Composition for increasing solubility of carbon dioxide in heavy oil, and preparation method and application thereof

Abstract

This invention relates to the field of crude oil extraction technology, specifically to a composition for improving the solubility of carbon dioxide in heavy oil, its preparation method, and its application. The composition comprises a silicon-containing amine compound of formula (I) and a polyether compound of formula (II); in formula (I), R1 and R2 are each independently selected from C1-C2. 20 hydrocarbon group, C1-C 20 The hydrocarbon siloxy group; R3 is selected from hydrogen, C1-C 20 hydrocarbon group, C1-C 20 The hydrocarbon siloxy group R4 is C3-C 10 The alkylene group; R5 and R6 are each independently selected from hydrogen, C1-C 24 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 31 The hydrocarbon group; in formula (II), R7 is selected from C1-C 20 hydrocarbon group, C1-C 20 The hydrocarbon siloxy group; R8, R8', and R8" are each independently selected from hydrogen or C1-C10 hydrocarbon groups; a, b, and c are the number of polyether segments, a = 1-50, b = 1-50, and c = 1-50; R9 is selected from hydrogen, C1-C10 hydrocarbon groups. 24 The hydrocarbon group or O = CR0', where R0' is selected from hydrogen, C1-C 31 The composition contains hydrocarbon groups. It can improve the efficiency of carbon dioxide-cooled heavy oil recovery.

Description

Technical Field

[0001] This invention relates to the field of crude oil extraction technology, specifically to a composition for improving the solubility of carbon dioxide in heavy oil, its preparation method, and its application. Background Technology

[0002] Heavy oil refers to crude oil with a high content of asphalt and gum and a high viscosity. In China, it is generally defined as crude oil with a relative density greater than 0.92 g / cm³. 3 Crude oil with a viscosity greater than 50 mPa·s at 20℃ is called heavy oil, also known as viscous oil. The American Petroleum Institute (API) defines heavy oil as oil with an API specific gravity less than 20 and a viscosity greater than 100 mPa·s. Currently, the main methods for extracting heavy oil are thermal recovery and cold recovery. Thermal recovery technology is a widely used extraction method, but its high cost and limited adaptability to reservoirs prevent its application in some complex heavy oil reservoirs. For low-permeability and water-sensitive heavy oil reservoirs, thermal recovery cannot achieve effective extraction due to multiple factors such as high crude oil viscosity, low permeability, and severe formation damage.

[0003] In the context of dual carbon, the development and application of CCUS (Carbon Capture, Utilization, and Storage) are receiving increasing attention. Among numerous carbon dioxide utilization projects, carbon dioxide flooding (CFD) has become one of the important technologies for enhanced oil recovery. The United States is the country that first and most extensively applied COD flooding trials. According to statistics, in 2014, the annual EOR (Extended Oil Recovery) production of COD flooding in the United States accounted for approximately 93% of the world's total annual EOR production. The carbon dioxide used comes from the tail gas of coal gasification plants and fertilizer plants, and most of it is extracted from natural carbon dioxide gas reservoirs. The enhanced oil recovery rate of COD-EOR miscible flooding ranges from 4% to 12%. As a traditional method for enhancing oil recovery, COD flooding can effectively improve injection capacity, avoid water sensitivity, and is one of the ways to improve the recovery rate of low-permeability reservoirs. The theoretical recovery rate of COD miscible flooding is over 90%, but it is mainly applicable to light oil reservoirs. Most heavy oil reservoirs are difficult to achieve COD miscible flooding, while COD huff and puff technology is currently one of the most economical and effective cold recovery methods for heavy oil reservoirs and has been applied in heavy oil reservoir production.

[0004] CN103510932A reports a cold recovery method for medium-deep, low-permeability heavy oil reservoirs with a permeability of 50 mD, a depth of 1500 m, and a maximum crude oil viscosity of 200,000 mPa·s. The method employs alternating injection of a microemulsion viscosity-reducing system and liquid carbon dioxide, with a total injection depth of 1000 m³ of the microemulsion viscosity-reducing system. 3 With 4 slugs and 400t of liquid carbon dioxide, and 8 slugs, the daily oil production per well exceeds 12t / d, achieving effective utilization. The patent does not report the specific chemical structure and properties of the microemulsion viscosity-reducing system.

[0005] Li Binfei et al. reported a successful case study of HDCS technology implementation in the Zheng 411 block of the Shengli Oilfield, an extra-heavy oil reservoir. This technology enabled the exploitation of an extra-heavy oil reservoir with a viscosity greater than 300,000 mPa / s (50℃), a burial depth greater than 1300 m, and an average oil layer thickness less than 8 m. Viscosity was reduced by injecting SLKF series oil-soluble viscosity reducers developed by the Shengli Petroleum Administration's Petroleum Development Center. By November 2006, 31 wells had been drilled, resulting in a cumulative increase in crude oil production of 13,268 tons, with an average increase of 428 tons per well.

[0006] Although the aforementioned reports have shown some success in using oil-soluble viscosity reducers to assist carbon dioxide extraction of heavy oil, these agents suffer from drawbacks such as high concentration requirements, high cost, and high operational risks. Furthermore, they require steam, significantly limiting their practical application. This invention describes a composition, preparation method, and application that efficiently and stably improves the solubility of carbon dioxide in heavy oil under reservoir conditions. Summary of the Invention

[0007] To overcome the problems of high concentrations, high costs, flammability, explosiveness, and high operational risks associated with existing chemical-assisted carbon dioxide extraction of heavy oil, this invention provides a composition, its preparation method, and its application. The composition incorporates silicon atoms, which effectively reduces surface tension and improves interfacial activity. It also contains heteroatoms such as nitrogen and oxygen, and the introduction of polyether fragments allows for flexible adjustment of the carbon dioxide affinity and heavy oil affinity balance. The composition has high boiling and flash points, ensuring its safety in use. This composition, which improves the solubility of carbon dioxide in heavy oil, can effectively increase the solubility of carbon dioxide in heavy oil even at relatively low concentrations, thus improving the efficiency of cold carbon dioxide extraction of heavy oil and showing great application potential.

[0008] To achieve the above objectives, a first aspect of the present invention provides a composition for improving the solubility of carbon dioxide in heavy oil, comprising a silicon-containing amine compound of formula (I) and a polyether compound of formula (II);

[0009]

[0010] In equation (I), R1 and R2 are each independently selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups;

[0011] R3 is selected from hydrogen, C1-C 20 hydrocarbon group, C1-C 20 hydrocarbon-based siloxy groups

[0012] R4 is C3-C 10 The alkylene group;

[0013] R5 and R6 are each independently selected from hydrogen, C1-C 24 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 31 hydrocarbon group;

[0014] In formula (II), R7 is selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups;

[0015] R8, R8', and R8" are each independently selected from hydrogen or C1-C. 10 hydrocarbon group;

[0016] a, b, and c represent the number of polyether fragments, where a = 1-50, b = 1-50, and c = 1-50.

[0017] R9 is selected from hydrogen, C1-C 24 The hydrocarbon group or O = CR0', where R0' is selected from hydrogen, C1-C 31 Hydrocarbon group.

[0018] A second aspect of the present invention provides a method for preparing the composition of the present invention, the method comprising:

[0019] The silicon-containing amine compound of formula (I) and the polyether compound of formula (II) are mixed evenly with a solvent, and the solvent is removed to obtain the composition.

[0020] The solvent is selected from one or more of small molecule alcohols, small molecule esters and aromatic hydrocarbons.

[0021] A third aspect of the present invention provides the application of the composition of the present invention in heavy oil carbon dioxide flooding or carbon dioxide huff and puff extraction.

[0022] Through the above technical solution, the introduction of silicon atoms into the composition of the present invention can effectively reduce surface tension and improve interfacial activity. The composition also contains heteroatoms such as nitrogen and oxygen. The introduction of polyether fragments gives the composition the ability to flexibly adjust the balance between carbon dioxide affinity and heavy oil affinity. The composition has a high boiling point and flash point, ensuring its safety in use. The composition can effectively increase the solubility of carbon dioxide in heavy oil at a low concentration, improving the efficiency of carbon dioxide cold extraction of heavy oil and showing great application prospects.

[0023] Attached Figures and Explanation of Figure Labels

[0024] Figure 1 For the apparatus for holding heavy oil and the composition, 1 is a quartz dish, 2 is a stir bar ①, and 3 is a brine bottle cap + stir bar ②. Detailed Implementation

[0025] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0026] In this invention, C1-C 24 hydrocarbon group, C1-C 20 hydrocarbon group, C1-C 16 hydrocarbon group, C1-C 10 The hydrocarbon groups include straight-chain hydrocarbon groups and branched hydrocarbon groups.

[0027] The first aspect of the present invention provides a composition for improving the solubility of carbon dioxide in heavy oil, comprising a silicon-containing amine compound of formula (I) and a polyether compound of formula (II);

[0028]

[0029] In equation (I), R1 and R2 are each independently selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups;

[0030] R3 is selected from hydrogen, C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups;

[0031] R4 is C3-C 10 The alkylene group;

[0032] R5 and R6 are each independently selected from hydrogen, C1-C 24 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 31 hydrocarbon group;

[0033] In formula (II), R7 is selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups;

[0034] R8, R8', and R8" are each independently selected from hydrogen or C1-C. 10 hydrocarbon group;

[0035] a, b, and c represent the number of polyether fragments, where a = 1-50, b = 1-50, and c = 1-50.

[0036] R9 is selected from hydrogen, C1-C 24 The hydrocarbon group or O = CR0', where R0' is selected from hydrogen, C1-C 31Hydrocarbon group.

[0037] The composition of this invention introduces silicon atoms, which can effectively reduce surface tension and improve interfacial activity. The composition also contains heteroatoms such as nitrogen and oxygen. The introduction of polyether fragments gives the composition the ability to flexibly adjust the balance between carbon dioxide affinity and heavy oil affinity. The composition has a high boiling point and flash point, ensuring its safety in use. The composition can effectively increase the solubility of carbon dioxide in heavy oil at a low concentration, improving the efficiency of carbon dioxide cold extraction of heavy oil and showing great application prospects.

[0038] According to a preferred embodiment of the present invention, in formula (I), R1 and R2 are each independently selected from C1-C 16 hydrocarbon group, C1-C 12 The hydrocarbon siloxy group, preferably selected from C1-C 10 hydrocarbon group, C1-C 10 Hydrocarbon-based siloxy groups.

[0039] According to a preferred embodiment of the present invention, in formula (I), R3 is selected from hydrogen, C1-C 16 hydrocarbon group, C1-C 20 The hydrocarbon siloxy group is preferably selected from hydrogen, C1-C 10 hydrocarbon group, C1-C 10 Substituted hydrocarbon groups, C1-C 10 Hydrocarbon-based siloxy groups.

[0040] According to a preferred embodiment of the present invention, in formula (I), R4 is a C3-C8 hydrocarbon group, preferably a C3-C6 hydrocarbon group.

[0041] According to a preferred embodiment of the present invention, in formula (I), R5 and R6 are each independently selected from hydrogen, C1-C2, C2-C2, C3-C4, C4-C6 ... 16 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 23 The hydrocarbon group; preferably, R5 and 6 are each independently selected from hydrogen, C1-C6. 12 The hydrocarbon group or O = CR0, where R0 is selected from C1-C 17 Hydrocarbon group.

[0042] According to a preferred embodiment of the present invention, in formula (II), R7 is selected from C1-C 16 hydrocarbon group, C1-C 16 Hydrocarbon siloxy groups; preferably selected from C1-C 10 hydrocarbon group, C1-C 10 Hydrocarbon-based siloxy groups.

[0043] According to a preferred embodiment of the present invention, in formula (II), R8, R8', and R8" are each independently selected from hydrogen or C1-C.10 The hydrocarbon group, preferably a C1-C3 hydrocarbon group.

[0044] According to a preferred embodiment of the present invention, in formula (II), a, b, and c are the number of polyether fragments, a = 1-50, b = 1-50, c = 1-50, preferably a = 1-20, b = 1-20, c = 1-20.

[0045] According to a preferred embodiment of the present invention, R9 is selected from hydrogen, C1-C 16 hydrocarbon group, C1-C 16 The substituted hydrocarbon group or O=CR0', where R0' is selected from hydrogen, C1-C 17 Hydrocarbon group.

[0046] In this invention, the ratio of the silicon-containing amine compound shown in formula (I) to the polyether compound shown in formula (II) can be selected in a wide range. According to a preferred embodiment of this invention, the molar ratio of the silicon-containing amine compound shown in formula (I) to the polyether compound shown in formula (II) is 1:(0.01-100), preferably 1:(0.1-10).

[0047] In this invention, silicon-containing amine compounds having the structure shown in formula (I) can all achieve the purpose of this invention. This invention does not have particular requirements for the preparation method of the silicon-containing amine compound shown in formula (I). According to a preferred embodiment of this invention, this invention provides a method for preparing the silicon-containing amine compound shown in formula (I) comprising:

[0048] (1) In the presence of a first catalyst, the compound shown in formula (III) is first contacted with acrylonitrile or CH2=CH-X to obtain the compound shown in formula (IV);

[0049] (2) Catalytic reduction or hydrolysis of the protecting group of the compound shown in formula (IV) yields the primary amine compound shown in formula (V); or

[0050] (3) Alkylation reaction of the primary amine compound shown in formula (V) yields the silicon-containing amine compound shown in formula (I);

[0051]

[0052] In equations (III), (IV), and (V), the definitions of R1, R2, and R3 are as described in the definition of equation (I);

[0053] X is R 10 -CN,R 10 It is a C1-C7 hydrocarbon group;

[0054] In equation (V), R4 is defined as described in equation (I);

[0055] or

[0056] In the presence of a second catalyst, the compound shown in formula (III) is subjected to a second contact with the unsaturated compound shown in formula (VI) to obtain the silicon-containing amine compound shown in formula (I').

[0057]

[0058] In formulas (VI) and (I'), R0 is selected from hydrogen, C1-C 31 R' is selected from at least one of the hydrocarbon groups, where R' is selected from hydrogen or C1-C3 hydrocarbon groups.

[0059] In this invention, in step (1), the range of types of the first catalyst and the second catalyst is relatively wide. According to a preferred embodiment of this invention, the first catalyst and the second catalyst are each independently a compound and / or a complex of at least one of platinum, palladium, rhodium, copper, iron, manganese, nickel, cobalt, and tungsten; preferably a compound and / or a complex of at least one of platinum, palladium, and rhodium, more preferably at least one of chloroplatinic acid, triphenylphosphine / chloroplatinic acid, alkali metal carbonate / chloroplatinic acid, and alkylalkenylsiloxane / chloroplatinic acid.

[0060] In this invention, taking triphenylphosphine / chloroplatinic acid as an example, the catalyst refers to triphenylphosphine, which is a compound with coordination effect, and can enhance the catalytic activity of chloroplatinic acid. Under experimental conditions, it has an enhancing effect on the catalytic activity of chloroplatinic acid; wherein, the mass ratio (or molar ratio) of the triphenylphosphine and the chloroplatinic acid is 1:0.1-10.

[0061] In this invention, the metal carbonate is used to enhance the catalytic activity of chloroplatinic acid. The range of types of metal carbonate is relatively wide. According to a preferred embodiment of this invention, the metal in the metal carbonate is selected from at least one of alkali metal elements. Preferably, the metal carbonate is selected from at least one of sodium carbonate, potassium carbonate, sodium bicarbonate, and potassium bicarbonate.

[0062] In this invention, in step (1), the conditions for the first contact and the second contact can be selected from a wide range. According to a preferred embodiment of this invention, the conditions for the first contact and the second contact each independently include: a temperature of 30-200℃, preferably 60-140℃; the contact time can be reasonably adjusted according to actual needs, preferably 2-24h, preferably 3-10h.

[0063] In this invention, in step (1), the ratio of the amount of the compound shown in formula (III), acrylonitrile, or CH2=CH-X first catalyst can be selected in a wide range. According to a preferred embodiment of this invention, the molar ratio of the compound shown in formula (III), acrylonitrile, or CH2=CH-X first catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001), preferably 1:(1-1.3):(0.000011-0.0001).

[0064] In this invention, the ratio of the compound shown in formula (III), the unsaturated compound shown in formula (VI), and the second catalyst can be selected over a wide range. According to a preferred embodiment of this invention, the molar ratio of the compound shown in formula (III), the unsaturated compound shown in formula (VI), and the second catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001), preferably 1:(1-1.3):(0.000011-0.0001).

[0065] According to a preferred embodiment of the present invention, step (1) is carried out in the presence of a solvent, preferably selected from one or more of benzene and isopropanol.

[0066] In this invention, there is no particular limitation on the amount of solvent used in step (1). According to a preferred embodiment of the invention, the amount of solvent used is such that the concentration of the compound shown in formula (II) is 20-90 wt%.

[0067] According to a preferred embodiment of the present invention, step (1) is carried out in an inert gas atmosphere, wherein the inert gas is selected from one or more of nitrogen and rare gases.

[0068] In this invention, step (1) further includes washing with water, separating oil and water, drying, and distilling after the reaction is completed to obtain the compound shown in formula (IV); wherein, washing with water, separating oil and water, drying, and distilling are all conventional separation and purification operations in the art, and there are no special limitations on the reaction conditions.

[0069] In this invention, in step (2), the catalytic reduction of the compound shown in formula (IV) is carried out. There are no particular limitations on the catalytic reduction conditions, as long as the compound shown in formula (V) can be obtained. According to a preferred embodiment of this invention, in step (2), the catalytic reduction is carried out by catalytic hydrogenation reduction, metal hydride catalytic reduction or supported metal catalytic reduction.

[0070] According to one embodiment of the present invention, the catalytic hydrogenation reduction is carried out in the presence of hydrogen and a metal catalyst, wherein the metal catalyst is selected from at least one of Raney nickel, Raney cobalt, Raney iron, and Raney copper.

[0071] According to a preferred embodiment of the present invention, the catalytic hydrogenation reduction conditions include: a temperature of 5-100°C and a pressure of 0.1-10.0 MPa.

[0072] According to a preferred embodiment of the present invention, the amount of the metal catalyst is 0.1 to 20 wt%, based on 100 wt% of the compound represented by formula (IV).

[0073] According to one embodiment of the present invention, the catalytic reduction of the metal hydride is carried out in the presence of a metal hydride catalyst, wherein the metal hydride catalyst is selected from a complex salt formed by a group IA ion and a group IIIA anhydride ion.

[0074] According to a preferred embodiment of the present invention, the conditions for the catalytic reduction of the metal hydride include: a temperature of -10 to 100°C;

[0075] According to a preferred embodiment of the present invention, the amount of the metal hydride catalyst is 4 to 12 mol, based on 1 mol of the compound shown in formula (IV).

[0076] According to one embodiment of the present invention, the supported metal catalytic reduction is carried out in the presence of a supported catalyst, the supported catalyst comprising a support and a metal component supported on the support, the metal component being selected from at least one of Pd, Pt and Rh, and the support being selected from at least one of carbon black, alumina, silica gel, diatomaceous earth and zeolite.

[0077] According to a preferred embodiment of the present invention, the amount of the supported catalyst is 0.01 to 5 wt%, based on 100 wt% of the compound represented by formula (IV).

[0078] According to a preferred embodiment of the present invention, the supported metal catalytic reduction conditions include a temperature of -10 to 50°C.

[0079] In step (2), after the reaction is complete, the catalyst is removed by filtration, the residue after filtration is dissolved by adding solvent, the oil and water are separated, and the solvent is removed to obtain the compound shown in formula (V).

[0080] In this invention, dichloromethane and / or trichloromethane are added in step (2).

[0081] In this invention, in step (2), oil-water separation and solvent removal are conventional separation and purification operations in the field, and there are no special limitations on the reaction conditions.

[0082] In this invention, the alkylation reaction can be a conventional alkylation reaction in the art. According to a preferred embodiment of this invention, in step (3), the alkylation reaction is carried out by a monohalogenated hydrocarbon-sodium hydroxide method, an aldehyde acid oxidation method, or an aldehyde catalytic hydrogenation method.

[0083] According to a preferred embodiment of the present invention, the aldehyde catalytic hydrogenation method comprises: reacting a primary amine compound of formula (V), R”CHO and H2 in a short-chain alcohol solvent to obtain a silicon-containing amine compound of formula (I).

[0084] According to a preferred embodiment of the present invention, the short-chain alcohol is selected from C1-C5 hydrocarbon groups or substituted hydrocarbon alcohols.

[0085] According to a preferred embodiment of the present invention, R” is selected from H, C1-C5 hydrocarbon groups or substituted hydrocarbon groups.

[0086] According to a preferred embodiment of the present invention, the molar ratio of the compound represented by formula (V): R”CHO:H2 is 1:(1-10):(1-20); the reaction conditions include: a temperature of 50-200℃; and a time of 1-10 hours.

[0087] In this invention, silicon-containing amine compounds having the structure shown in formula (II) can achieve the purpose of this invention. This invention does not have particular requirements for the preparation method of the silicon-containing amine compound shown in formula (II). According to a preferred embodiment of this invention, this invention provides a method for preparing the compound shown in formula (II), comprising:

[0088] It is obtained by polyetherification reaction using long-chain alcohols as raw materials; or

[0089] In the presence of a catalyst, the unsaturated compound-terminated as shown in formula (VII) reacts with R1'R2'R3'SiH to give the compound of formula (II').

[0090]

[0091]

[0092] R1'R2'R3' are C1-C6 hydrocarbon groups; R' is selected from hydrogen or C1-C3 hydrocarbon groups.

[0093] In this invention, the range of catalysts that can be selected is relatively wide. According to a preferred embodiment of this invention, the catalyst is a compound and / or a complex of at least one of platinum, palladium, rhodium, copper, iron, manganese, nickel, cobalt, and tungsten; preferably a compound and / or a complex of at least one of platinum, palladium, and rhodium; more preferably at least one of chloroplatinic acid, triphenylphosphine / chloroplatinic acid, alkali metal carbonate / chloroplatinic acid, and alkylalkenylsiloxane / chloroplatinic acid.

[0094] In this invention, the aforementioned metal carbonate is used to enhance the catalytic activity of chloroplatinic acid. The range of types of the aforementioned metal carbonate is relatively wide. According to a preferred embodiment of this invention, the metal in the aforementioned metal carbonate is selected from at least one of alkali metal elements. Preferably, the metal carbonate is selected from at least one of sodium carbonate, potassium carbonate, sodium bicarbonate, and potassium bicarbonate.

[0095] In this invention, the reaction conditions can be selected from a wide range. According to a preferred embodiment of this invention, the reaction conditions include: a temperature of 30-200℃, preferably 60-140℃; and a time of 2-24h, preferably 3-10h.

[0096] In this invention, the range of selectable amounts of R1'R2'R3'SiH, the compound shown in formula (VII), and the catalyst is relatively wide. According to a preferred embodiment of this invention, the molar ratio of R1'R2'R3'SiH, the compound shown in formula (VII), and the catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001), preferably 1:(1-1.3):(0.000011-0.0001).

[0097] A second aspect of the present invention provides a method for preparing the composition of the present invention, the method comprising:

[0098] The silicon-containing amine compound of formula (I) and the polyether compound of formula (II) are mixed evenly with a solvent, and the solvent is removed to obtain the composition.

[0099] The solvent is selected from one or more of small molecule alcohols, small molecule esters and aromatic hydrocarbons.

[0100] According to a preferred embodiment of the present invention, the small molecule alcohol is selected from C1-C5 alcohols or C1-C5 alcohols containing substituents, preferably methanol, ethanol, propanol or isopropanol.

[0101] According to a preferred embodiment of the present invention, the small molecule ester is selected from C1-C5 fatty acid esters or substituent-containing C1-C5 fatty acid esters, such as one or more selected from C1-C5 fatty acid methyl ester, C1-C5 fatty acid ethyl ester, C1-C5 fatty acid propyl ester, substituent-containing C1-C5 fatty acid methyl ester, substituent-containing C1-C5 fatty acid ethyl ester, and substituent-containing C1-C5 fatty acid propyl ester; preferably one or more selected from C1-C5 fatty acid methyl ester, C1-C5 fatty acid ethyl ester, substituent-containing C1-C5 fatty acid methyl ester, and substituent-containing C1-C5 fatty acid ethyl ester.

[0102] According to a preferred embodiment of the present invention, the aromatic hydrocarbon is selected from at least one of benzene, toluene, ethylbenzene, propylbenzene, xylene, diethylbenzene and methyl ethylbenzene, preferably at least one of benzene, toluene, ethylbenzene and xylene.

[0103] According to a preferred embodiment of the present invention, the amount of solvent used is such that the mass concentration of the silicon-containing amine compound shown in formula (I) and the polyether compound shown in formula (II) is 20-90 wt%.

[0104] A third aspect of this invention provides the application of the composition of this invention in heavy oil carbon dioxide flooding or carbon dioxide huff and puff extraction. The composition of this invention has high boiling and flash points, ensuring its safety in use; the composition can effectively increase the solubility of carbon dioxide in heavy oil even at low concentrations, improving the efficiency of carbon dioxide cold extraction of heavy oil and showing great application potential.

[0105] According to a preferred embodiment of the present invention, the composition is injected with or after being dissolved in carbon dioxide.

[0106] According to a preferred embodiment of the present invention, the injection amount of the composition is 0.01-5 wt% of carbon dioxide.

[0107] The present invention will now be described in detail with reference to specific embodiments. It should be noted that the following embodiments are only used to further illustrate the present invention and should not be construed as limiting the scope of protection of the present invention. Some non-essential improvements and adjustments made by those skilled in the art based on the content of the present invention are still within the scope of protection of the present invention.

[0108] It should also be noted that the various specific technical features described in the following embodiments can be combined in any suitable manner without contradiction. To avoid unnecessary repetition, the various possible combinations will not be described separately in this invention.

[0109] Furthermore, various embodiments of the present invention can be combined in any way, as long as they do not violate the spirit of the present invention. The resulting technical solutions are part of the original disclosure of this specification and also fall within the protection scope of the present invention.

[0110] Unless otherwise specified, the raw materials used in the examples and comparative examples are all disclosed in the prior art, such as those that can be directly purchased or prepared according to the preparation methods disclosed in the prior art.

[0111] The effect of the composition on improving the solubility of carbon dioxide in heavy oil was evaluated by the change rate of heavy oil mass (%). The change in volume and mass of heavy oil was calculated according to formula (1), and the change rate of heavy oil mass (%) was obtained according to formula (2) compared with the original heavy oil mass.

[0112] m (CO2) =ΔV×ρ (CO2)

[0113] Formula (1)

[0114] Heavy oil mass change rate (%) = m (CO2) ×100 / m (heavy oil)

[0115] Formula (2)

[0116] Where, m (CO2) : Mass of CO2 dissolved in heavy oil or mass of crude oil extracted, g; ΔV: Actual volume change of heavy oil, mL; ρ (CO2) CO2 density dissolved in heavy oil or crude oil density extracted, in g / cm³ 3 m (heavy oil) The mass of the added heavy oil is in grams.

[0117] Synthesis of the compound shown in Formula (IV') of Example 1

[0118]

[0119] Preparation Example 1-1

[0120] Under nitrogen protection, 1.5 × 10⁻⁶ mol of isopropanol solution containing 1 mol of trimethylsilane and H₂PtCl₆ / tetramethyldivinylsiloxane (molar ratio 1:0.5) was added to a dry pressure vessel. -5 1 mol (calculated as Pt) and 100 mL of dry benzene were stirred and mixed. The mixture was heated to 40 °C, and 1.2 mol of acrylonitrile was slowly added dropwise. The temperature was then raised to 90 °C, and the reaction was allowed to proceed for 2 h. After the reaction was complete, the reaction solution was washed with water to remove water-soluble substances, and the layers were separated. The layers were extracted three times with benzene, and the organic phases were combined. The mixture was dried over anhydrous MgSO4, and the solvent benzene was removed by vacuum distillation to obtain intermediate IV-1 (in formula (IV'), R1 = CH3, R2 = CH3, R3 = CH3). The content of IV-1 in the product was determined to be 92.7% by high performance liquid chromatography (HPLC).

[0121] Preparation Examples 1-2

[0122] Under nitrogen protection, 1.2 × 10⁻⁶ mol of trimethylsiloxydimethylsilane and PPh₃ / H₂PtCl₆ (molar ratio 1.6:1) isopropanol solution were added to a dry pressure vessel. -51 mol (calculated as Pt) and 100 mL of dry benzene were stirred and mixed. The mixture was heated to 40 °C, and 1.2 mol of acrylonitrile was added dropwise. The reaction was carried out slowly, and then the temperature was raised to 80 °C for 3.5 h. After the reaction was completed, the reaction solution was washed with water to remove water-soluble substances, and the layers were separated. The layers were extracted three times with benzene, and the organic phases were combined. The mixture was dried over anhydrous MgSO4, and the solvent benzene was removed by vacuum distillation to obtain intermediate IV-2 (in formula (IV'), R1 = (CH3)3SiO, R2 = CH3, R3 = CH3). The content of III-2 in the product was determined to be 91.9% by high performance liquid chromatography (HPLC).

[0123] Preparation Examples 1-3

[0124] Under nitrogen protection, 1.2 × 10⁻⁶ mol of dimethylphenylsilane and PPh₃ / H₂PtCl₆ (molar ratio 1.6:1) isopropanol solution were added to a dry pressure vessel. -5 1 mol (calculated as Pt) and 100 mL of dry benzene were stirred and mixed. The mixture was heated to 40 °C, and 1.2 mol of acrylonitrile was added dropwise. The heat was released slowly, and then the temperature was raised to 100 °C. The reaction was allowed to proceed for 3 h. After the reaction was complete, the reaction solution was washed with water to remove PPh3 / H2PtCl6 and isopropanol. The layers were separated and extracted three times with benzene. The organic phases were combined, dried over anhydrous MgSO4, and then the solvent benzene was removed by vacuum distillation to obtain intermediate III-3 (in formula (IV'), R1 = C6H5, R2 = CH3, R3 = CH3). The content of III-3 in the product was determined to be 93.2% by high performance liquid chromatography (HPLC).

[0125] Synthesis of the compound shown in Formula (V) in Example 2

[0126]

[0127] Preparation Example 2-1

[0128] In a stainless steel hydrogenation autoclave, 1.0 mol IV-1, 240 g 1,4-dioxane, and 0.24 g 5 wt% Pd-C were sequentially added. After purging with hydrogen five times, the autoclave was shut off, the stirrer was turned on, and hydrogen was introduced to a pressure of 1.2 MPa. The reaction temperature was controlled at 35 °C, and the reaction was continued for 2 hours when the reaction no longer absorbed hydrogen. After cooling, the reaction solution was filtered to remove the catalyst, and the solvent was evaporated. The residue was dissolved in dichloromethane, washed with water, and the organic phase was dried to remove dichloromethane, yielding intermediate V-1 (in formula (V), R1 = CH3, R2 = CH3, R3 = CH3, R4 = C3H6), with a yield of 93.9%.

[0129] Preparation Example 2-2

[0130] The method of Preparation Example 2-1 was followed, except that IV-2 was used as the reactant, and the other conditions were the same as in Preparation Example 2-1; intermediate V-2 (in formula (V), R1 = (CH3)3SiO, R2 = CH3, R3 = CH3, R4 = C3H6) was obtained with a yield of 91.5%.

[0131] Preparation Examples 2-3

[0132] The method of Preparation Example 2-1 was followed, except that IV-2 was used as the reactant, and the other conditions were the same as in Preparation Example 2-1; intermediate V-3 (in formula (V), R1 = C6H5, R2 = CH3, R3 = CH3, R4 = C3H6) was obtained with a yield of 92.2%.

[0133] Preparation Example 3: Synthesis of Silicon-Containing Amine Compounds

[0134] Preparation Example 3-1

[0135] 1.0 mol V-1, 200 g isopropanol, 6 g RancyNi and 3.5 mol butyraldehyde were added to a dry pressure reactor equipped with a stirrer. After deoxygenation, H2 was introduced and the reaction was carried out at 130 °C for reduction. After hydrogen absorption, the temperature was maintained for 3 hours. Post-treatment yielded silicon-containing amine compound I-1. The composition of the compound is shown in Table 1.

[0136] Preparation Example 3-2

[0137] Following the method of Preparation Example 3-1, except that V-2 (R1=(CH3)3SiO, R2=CH3, R3=CH3, R4=C3H6) was used instead of V-1, and the other conditions were the same as in Preparation Example 3-1, to obtain silicon-containing amine compound I-2. The composition of the compound is shown in Table 2.

[0138] Preparation Example 3-3

[0139] Following the method of Preparation Example 3-1, except that V-3 (R1 = C6H5, R2 = CH3, R3 = CH3, R4 = C3H6) was used instead of V-1, and the other conditions were the same as in Preparation Example 3-1, to obtain silicon-containing amine compound I-3. The composition of the compound is shown in Table 1.

[0140] Preparation Examples 3-4

[0141] 1.0 mol V-1 (R1=CH3, R2=CH3, R3=CH3, R4=C3H6), 200 g isopropanol, 3.5 g Rancy Ni and 3.0 mol hydroxypropanal were added to a dry pressure reactor equipped with a stirrer. After deoxygenation, H2 was introduced and the reaction was carried out at 100 °C for reduction. After hydrogen absorption, the temperature was maintained for 1 hour. Post-treatment yielded silicon-containing amine compound I-4. The composition of the compound is shown in Table 1.

[0142] Preparation Examples 3-5

[0143] 1.0 mol V-1 (R1=CH3, R2=CH3, R3=CH3, R4=C3H6), 200 g isopropanol, 2.1 g Rancy Ni and 1.1 mol isooctaldehyde were added to a dry pressure reactor equipped with a stirrer. After deoxygenation, H2 was introduced and the reaction was carried out at 140 °C for reduction. After hydrogen absorption, the temperature was maintained for another 2 hours. Post-treatment yielded silicon-containing amine compound I-5. The composition of the compound is shown in Table 1.

[0144] Table 1

[0145]

[0146] Preparation Examples 3-6

[0147]

[0148] Under nitrogen protection, 1.5 × 10⁻⁶ mol of trimethylsilane and H₂PtCl₆ / K₂CO₃ (molar ratio 1:0.2) isopropanol solution were added to a dry pressure vessel. -5 1 mol (calculated as Pt) and 100 mL of dry benzene were heated to 40 °C and activated for 60 min. Then, 1.1 mol of N-allyl octamide VI-1 (in formula (VI), R' = H, R0 = C7H) was added dropwise. 15 The benzene solution was slowly heated to 140℃ and reacted for 6 hours. After the reaction was completed, the reaction solution was washed with water to remove H2PtCl6 / K2CO3 and isopropanol. The layers were separated and extracted three times with benzene. The organic phases were combined, dried over anhydrous MgSO4, and then the solvent benzene was removed by vacuum distillation to obtain silicon-containing amine compound I-6. The composition of the compound is shown in Table 2.

[0149] Synthesis of the compound shown in Formula II in Example 4

[0150]

[0151] Preparation Example 4-1

[0152] In a dry reaction flask equipped with a water separator, 0.5 mol of isooctylphenol polyoxyethylene ether 3, 2.0 mol of finely granulated potassium hydroxide, and 500 mL of benzene were added sequentially. The mixture was heated under reflux until the amount of water carried over reached more than 90% of the theoretical value. 1.0 mol of acetyl chloride was slowly added dropwise, and reflux was continued for 8 hours after the addition was complete. After cooling, the reaction solution was poured into water, and the pH was adjusted to neutral with 10 wt% brine. The aqueous layer was separated, and the mixture was washed three times with saturated brine. The lower water layer was removed, and the solvent benzene and unreacted acetyl chloride were evaporated under reduced pressure to obtain polyether compound II-1, the composition of which is shown in Table 2.

[0153] Preparation Example 4-2

[0154] Following the method of Preparation Example 4-1, the difference is that isotridecyl alcohol polyoxyethylene ether 3 is replaced with molar isooctylphenol polyoxyethylene ether 3 to obtain polyether compound II-2, the composition of which is shown in Table 2.

[0155] Preparation Example 4-3

[0156] 1.0 mol of isooctyl alcohol and 8.5 g of potassium hydroxide were added to a 2 L pressure reactor equipped with a stirrer. The mixture was heated to 80–90 °C, and the vacuum system was turned on. The mixture was dehydrated under high vacuum for 1 hour. Then, the mixture was purged with nitrogen 3–4 times. The reaction temperature of the system was adjusted to 150 °C and 5.1 mol of propylene oxide was slowly introduced while controlling the pressure to ≤0.40 MPa. After the propylene oxide reaction was completed, the temperature was adjusted to 160 °C and 2.05 mol of butyl oxide was slowly introduced. After the reaction was completed, the temperature was lowered to 90 °C, and low-boiling substances were removed under vacuum. After cooling, the mixture was neutralized and dehydrated to obtain polyether compound II-3, the composition of which is shown in Table 2.

[0157] Preparation Example 4-4

[0158] In a pressure reactor, 0.5 mol of II-3, 2.0 mol of fine-particle potassium hydroxide, and 500 mL of benzene were added sequentially. The mixture was heated under reflux until the amount of water carried over reached more than 90% of the theoretical value. Then, 2.5 mol of monochloroethane was introduced to continue the reaction for 7 hours. After cooling, the reaction solution was poured into water, and the pH was adjusted to neutral with 10% brine. The aqueous layer was separated, and the mixture was washed three times with saturated brine. The lower water layer was removed to obtain polyether compound II-4, the composition of which is shown in Table 2.

[0159] Preparation Examples 4-5

[0160] ① Polymerization reaction: 1.0 mol of isooctanol and 10.5 g of potassium hydroxide were added to a 2L pressure reactor equipped with a stirrer. The mixture was heated to 85°C, and the vacuum system was activated. Dehydration was carried out under high vacuum for 1 hour. The system was then purged with nitrogen three times. The reaction temperature was adjusted to 140°C, and 2.05 mol of ethylene oxide was slowly introduced while controlling the pressure to ≤0.40 MPa. After the ethylene oxide reaction was complete, the temperature was adjusted to 150°C, and 10.3 mol of propylene oxide was slowly introduced. After the reaction was complete, the temperature was lowered to 90°C, and low-boiling substances were removed under vacuum. After cooling, neutralization and dehydration were performed to obtain an uncapped polyether compound (R7=C8H). 17 , R8=H, R8'=CH3, a=2, b=10).

[0161] ② Capping reaction: Same as the synthesis of II-4, except that an uncapped polyether compound (R7=C8H) is used. 17 (R8 = H, R8' = CH3, a = 2, b = 10), to obtain polyether compound II-5, the composition of which is shown in Table 2.

[0162] Table 2

[0163] serial number <![CDATA[R7]]> <![CDATA[R8]]> <![CDATA[R8’]]> <![CDATA[R8 ” ]]> a b c <![CDATA[R9]]> II-1 <![CDATA[C8H 17 C6H5]]> H - - 3 0 0 <![CDATA[CH3CO]]> II-2 <![CDATA[i-C 13 H 27 ]]> H - - 3 0 0 <![CDATA[CH3CO]]> II-3 <![CDATA[i-C8H 17 ]]> - <![CDATA[CH3]]> <![CDATA[C2H5]]> 0 5 2 H II-4 <![CDATA[i-C8H 17 ]]> - <![CDATA[CH3]]> <![CDATA[C2H5]]> 0 5 2 <![CDATA[C2H5]]> II-5 <![CDATA[i-C8H 17 ]]> H <![CDATA[CH3]]> - 2 10 0 <![CDATA[C2H5]]>

[0164] Preparation Examples 4-6

[0165]

[0166]

[0167] Under nitrogen protection, 1.5 × 10⁻⁶ mol of dimethylphenylsilane (IIO₃) and PPh₃ / H₂PtCl₆ (molar ratio 1.6:1) isopropanol solution were added to a dry pressure vessel. -5 1 mol (based on Pt) and 100 mL of dry benzene were stirred and mixed. The mixture was heated to 70 °C, and a benzene solution of 1 mol of olefin polyether VI01 (R'=H, R8=H, R8'=CH3, a=2, b=10, R9=C2H5) was slowly added dropwise. The reaction was continued at 70 °C for 3 h. After the reaction was completed, the reaction solution was washed with water to remove the aqueous residue, and the layers were separated. The layers were extracted three times with benzene, and the organic phases were combined, dried over anhydrous MgSO4, and then the solvent benzene was removed by vacuum distillation to obtain polyether compound II-6.

[0168] Preparation of compositions B01-B20 in Examples 1-20

[0169] Silicon-containing amine compounds I-1 to I-6 and polyether compounds II-1 to II-6 were mixed in a certain proportion and then dissolved in a solvent at a mass ratio of 0.5-2 wt%. The mixture was stirred and mixed evenly, and then the solvent was removed by vacuum evaporation to obtain compositions B01 to B20 that improve the solubility of carbon dioxide in heavy oil, as shown in Table 4.

[0170] Example 21

[0171] The difference from Example 1 is that no solvent was used in the preparation of the composition; specifically:

[0172] The composition of Example 1 was mixed in proportion and stirred until homogeneous to obtain B21.

[0173] Comparative Example 1

[0174] The silicon-containing amine compound I-1 was dissolved in a solvent at a mass ratio of 1 wt%, stirred and mixed evenly, and then the solvent was removed by pressure evaporation to obtain B01'.

[0175] Comparative Example 2

[0176] Polyether compound II-1 was dissolved in a solvent at a mass ratio of 1 wt%, stirred and mixed evenly, and then the solvent was removed by pressure to obtain B01.

[0177] Test Example 1

[0178] Using imaging methods in a supercritical visible volumetric system, the effect of the composition on improving the solubility of carbon dioxide in heavy oil was evaluated by observing the phase changes of the composition / carbon dioxide / heavy oil. (See...) Figure 1 Among them, 1 is a quartz dish, 2 is a stir bar ①, and 3 is a saline bottle cap + stir bar ②.

[0179] Experimental Procedure: Approximately 2.0g of crude oil and a certain proportion of the mixture were weighed into a quartz dish equipped with a stir bar and placed in the viewing system at its maximum volume. The dish was ventilated twice with carbon dioxide at <0.5MPa. The temperature was raised to the set point while stirring. The pressure inside the dish was adjusted to P0 = 1.0MPa ± 1.0MPa. Stirring was stopped, and the dish was allowed to stand for 1 hour. A photograph was taken, and the liquid level h was recorded. 0，视窗 Gradually increase pressure P i After stirring for 10 minutes each time, let it stand for 50 minutes, take a picture, and record the liquid level height h. i，视窗 The volume and mass changes of heavy oil were calculated to obtain the mass change rate (%) of heavy oil. The maximum mass change rate of heavy oil was used for relative comparison. The highest experimental pressure in the experiment was 25.0 MPa.

[0180] The experimental results for compositions B01-B20, B01', and B01"' are shown in Table 3. The experimental temperature was 50℃, the viscosity of the degassed heavy oil was 3835.4 mPa·s (50℃), and the specific gravity was 0.965 g / cm³. 3 .

[0181] Table 4

[0182]

[0183]

[0184] As shown in the table above, the composition effectively improves the solubility of CO2 in heavy oil, enhancing the efficiency of CO2 extraction. At a concentration of 2.0 wt%, the maximum mass change rate of heavy oil is 36.7–44.5%. Comparing the experimental results of B01', B01”, and B01, it can be seen that the silicon-containing amine compound I and polyether compound II have a good synergistic effect. The combination significantly improves the solubility of CO2 in heavy oil, with the maximum mass change rate being 2.5 and 3.0 times that of the single agents, respectively. The introduction of silicon and benzene ring groups is beneficial for enhancing the solubilization efficiency of the composition.

[0185] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A composition for improving the solubility of carbon dioxide in heavy oil, characterized in that, Including silicon-containing amine compounds of formula (I) and polyether compounds of formula (II); (AND), (II), In equation (I), R1 and R2 are each independently selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups; R3 is selected from hydrogen, C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups; R4 is C3-C 10 The alkylene group; R5 and R6 are each independently selected from hydrogen, C1-C 24 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 31 hydrocarbon group; In formula (II), R7 is selected from C1-C 20 hydrocarbon group, C1-C 20 Hydrocarbon-based siloxy groups; R8, R8' and R8” are each independently selected from hydrogen or C1-C10 hydrocarbon groups; a, b, and c represent the number of polyether fragments, where a = 1-50, b = 1-50, and c = 1-50. R9 is selected from hydrogen, C1-C 24 The hydrocarbon group or O=CR0', where R0' is selected from hydrogen, C1-C 31 Hydrocarbon group.

2. The composition according to claim 1, wherein, In equation (I), R1 and R2 are each independently selected from C1-C 16 hydrocarbon group, C1-C 12 hydrocarbon siloxy groups; and / or In formula (I), R3 is selected from hydrogen, C1-C 16 hydrocarbon group, C1-C 20 hydrocarbon siloxy groups; and / or In formula (I), R4 is a C3-C8 hydrocarbon group; and / or In formula (I), R5 and R6 are each independently selected from hydrogen, C1-C 16 The hydrocarbon group or O=CR0, where R0 is selected from hydrogen, C1-C 23 Hydrocarbon group.

3. The composition according to claim 2, wherein, In equation (I), R1 and R2 are each independently selected from C1-C 10 hydrocarbon group, C1-C 10 Hydrocarbon-based siloxy groups; In formula (I), R3 is selected from hydrogen, C1-C 10 hydrocarbon group, C1-C 10 Hydrocarbon-based siloxy groups; In formula (I), R4 is a C3-C6 hydrocarbon group; In formula (I), R5 and R6 are each independently selected from hydrogen, C1-C 12 The hydrocarbon group or O=CR0, where R0 is selected from C1-C 17 Hydrocarbon group.

4. The composition according to claim 1, wherein, In formula (II), R7 is selected from C1-C 16 hydrocarbon group, C1-C 16 hydrocarbon siloxy groups; and / or In formula (II), R8, R8', and R8" are each independently selected from hydrogen or C1-C6 hydrocarbon groups, n=1-3; and / or In formula (II), a, b, and c represent the number of polyether fragments, where a = 1-50, b = 1-50, and c = 1-50; and / or R9 is selected from hydrogen, C1-C 16 hydrocarbon group, C1-C 16 The substituted hydrocarbon group or O=CR0', where R0' is selected from hydrogen, C1-C 17 Hydrocarbon group.

5. The composition according to claim 4, wherein, In formula (II), R7 is selected from C1-C 10 hydrocarbon group, C1-C 10 Hydrocarbon-based siloxy groups; In equation (II), a = 1-20, b = 1-20, and c = 1-20.

6. The composition according to any one of claims 1-5, wherein, The molar ratio of the silicon-containing amine compound shown in formula (I) to the polyether compound shown in formula (II) is 1:(0.01-100).

7. The composition according to claim 6, wherein, The molar ratio of the silicon-containing amine compound shown in formula (I) to the polyether compound shown in formula (II) is 1:(0.1-10).

8. The composition according to claim 1, wherein, The method for preparing the silicon-containing amine compound shown in formula (I) includes: (1) In the presence of a first catalyst, the compound shown in formula (III) is reacted with acrylonitrile or The first contact yielded the compound shown in formula (IV); (2) The protecting group of the compound shown in formula (IV) is removed by catalytic reduction or hydrolysis to obtain the primary amine compound shown in formula (V); (3) Alkylation reaction of the primary amine compound shown in formula (V) yields the silicon-containing amine compound shown in formula (I); (III)、 (IV)、 (V)、 In formulas (III), (IV), and (V), the definitions of R1, R2, and R3 are as described in claim 1 or 2; X is R 10 -CN,R 10 It is a C1-C7 hydrocarbon group; In formula (V), R4 is defined as described in claim 1 or 2.

9. The composition according to claim 1, wherein, The method for preparing the silicon-containing amine compound shown in formula (I) includes: In the presence of a second catalyst, the compound shown in formula (III) is brought into a second contact with the unsaturated compound shown in formula (VI) to obtain the silicon-containing amine compound shown in formula (I'). (WE), (IN') In formulas (VI) and (I'), R0 is selected from hydrogen, C1-C 31 R' is selected from at least one of the hydrocarbon groups, where R' is selected from hydrogen or C1-C3 hydrocarbon groups.

10. The composition according to claim 8 or 9, wherein, The first catalyst and the second catalyst are each independently a compound and / or a complex of at least one of the elements platinum, palladium, rhodium, copper, iron, manganese, nickel, cobalt, and tungsten; The conditions for the first and second contacts are each independent of each other: temperature of 30-200℃ and time of 2-24h; and / or The molar ratio of the compound shown in formula (III), acrylonitrile, and the first catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001). The molar ratio of the compound shown in formula (III), the unsaturated compound shown in formula (VI), and the second catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001).

11. The composition according to claim 10, wherein, The first catalyst and the second catalyst are each independently compounds and / or complexes of at least one of platinum, palladium, and rhodium. The conditions for the first and second contacts are each independent of each other: temperature of 60-140℃ and time of 3-10h; The molar ratio of the compound shown in formula (III), acrylonitrile, and the first catalyst, based on the amount of metal element, is 1:(1-1.3):(0.000011-0.0001). The molar ratio of the compound shown in formula (III), the unsaturated compound shown in formula (VI), and the second catalyst, based on the amount of metal element, is 1:(1-1.3):(0.000011-0.0001).

12. The composition according to claim 11, wherein, The first catalyst and the second catalyst are each independently selected from at least one of chloroplatinic acid, triphenylphosphine / chloroplatinic acid, alkali metal carbonate / chloroplatinic acid, and alkylalkenylsiloxane / chloroplatinic acid, wherein the metal in the metal carbonate is selected from at least one alkali metal element.

13. The composition according to claim 8, wherein, In step (2), the catalytic reduction is carried out by catalytic hydrogenation reduction, metal hydride catalytic reduction or supported metal catalytic reduction; The catalytic hydrogenation reduction is carried out in the presence of hydrogen and a metal catalyst, wherein the metal catalyst is selected from at least one of Raney nickel, Raney cobalt, Raney iron, and Raney copper. The conditions for the catalytic hydrogenation reduction include: a temperature of 5-100℃ and a pressure of 0.1-10.0 MPa; or The catalytic reduction of the metal hydride is carried out in the presence of a metal hydride catalyst, which is selected from a complex salt formed by a group IA ion and a group IIIA anhydride ion. The conditions for the catalytic reduction of the metal hydride include: a temperature of -10 to 100°C; or The supported metal catalytic reduction is carried out in the presence of a supported catalyst, which comprises a support and a metal component supported on the support. The metal component is selected from at least one of Pd, Pt, and Rh, and the support is selected from at least one of carbon black, alumina, silica gel, diatomaceous earth, and zeolite; and / or The conditions for the supported metal catalytic reduction include: a temperature of -10 to 50°C; and / or In step (3), the alkylation reaction is carried out by a monohalogenated hydrocarbon-sodium hydroxide method, an aldehyde acid oxidation method, or an aldehyde catalytic hydrogenation method; The aldehyde catalytic hydrogenation method includes: reacting the primary amine compound shown in formula (V), R”CHO and H2 in a short-chain alcohol solvent to obtain the silicon-containing amine compound shown in formula (I); The short-chain alcohol is selected from C1-C5 hydrocarbon alcohols or substituted hydrocarbon alcohols; "R" is selected from H, C1-C5 hydrocarbon group or substituted hydrocarbon group; The compound represented by formula (V) has a molar ratio of R”CHO:H2 of 1:(1-10):(1-20); the reaction conditions include a temperature of 50-200℃ and a time of 1-10 hours.

14. The composition according to claim 13, wherein, In step (2), the amount of the metal catalyst is 0.1~20 wt%, based on 100 wt% of the compound shown in formula (IV); The amount of the metal hydride catalyst is 4 to 12 mol, based on the amount of 1 mol of the compound shown in formula (IV). The amount of the supported catalyst is 0.01 to 5 wt%, based on 100 wt% of the compound shown in formula (IV).

15. The composition according to any one of claims 1-5, wherein, The preparation method of the compound shown in formula (II) includes: It is obtained by polyetherification reaction using long-chain alcohols as raw materials.

16. The composition according to any one of claims 1-5, wherein, The preparation method of the compound shown in formula (II) includes: In the presence of a catalyst, the unsaturated compound-terminated as shown in formula (VII) reacts with R1'R2'R3'SiH to obtain the polyether compound shown in formula (II'); (VII) (II’), R1'R2'R3' are C1-C6 hydrocarbon groups; R' is selected from hydrogen or C1-C3 hydrocarbon groups.

17. The composition according to claim 16, wherein, The catalyst is a compound and / or a complex of at least one of the elements platinum, palladium, rhodium, copper, iron, manganese, nickel, cobalt, and tungsten. The reaction conditions include: a temperature of 30-200℃ and a time of 2-24h; The molar ratio of the catalyst, R1', R2', R3', SiH, the compound shown in formula (VII), and the catalyst, based on the amount of metal element, is 1:(1-2):(0.00001-0.001).

18. The composition according to claim 17, wherein, The catalyst is a compound and / or a complex of at least one of platinum, palladium, and rhodium. The reaction conditions include: a temperature of 60-140℃ and a time of 3-10h; The molar ratio of the catalyst, R1', R2', R3', SiH, the compound shown in formula (VII), and the catalyst, based on the amount of metal element, is 1:(1-1.3):(0.000011-0.0001).

19. The composition according to claim 17, wherein, The catalyst is at least one of chloroplatinic acid, triphenylphosphine / chloroplatinic acid, alkali metal carbonate / chloroplatinic acid, and alkylalkenylsiloxane / chloroplatinic acid, wherein the metal in the metal carbonate is selected from at least one alkali metal element.

20. A method for preparing the composition according to any one of claims 1-19, characterized in that, The method includes: The silicon-containing amine compound of formula (I) and the polyether compound of formula (II) are mixed evenly with a solvent, and the solvent is removed to obtain the composition. The solvent is selected from one or more of small molecule alcohols, small molecule esters and aromatic hydrocarbons.

21. The preparation method according to claim 20, wherein, The small molecule alcohol is selected from C1-C5 alcohols or C1-C5 alcohols containing substituents; The small molecule ester is selected from C1-C5 fatty acid methyl esters, fatty acid ethyl esters, or C1-C5 fatty acid methyl esters or C1-C5 fatty acid ethyl esters containing substituents. The aromatic hydrocarbon is selected from at least one of benzene, toluene, ethylbenzene, propylbenzene, xylene, diethylbenzene, and methyl ethylbenzene; and / or The amount of solvent used is such that the mass concentration of the silicon-containing amine compound shown in formula (I) and the polyether compound shown in formula (II) is 20-90 wt%.

22. The use of the composition according to any one of claims 1-19 in heavy oil carbon dioxide flooding or carbon dioxide huff and puff extraction.

23. The application according to claim 22, wherein, The composition is injected with or after being dissolved in carbon dioxide.

24. The application according to claim 23, wherein, The injection amount of the composition is 0.01-5 wt% of carbon dioxide.

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