the reservoir temperature, and the narrow distillates 5 and 6 have no fluidity at the reservoir temperature;
3) Obtaining a target crude oil pseudo-component based on whether the oxidation rate of each narrow-cut oil of the target crude oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at reservoir temperature;
mixing the narrow distillates having an oxidation rate having a negative temperature coefficient range and fluidity at reservoir temperature to form a target crude oil first pseudo-component; in this example, the oil consists of a narrow fraction oil 1 and a narrow fraction oil 2;
mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that is mobile at reservoir temperatures to form a target crude oil second pseudo-component; in this example consisting of narrow distillates 3, 4;
mixing the narrow distillates having an oxidation rate with a negative temperature coefficient range and no fluidity at reservoir temperature to form a target crude third pseudo-component; in this example consisting of a narrow fraction oil 5;
Mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that does not have fluidity at reservoir temperature to form a target crude fourth pseudo-component; in this example consisting of a narrow cut oil 6.
As can be seen from table 1, the narrow-cut oil reactivity with NTC interval has a distinct advantage over the reactivity of the narrow-cut oil without NTC interval.
The embodiment also provides a method for determining an air injection development reservoir based on crude oil component analysis, wherein the method comprises the following steps:
the crude oil quasi-component obtaining method provided by the embodiment is referred to for obtaining a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component;
the No. 1 crude oil contains a first quasi-component and a third quasi-component, and a reservoir where the No. 1 crude oil is located is used as an air injection development reservoir for air injection development.
In the process of air injection development of the reservoir where the No. 1 crude oil is located, the crude oil is smoothly combusted and enters a high-temperature zone, and air injection development is smoothly realized.
Example 2
The embodiment provides a crude oil quasi-component acquisition method and a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component acquired by the method.
The method for obtaining the crude oil pseudo-component in the embodiment comprises the following steps:
1) Collecting the No. 2 crude oil (the ground degassing oil viscosity is 5900 mPa.s), and distilling the No. 2 crude oil to obtain a narrow fraction oil group of the No. 2 crude oil;
the distillation range temperatures of the individual narrow distillates in the narrow-cut oil group are shown in Table 2;
2) Carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval (namely NTC interval); carrying out a flowability test at a reservoir temperature on each narrow-fraction oil in the narrow-fraction oil group to determine whether each narrow-fraction oil has flowability at the reservoir temperature (the narrow-fraction oil with the viscosity of not more than 500 mPas has flowability at the reservoir temperature, and the narrow-fraction oil with the viscosity of more than 500 mPas does not have flowability);
wherein, the oxidation kinetics test adopts a rapid compressor to test the narrow distillate oil; the results are shown in Table 2;
table 2 2 results of oxidation kinetics test of crude oil narrow cut with fast compressor
The narrow distillate 1, the narrow distillate 2 and the narrow distillate 5 have obvious low-temperature, negative-temperature coefficient and high-temperature three-stage oxidation characteristics, the reaction activity is strong, and the ignition delay is arranged in a negative-temperature coefficient interval;
the narrow distillates 1, 2 have fluidity at the reservoir temperature, and the narrow distillates 3, 4 and 5 have no fluidity at the reservoir temperature;
3) Obtaining a target crude oil pseudo-component based on whether the oxidation rate of each narrow-cut oil of the target crude oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at reservoir temperature;
mixing the narrow distillates having an oxidation rate having a negative temperature coefficient range and fluidity at reservoir temperature to form a target crude oil first pseudo-component; in this example consisting of a narrow fraction oil 1;
mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that is mobile at reservoir temperatures to form a target crude oil second pseudo-component; in this example consisting of a narrow fraction oil 2;
mixing the narrow distillates having an oxidation rate with a negative temperature coefficient range and no fluidity at reservoir temperature to form a target crude third pseudo-component; in this example consisting of a narrow cut oil 3;
mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that does not have fluidity at reservoir temperature to form a target crude fourth pseudo-component; in this example consisting of narrow distillates 4, 5.
As can be seen from table 2, the narrow-cut oil reactivity with NTC interval has a distinct advantage over the reactivity of the narrow-cut oil without NTC interval.
The embodiment also provides a method for determining an air injection development reservoir based on crude oil component analysis, wherein the method comprises the following steps:
the crude oil quasi-component obtaining method provided by the embodiment is referred to for obtaining a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component;
the reservoir where the 2# crude oil is located is subjected to air injection development in a conventional manner as an air injection development reservoir, specifically according to the air injection amounts shown in table 3, with the 2# crude oil containing both the first and third pseudo components.
In the conventional air injection development process of the reservoir where the No. 2 crude oil is located, the crude oil is smoothly combusted and enters a high-temperature zone, and air injection development is smoothly realized. Development index is shown in table 3.
Example 2 produced less oil during air injection development than example 1. The effect of each quasi-component in the oxidation process can be further simulated and analyzed to determine a proper exploitation method to control the oxidation process and be applied to actual exploitation; other methods may be employed to control the oxidation process; thus, the exploitation efficiency is improved, for example, the combustion temperature is controlled to be at the optimal combustion temperature, and thus, better exploitation effect can be obtained.
In order to better realize the air injection development of the reservoir where the No. 2 crude oil is located, the embodiment provides a novel air injection development reservoir determining method based on crude oil component analysis, wherein the method comprises the following steps:
the crude oil quasi-component obtaining method provided by the embodiment is referred to for obtaining a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component;
carrying out air injection development simulation experiments under different combustion temperature conditions on a reservoir where the No. 2 crude oil is located; the results are shown in Table 4; according to the simulation experiment result, determining the optimal combustion temperature, wherein the determined optimal combustion temperature is 450-500 ℃ and not higher than 550 ℃;
the No. 2 crude oil contains a first quasi-component and a third quasi-component, the reservoir where the No. 2 crude oil is located is used as an air injection development reservoir for air injection development for controlling the combustion temperature, specifically, the air injection development is carried out according to the air injection amount shown in the table 3, and the combustion temperature is maintained between 450 ℃ and 500 ℃ in the air injection development process.
In the air injection development process of controlling the combustion temperature of the reservoir where the No. 2 crude oil is located, the crude oil is smoothly combusted and enters a high-temperature zone, and air injection development is smoothly realized. Development index is shown in table 3.
As can be seen from Table 3, measures for controlling the oxidation process are taken to significantly improve the mining effect.
Injection and production index comparison during reservoir production field test where table 3 2# crude oil is located
TABLE 4 optimal combustion temperature data for thickened oil of EXAMPLE 4
Example 3
The embodiment provides a crude oil quasi-component acquisition method and a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component acquired by the method.
The method for obtaining the crude oil pseudo-component in the embodiment comprises the following steps:
1) Collecting 3# crude oil (ground degassing oil viscosity 21000 mPa.s), and distilling the 3# crude oil to obtain a narrow fraction oil group of the 1# crude oil;
the distillation range temperatures of the respective narrow distillates in the narrow-cut oil group are shown in table 3;
2) Carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval (namely NTC interval); carrying out a flowability test at a reservoir temperature on each narrow-fraction oil in the narrow-fraction oil group to determine whether each narrow-fraction oil has flowability at the reservoir temperature (the narrow-fraction oil with the viscosity of not more than 500 mPas has flowability at the reservoir temperature, and the narrow-fraction oil with the viscosity of more than 500 mPas does not have flowability);
wherein, the oxidation kinetics test is carried out by adopting a rapid compressor and an adiabatic acceleration calorimeter;
The results are shown in Table 5;
table 5 3 results of oxidation kinetics test of crude oil narrow cut with fast compressor
The No. 3 crude oil has almost no fraction below 200 ℃ and no fraction between 250 ℃ and 425 ℃, and has very little fraction in two distillation temperature ranges of 200 ℃ to 225 ℃ and 225 ℃ to 250 ℃ and can be ignored; the distillate oil at 200-225 ℃ has no NTC phenomenon; because of less distillation harvest, the distillate oil at 225-250 ℃ can not judge whether NTC interval exists or not;
the 3# crude oil cannot adopt the rapid compressor to carry out experiments under the restriction that the distillation temperature of the experimental oil is not higher than 300 ℃ in the prior stage; carrying out oxidation dynamics lumped characteristic test on other narrow-fraction oil of the 3# crude oil which cannot be tested by the rapid compressor by adopting an adiabatic acceleration calorimeter (ARC); in order to ensure the continuity and comparability of the results, firstly, carrying out a comparison experiment on the 1# crude oil and the 2# crude oil under the same temperature and pressure control condition by adopting an adiabatic acceleration calorimeter and a rapid compressor to obtain the same result, and confirming the comparability of two experimental devices to crude oil experiments;
carrying out oxidation kinetics test on 425-450 ℃ distillate oil of 3# crude oil and residual oil with distillation temperature higher than 505 ℃ and 3# crude oil by adopting an adiabatic acceleration calorimeter; 425-450 ℃ distillate oil of 3# crude oil, residual oil with distillation temperature higher than 505 ℃ and 3# crude oil all show three-stage oxidation characteristics of low temperature, negative temperature coefficient and high temperature; wherein, the distillate oil at 425-450 ℃ has low-temperature heat release at 150-180 ℃, the high-temperature heat release starts at 200 ℃, and has weaker ignition delay phenomenon between 180-200 ℃, and the continuous temperature interval of the ignition delay phenomenon is narrower; the residual oil with the distillation temperature of more than 505 ℃ has strong low-temperature reaction and strong ignition delay phenomenon, and obvious high-temperature reaction is only seen after the distillation temperature is 350 ℃; the low-temperature oxidation heat release of the 3# crude oil is 170-230 ℃, the high-temperature heat release starts from 350 ℃, and the continuous temperature interval of the ignition delay phenomenon is wider.
3) Obtaining a target crude oil pseudo-component based on whether the oxidation rate of each narrow-cut oil of the target crude oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at reservoir temperature;
mixing the narrow distillates having an oxidation rate having a negative temperature coefficient range and fluidity at reservoir temperature to form a target crude oil first pseudo-component; in this example, this component is absent.
Mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that is mobile at reservoir temperatures to form a target crude oil second pseudo-component; in this example, this component is absent.
Mixing the narrow distillates having an oxidation rate with a negative temperature coefficient range and no fluidity at reservoir temperature to form a target crude third pseudo-component; in this example the narrow distillates 1 and 2 consist.
Mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that does not have fluidity at reservoir temperature to form a target crude fourth pseudo-component; in this example, this component is absent.
As can be seen from Table 3, the narrow-cut oil with NTC interval had better reactivity.
The embodiment also provides a method for determining the exploitation mode based on the crude oil component analysis in the air injection development, wherein the method comprises the following steps:
The crude oil quasi-component obtaining method provided by the embodiment is referred to for obtaining a first quasi-component, a second quasi-component, a third quasi-component and a fourth quasi-component;
the 3# crude oil only contains a third pseudo component, and the reservoir where the 3# crude oil is located is used as an air injection development reservoir for air injection development.
In the process of air injection development of the reservoir where the No. 3 crude oil is located, the crude oil is smoothly combusted and enters a high-temperature zone, and air injection development is smoothly realized.
Example 2 produced less oil during the air injection development than when example 2 used conventional means for air injection production. The effect of each quasi-component in the oxidation process can be further simulated and analyzed to determine a proper exploitation method to control the oxidation process and be applied to actual exploitation; other methods may be employed to control the oxidation process; thus, the production efficiency is improved, for example, the combustion temperature is controlled to be at the optimum combustion temperature in the same manner as in example 2 to perform the oxidation reaction, so that a better production effect can be obtained.
According to the embodiment of the invention, the reservoirs where the crude oil with the NTC interval distillate oil is located are selected from the 1# oil, the 2# oil and the 3# oil for air injection exploitation, and finally the air injection exploitation can be smoothly carried out, so that the air injection exploitation of the reservoirs where the crude oil with the NTC interval distillate oil is located is illustrated, and the smooth air exploitation can be ensured.
The foregoing description of the preferred embodiments of the invention is not intended to limit the invention to the precise form disclosed, and any such modifications, equivalents, and alternatives falling within the spirit and scope of the invention are intended to be included within the scope of the invention.
Claims (10)
1. A crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having a negative temperature coefficient range for oxidation rate and fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
2. A crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having no negative temperature coefficient interval for oxidation rate and fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
3. A crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having a negative temperature coefficient range for oxidation rate and no fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
4. A crude oil mimetic composition, wherein the crude oil mimetic composition is formed by blending narrow distillates having no negative temperature coefficient interval for oxidation rate and no fluidity at reservoir temperature in a narrow distillate group of a target crude oil.
5. The crude oil mimetic composition of any one of claims 1-4 wherein,
the distillation range temperature range of the narrow distillate oil is 25 ℃;
the narrow-cut oil having a viscosity of not more than 500mpa·s at the reservoir temperature has fluidity, and the narrow-cut oil having a viscosity of more than 500mpa·s does not have fluidity.
6. The method for obtaining a crude oil mimetic composition as claimed in any one of claims 1 to 4, wherein the method comprises:
obtaining a narrow fraction oil group of target crude oil;
carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval or not; carrying out mobility test on each narrow fraction oil in the narrow fraction oil group at the reservoir temperature to determine whether each narrow fraction oil has mobility at the reservoir temperature;
obtaining a target crude oil pseudo-component based on whether the oxidation rate of each narrow-cut oil of the target crude oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at reservoir temperature; wherein,,
mixing the narrow distillates having an oxidation rate having a negative temperature coefficient range and fluidity at reservoir temperature to form a target crude oil first pseudo-component;
mixing the narrow distillates having an oxidation rate that does not have a negative temperature coefficient range and that is mobile at reservoir temperatures to form a target crude oil second pseudo-component;
Mixing the narrow distillates having an oxidation rate with a negative temperature coefficient range and no fluidity at reservoir temperature to form a target crude third pseudo-component;
the narrow distillates, which do not have a negative temperature coefficient range for oxidation rate and which do not have fluidity at reservoir temperature, are mixed to form the target crude fourth pseudo-component.
7. A method of determining a gas injection development reservoir based on analysis of crude oil composition, wherein the method comprises:
obtaining a narrow fraction oil group of crude oil of a target reservoir;
carrying out oxidation kinetics test on each narrow-fraction oil in the narrow-fraction oil group to determine whether the oxidation rate of each narrow-fraction oil has a negative temperature coefficient interval or not; carrying out mobility test on each narrow fraction oil in the narrow fraction oil group at the target reservoir temperature, and determining whether each narrow fraction oil has mobility at the target reservoir temperature;
determining a first, second, third and fourth pseudo-components of the target reservoir crude based on whether the oxidation rate of each narrow-cut oil has a negative temperature coefficient interval and whether each narrow-cut oil has fluidity at the target reservoir temperature; wherein the first crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate having negative temperature coefficient interval and fluidity at reservoir temperature, the second crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate not having negative temperature coefficient interval and fluidity at reservoir temperature, the third crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate having negative temperature coefficient interval and not fluidity at reservoir temperature, and the fourth crude oil quasi-component consists of crude oil narrow-cut oil with oxidation rate not having negative temperature coefficient interval and not fluidity at reservoir temperature;
When the target reservoir crude oil has a first mimetic component and/or a third mimetic component, the target reservoir is air-injected developed as an air-injected development reservoir.
8. The determination method according to claim 7, wherein,
the distillation range temperature range of the narrow distillate oil is 25 ℃;
the narrow-cut oil having a viscosity of not more than 500mpa·s at the reservoir temperature has fluidity, and the narrow-cut oil having a viscosity of more than 500mpa·s does not have fluidity.
9. The determination method according to claim 7, wherein the control of the crude oil oxidation process is achieved by controlling the combustion temperature to be in an optimal combustion temperature interval during the air injection development.
10. The determination method according to claim 9, the optimum combustion temperature being determined by:
injecting air under different combustion temperature conditions to develop a simulation experiment for a target reservoir;
and determining the optimal combustion temperature according to the simulation experiment result.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111676356.3A CN116411957A (en) | 2021-12-31 | 2021-12-31 | Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis |
| PCT/CN2022/102994 WO2023123977A1 (en) | 2021-12-31 | 2022-06-30 | Crude oil pseudocomponents, acquisition method thereof, and air injection reservoir development determination method based on crude oil component analysis |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111676356.3A CN116411957A (en) | 2021-12-31 | 2021-12-31 | Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116411957A true CN116411957A (en) | 2023-07-11 |
Family
ID=86997371
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111676356.3A Pending CN116411957A (en) | 2021-12-31 | 2021-12-31 | Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis |
Country Status (2)
| Country | Link |
|---|---|
| CN (1) | CN116411957A (en) |
| WO (1) | WO2023123977A1 (en) |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3322585B2 (en) * | 1996-12-18 | 2002-09-09 | 中部電力株式会社 | Mixing method of dust collection ash and drainage and drainage of heavy oil fuel fired boiler |
| CN108872294B (en) * | 2018-03-23 | 2021-01-29 | 中国石油天然气股份有限公司 | Method and device for determining ignition parameters of crude oil |
-
2021
- 2021-12-31 CN CN202111676356.3A patent/CN116411957A/en active Pending
-
2022
- 2022-06-30 WO PCT/CN2022/102994 patent/WO2023123977A1/en unknown
Also Published As
| Publication number | Publication date |
|---|---|
| WO2023123977A1 (en) | 2023-07-06 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102767356B (en) | Method for using combustion and vapor combination flooding to exploit thick oil | |
| CA1060784A (en) | Method of in situ recovery of viscous oils and bitumens | |
| CN101449027B (en) | Systems and methods for producing oil and/or gas | |
| CN105473811A (en) | Accelerated solvent-aided SAGD start-up | |
| Abu-Khamsin et al. | Reaction kinetics of fuel formation for in-situ combustion | |
| Belhaj et al. | Miscible oil recovery utilizing N2 and/or HC gases in CO2 injection | |
| CN103069105A (en) | Olefin reduction for in situ pyrolysis oil generation | |
| Hu et al. | Numerical simulation of mechanism of high-pressure air injection (HPAI) in light oil reservoirs | |
| Gates et al. | In situ upgrading of Llancanelo heavy oil using in situ combustion and a downhole catalyst bed | |
| Greaves et al. | Recent laboratory results of THAI and its comparison with other IOR processes | |
| CN103114830A (en) | Enriched-gas-drive water-altering-gas (WAG) injection method | |
| CN105239982B (en) | The method and apparatus of air requirements amount during a kind of determination combustion in situ | |
| CN116411957A (en) | Crude oil pseudo-component, acquisition method thereof and air injection development reservoir determination method based on crude oil component analysis | |
| Ilyasov et al. | Results of the first polymer flooding pilot at East-Messoyakhskoe oil field | |
| CN102132003A (en) | Systems and methods for producing oil and/or gas | |
| CN113012763B (en) | Crude oil oxidation reaction kinetic model building method based on four-group components | |
| Liu et al. | Effect of methanol additives on soot inhibition during n-decane pyrolysis | |
| Yuan et al. | Reaction schemes and characteristics in crude oil oxidation process using a TGA testing method | |
| Rios et al. | 3-d physical modeling of hybrid steam and oxygen injection for in-situ recovery of oil sands | |
| Apolinar Morales | An Analytical Study for High-Pressure Air Injection Applicability in a Potentially Candidate Sandstone Light Oil Reservoir | |
| Abutaqiya | Advances in Thermodynamic Modeling of Nonpolar Hydrocarbons and Asphaltene Precipitation in Crude Oils | |
| Alizadeh | A Robust Kinetic Model for Computer Modelling of In Situ Combustion Processes in Athabasca Oil Sands | |
| Fazlyeva et al. | In situ combustion | |
| Kök | Non-isothermal kinetic analysis and feasibilty study of medium grade crude oil field | |
| CN104865325B (en) | A kind of alternative fuel chemical reaction mechanism construction method similar based on molecular structure |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination |