CN113773824A - Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof - Google Patents

Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof Download PDF

Info

Publication number
CN113773824A
CN113773824A CN202010520565.8A CN202010520565A CN113773824A CN 113773824 A CN113773824 A CN 113773824A CN 202010520565 A CN202010520565 A CN 202010520565A CN 113773824 A CN113773824 A CN 113773824A
Authority
CN
China
Prior art keywords
hydrogen
ether
formula
hydroxy
viscosity
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.)
Granted
Application number
CN202010520565.8A
Other languages
Chinese (zh)
Other versions
CN113773824B (en
Inventor
沈之芹
林吉生
吴春芳
何秀娟
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Original Assignee
China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China Petroleum and Chemical Corp, Sinopec Shanghai Research Institute of Petrochemical Technology filed Critical China Petroleum and Chemical Corp
Priority to CN202010520565.8A priority Critical patent/CN113773824B/en
Publication of CN113773824A publication Critical patent/CN113773824A/en
Application granted granted Critical
Publication of CN113773824B publication Critical patent/CN113773824B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Images

Classifications

    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
    • C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C08G65/2603—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen
    • C08G65/2606—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups
    • C08G65/2612—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing oxygen containing hydroxyl groups containing aromatic or arylaliphatic hydroxyl groups
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08G—MACROMOLECULAR COMPOUNDS OBTAINED OTHERWISE THAN BY REACTIONS ONLY INVOLVING UNSATURATED CARBON-TO-CARBON BONDS
    • C08G65/00—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule
    • C08G65/02—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring
    • C08G65/26—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds
    • C08G65/2618—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing nitrogen
    • C08G65/2621—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing nitrogen containing amine groups
    • C08G65/2627—Macromolecular compounds obtained by reactions forming an ether link in the main chain of the macromolecule from cyclic ethers by opening of the heterocyclic ring from cyclic ethers and other compounds the other compounds containing nitrogen containing amine groups containing aromatic or arylaliphatic amine groups
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09K—MATERIALS FOR MISCELLANEOUS APPLICATIONS, NOT PROVIDED FOR ELSEWHERE
    • C09K8/00—Compositions for drilling of boreholes or wells; Compositions for treating boreholes or wells, e.g. for completion or for remedial operations
    • C09K8/58—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids
    • C09K8/588—Compositions for enhanced recovery methods for obtaining hydrocarbons, i.e. for improving the mobility of the oil, e.g. displacing fluids characterised by the use of specific polymers
    • 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
    • E21B43/164—Injecting CO2 or carbonated water

Landscapes

  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Geology (AREA)
  • Mining & Mineral Resources (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Health & Medical Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Fluid Mechanics (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Environmental & Geological Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Materials Engineering (AREA)
  • Lubricants (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention discloses a thickened oil viscosity-reducing synergistic composition, a preparation method and an application thereof, wherein the thickened oil viscosity-reducing synergistic composition comprises at least one of organic matters shown in a formula (I) and a fat synergist:
Figure DDA0002531051980000011
R1and R2Independently selected from hydrogen, C1～C32Or C is a hydrocarbon group1～C32Substituted hydrocarbyl, ester, hydroxyl, amino or alkoxy groups of (a); r3、R4And R5Each independently selected from hydroxy, hydrogen orAn alkyl group; r6Is selected from C1～C24Or C is a hydrocarbon group1～C24Substituted hydrocarbyl groups of (a); a is 0-50, b is 0-50, c is 0-50, and a, b and c are not 0 at the same time; d is 0 or 1; j is 0, 1 or 2. The composition is used for the production of heavy oil reservoirs with the formation temperature of 30-100 ℃ and the crude oil viscosity of 30,000-100,000 mPa.s.

Description

Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof
Technical Field
The invention belongs to the field of thickened oil viscosity reduction, and particularly relates to a thickened oil viscosity reduction synergistic composition and a preparation method and application thereof.
Background
The thickened oil refers to crude oil with high content of asphaltene and colloid and high viscosity. The relative density is usually more than 0.92g/cm3(20 ℃) and the underground viscosity of the crude oil is more than 50 mPas, which is called thick oil and also called heavy oil. At present, the exploitation modes of the thickened oil mainly comprise cold exploitation and hot exploitation. Wherein the thermal recovery mode comprises: steam flooding, steam stimulation, Steam Assisted Gravity Drainage (SAGD); the cold mining method comprises the following steps: polymer flooding, surfactant flooding, foam flooding, solvent extraction (VAPEX), microbial flooding, and the like. For extra-thick oil and ultra-thick oil with the viscosity of more than 10,000mPa.s, a development mode of thermal recovery is often adopted.
According to data of the United states geological exploration service (USGS), the thick oil reserves are about 33960 hundred million barrels in the world, and the thick oil resources are abundant. When the oil reservoir is buried deeply, the reservoir is thin, the oil reservoir characteristics are not good, and the thermal recovery method is not suitable for recovery, the non-thermal recovery method can be considered for recovery, and the preferred method is to carry out carbon dioxide flooding. Talbi et al studied the change in physical properties of the thick oil after saturation with carbon dioxide through laboratory experiments, tested the thick oil in south Soviet, Kansas, and northeast of Okla, studied the physical properties of the crude oil and determined the curves of the viscosity, density, saturation, and expansion coefficient of the crude oil as a function of temperature and pressure. The depth of the heavy oil reservoir of the Bati Raman oil field is about 1310 meters, after primary oil recovery, the reservoir pressure is reduced from 12410KPa to 2758KPa, and the recovery rate is about 1.5 percent. Since the Dodan carbon dioxide field was found about 88 km away from the reservoir. Thus, 33 wells of 1200 acres area in the west of the Bati Raman field began conducting the carbon dioxide flooding pilot test in 3 months 1986. Initially in the form of steam throughput. In 1988, continuous injection of carbon dioxide was selected as the final solution by indoor studies, numerical simulations and in view of economic efficiency. Firstly, the process is carried outThe experiment and the scale are enlarged, and 954m is reached in the third year3Oil production per day, and reached 1669m by the fifth year3And d, oil production and better exploitation effect.
After about 20 years, Babadagli et al conducted feasibility studies on the conversion of carbon dioxide flooding into steam flooding of the heavy oil reservoir in the Bati Raman Turkey block. Experimental results show that the conversion of carbon dioxide flooding into steam flooding at the later stage is an economical and reasonable scheme. It was found by fitting that zones with higher vertical permeability are particularly suitable for this approach. The oil layer is heated by injecting steam, so that the viscosity of the thick oil is reduced, and the fluidity of the thick oil is increased. When the temperature rises, carbon dioxide is released from the thickened oil to play a role of dissolved gas flooding, so that the crude oil recovery rate is improved.
China has rich thickened oil resources, which mainly comprises a single temple oil field, a victory lump three region, a haoqiao oil field, an island oil field and the like of a victory oil field, a nine region, a hexaeast region, a red mountain tip oil field and a Fengcheng thickened oil region of Craya, an eosin one region, a happy ridge thickened oil region and a high rising oil field of a Liaohe oil field, a shaft building oil field, an ancient city oil field and the like of a Henan oil field, a jujube garden oil field, a Yangsu oil field and the like of a Hongkong oil field. Wangchunzhi et al designed a three-dimensional large-sized core displacement experimental device for simulating the HDCS flooding process, monitoring the pressure and temperature conditions in the injection, soaking and recovery stages, and providing a laboratory simulation means for the exploitation of thick oil. Experiments were performed using victory oil field simulated oil and SLKF series oil soluble viscosity depressants. Experiments show that when the HDCS huff and puff experiment is carried out to the sixth period, the recovery water content reaches 85%, the oil reservoir pressure is reduced to be below 5MPa, the condition of transferring to steam flooding is achieved, then steam flooding is used, and meanwhile profile control agents are used for plugging a high-permeability zone, so that the recovery ratio can be improved.
Although carbon dioxide and steam flooding are adopted to produce thick oil to achieve certain effects in the reports, the existing chemical agent is weak in time capability of shortening carbon dioxide saturated thick oil, poor in effect of synergistically reducing viscosity of thick oil, and unstable in structure in subsequent steam flooding, so that the application of the chemical agent is greatly limited. The invention relates to a thickened oil viscosity-reducing synergistic composition with a stable structure in a thickened oil recovery process, and a preparation method and application thereof.
Disclosure of Invention
The invention provides a thickened oil viscosity-reducing composition in order to solve the problems of high use concentration of chemical agents and low carbon dioxide solubilization rate in the prior art. The thickened oil viscosity-reducing synergistic composition has strong action capacity with thickened oil due to the fat/aromatic oleophilic chain segment and heteroatom in the molecular structure, has good carbon dioxide-philic performance, is easy to adsorb on a carbon dioxide thickened oil interface, improves the mixing efficiency of carbon dioxide and thickened oil, effectively shortens the dissolving time of carbon dioxide in the thickened oil, is the viscosity-reducing synergistic composition with the carbon dioxide content of 1%, 2% and 4%, has the maximum carbon dioxide solubilization rates of 444.7%, 670.3% and 863.9%, and has good application prospect of improving the recovery ratio.
The invention aims to provide a thickened oil viscosity-reducing synergistic composition, which comprises at least one of organic matters shown in a formula (I) and a fat synergist:
Figure BDA0002531051960000031
in the formula (I), R1And R2Independently selected from hydrogen, C1～C32A hydrocarbon group of1～C32Substituted hydrocarbyl, ester, hydroxyl, amino or alkoxy groups of (a); and/or, R3、R4And R5Each independently selected from hydroxy, hydrogen or alkyl; and/or, R6Is selected from C1～C24Or C is a hydrocarbon group1～C24Substituted hydrocarbyl groups of (a); and/or, a is 0-50, b is 0-50, c is 0-50, and a, b and c are not 0 at the same time; and/or, d ═ 0 or 1; and/or, j ═ 0, 1, or 2.
In a preferred embodiment, the fatty synergist is selected from at least one of fatty alcohols, fatty alcohol ethers, fatty amines, fatty amine ethers and fatty acid esters.
In a further preferred embodiment, the fatty alcohol is selected from C1～C18The alcohol of (1); and/or, the fatThe alcohol ether is selected from C1～C18Alcohol ethers of (1); and/or the fatty amine is selected from C1～C24An amine of (a); and/or the fatty amine ether is selected from C1～C24Amine polyether of (a); and/or the ether in the fatty alcohol ether and the fatty amine ether is at least one of polyoxyethylene ether, polyoxypropylene ether and polyoxybutylene ether; and/or the fatty acid ester is C1～C18At least one of acid esters.
In a still further preferred embodiment, the fat-based potentiator is selected from C1～C12Fatty alcohol of (2), C1～C12Fatty alcohol ether of (C)1～C18Fatty amine of (2), C1～C18Fatty amine ether of (C)1～C12At least one fatty acid ester.
The composite compound prepared by the invention has a flexible and adjustable structure, has good affinity effect on fatty substances and aromatic substances in the thickened oil by introducing oxygen atoms, nitrogen atoms and benzene ring groups, is beneficial to reducing the viscosity of the thickened oil, enhances the carbon dioxide affinity of the composite by the Lewis acid-base action of heteroatoms such as oxygen and nitrogen in the composite and carbon dioxide, has the amphiphilic characteristic of affinity to the thickened oil and the carbon dioxide affinity, can strengthen the interaction between the carbon dioxide and the thickened oil, and can greatly reduce the dosage of the conventional chemical agent, thereby effectively starting the thickened oil.
In a preferred embodiment, in formula (I), R1And R2Each independently selected from hydrogen and C1～C28A hydrocarbon group of1～C28Substituted hydrocarbyl, alkoxy, ester, amine or hydroxyl groups;
preferably, the alkoxy group is OR7，R7Is (CHR)0)eH，R0Is hydrogen, methyl or ethyl, e is any integer of 1-12; and/or the ester group is COOR8，R8Is (CHR'0)fH，R’0Is hydrogen, methyl or ethyl, and f is any integer of 1-18.
In a further preferred embodimentWherein in the formula (I), R1And R2Selected from hydrogen, C1～C18A hydrocarbon group of1～C18Substituted hydrocarbyl of (2), COO (CHR'0)fH or amino, wherein R'0Is hydrogen or methyl, and f is an integer of 1 to 12.
In a preferred embodiment, in formula (I), R3、R4And R5Each independently selected from hydroxy, hydrogen or C1～C8Alkyl group of (1).
In a further preferred embodiment, in formula (I), R3、R4And R5Each independently selected from hydroxy, hydrogen or C1～C4Alkyl group of (1).
In a still further preferred embodiment, in formula (I), R3、R4And R5Each independently selected from hydroxy, hydrogen or C1～C2Alkyl group of (1).
In a preferred embodiment, in formula (I), R6Is selected from C1～C24Is preferably selected from C1～C20More preferably from C1～C16A hydrocarbon group of (1).
In a preferred embodiment, in formula (I), a is 0 to 30, b is 0 to 30, c is 0 to 30, and a, b and c are not 0 at the same time; and/or, j ═ 0, 1, or 2.
Wherein a, b and c are the addition number of polyether segments, and j is the number of phenolic ether groups.
In a preferred embodiment, in the composition, the mass ratio of the fat synergist to the organic matter represented by the formula (I) is 1: (0-200) and does not contain 0.
In a further preferred embodiment, in the composition, the mass ratio of the fat synergist to the organic matter represented by the formula (I) is 1: (0.1-50).
In a further preferred embodiment, in the composition, the mass ratio of the fat synergist to the organic matter represented by the formula (I) is 1: (0.1-20).
In a preferred embodiment, the composition optionally further comprises a pour point depressant and/or a viscosity reducing agent.
In a further preferred embodiment, the composition optionally further comprises at least one of an ethylene acrylate copolymer, an acrylate long carbon chain ester copolymer, an anionic surfactant, a nonionic surfactant, and a built surfactant.
Wherein the pour point depressant and viscosity reducing agent may also be selected from other types commonly used in the art.
The second object of the present invention is to provide a process for preparing the thickened oil viscosity-reducing composition of the first object of the present invention, which comprises: obtaining an organic matter shown in a formula (I), and then mixing the organic matter with a fat synergist to obtain the thickened oil viscosity-reducing composition; wherein, when j is 1 or 2, the organic compound represented by formula (I) is obtained as follows:
step 1, taking a compound shown as a formula (II), optionally reacting with a halogenated epoxy compound, and carrying out aftertreatment to obtain a glycidyl ether intermediate;
step 2, in the presence of a catalyst, reacting the compound shown in the formula (II) or the glycidyl ether intermediate with an epoxy compound to obtain a polyether intermediate product shown in the formula (III);
and 3, reacting the polyether intermediate product with a blocking agent in the presence of a catalyst to obtain the organic matter shown in the formula (I).
Figure BDA0002531051960000051
Wherein, in formula (II) and formula (III), j is 1 or 2.
When j is 0, the steps 1 to 3 are not required, and the organic compound represented by formula (I) when j is 0 is a compound represented by formula (II) when j is 0 (represented by formula (IV)), which can be purchased and used directly from the market, or can be obtained by a common etherification, esterification, or the like reaction to obtain R1、R2Organic compounds which are ether or ester substituents.
In formula (II) and formula (III):
R1and R2Each independently selected from hydrogen and C1～C32Or C is a hydrocarbon group1～C32The substituted hydrocarbyl, ester, hydroxyl, amino or alkoxy of (A) is preferably selected from hydrogen, C1～C28A hydrocarbon group of1～C28Substituted hydrocarbyl, alkoxy, ester, amine or hydroxyl groups; preferably, the alkoxy group is OR7，R7Is (CHR)0)eH，R0Is hydrogen, methyl or ethyl, e is any integer of 1-12; and/or the ester group is COOR8，R8Is (CHR'0)fH，R’0Is hydrogen, methyl or ethyl, and f is any integer of 1-18; more preferably, R1And R2Each independently selected from hydrogen and C1～C18A hydrocarbon group of1～C18Substituted hydrocarbyl of (2), COO (CHR'0)fH or amino, R'0Is hydrogen or methyl, f is an integer of 1-12; and/or
R3、R4And R5Each independently selected from hydroxy, hydrogen or alkyl, preferably from hydroxy, hydrogen or C1～C8More preferably from hydroxy, hydrogen or C1～C4Most preferably selected from hydroxy, hydrogen or C1～C2Alkyl group of (1).
a is 0-50, b is 0-50, c is 0-50, preferably a is 0-30, b is 0-30, c is 0-30, and a, b and c are not 0 at the same time;
d is 0 or 1.
Wherein, in step 2, when the compound represented by formula (II) is used to directly react with an epoxy compound, d ═ 0 in the obtained product; when the glycidyl ether compound intermediate is used in the reaction with an epoxy compound, d-1 is obtained as a product.
In a preferred embodiment, in step 1, the halogenated epoxy compound is selected from at least one of epichlorohydrin, chloroepoxybutane and chloroepoxypentane, and is preferably epichlorohydrin.
In a preferred embodiment, in step 1, the post-treatment comprises an open loop treatment: and adding an alkali solution for ring opening treatment to obtain the glycidyl ether intermediate.
Wherein, the reaction conditions for preparing the intermediate of the glycidyl ether by the reaction of the compound shown in the formula (II) and the halogenated epoxy compound are disclosed in the prior art.
In a preferred embodiment, in step 2, the catalyst is a basic catalyst, preferably at least one selected from potassium hydroxide, anhydrous potassium carbonate, sodium hydroxide, and sodium bicarbonate.
In a preferred embodiment, in step 2, the epoxy compound is selected from at least one of ethylene oxide, propylene oxide, butylene oxide, pentylene oxide, hexylene oxide, heptylene oxide and octylene oxide, preferably at least one of ethylene oxide, propylene oxide and butylene oxide.
In a preferred embodiment, in step 3, the catalyst is selected from at least one of alkali metals, alkali metal hydroxides, alkali metal carbonates, preferably at least one selected from sodium hydroxide, potassium hydroxide, sodium carbonate and potassium carbonate.
In step 3, Williamson etherification reaction is carried out on the polyether intermediate product shown in the formula (III) and a blocking agent to realize the blocking of the terminal hydroxyl.
In a preferred embodiment, in step 3, the capping agent is X1R6Wherein X is1Selected from hydroxy, halogen or alkoxy, preferably from hydroxy, halogen or C1～C8More preferably from hydroxy, Cl, Br, or C1～C5Most preferably selected from hydroxy, Cl, CH3O or C2H5O; and/or, R6Is selected from C1～C24Is preferably selected from C1～C20More preferably from C1～C16A hydrocarbon group of (1).
In a preferred embodiment, in step 3, the molar ratio of the polyether intermediate, the catalyst and the end capping agent is 1: (1-10): (1-5), preferably 1: (1-5): (1-4).
WhereinThe molar amount of the polyether intermediate is based on the molar amount of the hydroxyl groups therein, the molar amount of the catalyst is based on the molar amount of the molecules thereof, the molar amount of the end-capping agent is based on the molar amount of the end-capping agent wherein X1Based on the molar amount of (a).
The third object of the present invention is to provide the use of the composition according to the first object of the present invention or the composition obtained by the preparation method according to the second object of the present invention in viscosity reduction of thickened oils.
Wherein the oil reservoir temperature is 60-100 ℃, and the crude oil viscosity is 30,000-100,000 mPa.s.
In a preferred embodiment, the application is carried out as follows: and injecting the thickened oil viscosity-reducing synergistic composition slug and a carbon dioxide slug into thickened oil in sequence, or dissolving the thickened oil viscosity-reducing synergistic composition into carbon dioxide and then injecting the slug into the thickened oil.
In a further preferred embodiment, the carbon dioxide solubility in the thick oil is measured after a period of time after mixing with the thick oil and the carbon dioxide solubilization rate is calculated by comparison with the solubility measured for the carbon dioxide slug alone.
The thickened oil viscosity-reducing composition can be applied according to the prior art, can be used independently, and can also be used in combination with the existing chemical agent of an oil field.
The combined compound prepared by the invention has a flexible and adjustable structure, and the interaction of carbon dioxide and thickened oil is enhanced by introducing oxygen atoms, nitrogen atoms and benzene ring groups, so that the dosage of the existing chemical agent can be greatly reduced, and the thickened oil can be effectively started.
The invention relates to the situation of the content or concentration of the combined compound, which refers to the total concentration of the components of the aliphatic synergist (1) and the aromatic compound (2) containing benzene ring in the technical scheme.
Compared with the prior art, the invention has the following beneficial effects:
(1) the prepared combined compound has a flexible and adjustable structure, enhances the interaction of carbon dioxide and thickened oil by introducing oxygen atoms, nitrogen atoms and benzene ring groups, and can greatly reduce the dosage of the existing chemical agent, thereby effectively starting the thickened oil;
(2) the composition is used for the production of heavy oil reservoirs with the formation temperature of 30-100 ℃ and the crude oil viscosity of 30,000-100,000 mPa.s. The viscosity-reducing synergistic composition comprises 1%, 2% and 4% of carbon dioxide by mass, and the maximum solubilization rates of the carbon dioxide are 444.7%, 670.3% and 863.9% respectively, so that a good technical effect is achieved.
Drawings
FIG. 1 is an infrared spectrum of hydroquinone polyoxypropylene (6) polyoxybutylene (4) di-n-octyl ether prepared in example 1.
Wherein, 2938.7cm-1And 2864.1cm-1Is a characteristic peak of C-H stretching of methyl and methylene, 1520.3cm-1And 1603.7cm-1Is the stretching vibration peak of benzene ring, 1094.5m-1Is C-O-C stretching vibration peak, 822.3cm-1And 936.7cm-1Is the in-plane rocking absorption peak of CH plane in the benzene ring.
FIG. 2 is a schematic view of an apparatus for measuring a carbon dioxide solubilization rate.
Wherein, 1 is the plunger pump, 2 is the valve, 3 is the appearance cauldron of joining in marriage, 4 are constant temperature system, 5 are liquid collecting bottle, 6 are gas indicator bottle, 7 are gas meter.
FIG. 3 is a graph of carbon dioxide solubilization efficiency versus concentration for viscosity reducing benefit compositions E01-E05.
FIG. 4 is a graph of carbon dioxide solubilization efficiency versus concentration for viscosity reducing benefit compositions E06-E11.
Fig. 5 is a graph of carbon dioxide dissolution rate versus concentration for E01, E12, and E13.
FIG. 6 is a graph showing the carbon dioxide solubilization rate-concentration in comparative examples 1 to 5.
Detailed Description
While the present invention will be described in detail with reference to the following examples, it should be understood that the following examples are illustrative of the present invention and are not to be construed as limiting the scope of the present invention.
The raw materials used in the examples and comparative examples are disclosed in the prior art if not particularly limited, and may be, for example, directly purchased or prepared according to the preparation methods disclosed in the prior art.
Determination of the solubility of the adhesion-reducing synergistic composition in carbon dioxide: purging air of the high-temperature high-pressure phase equilibrium kettle by carbon dioxide, and injecting a certain amount of the viscosity-reducing synergistic composition into the equilibrium kettle by a high-pressure infusion pump. And opening a carbon dioxide sample injection valve, slowly injecting carbon dioxide into the balance kettle, adjusting the temperature and pressure in the kettle to set values, and stirring and balancing. Connect gas sampling bottle to the balance kettle, gas flowmeter is connected to gas sampling bottle gas outlet, slowly emits the gas sample after a small amount of mixings, measures the quality of gas phase sampling bottle respectively, records gas mass flowmeter's reading simultaneously. The solubility S was calculated according to the formula (1), and the results are shown in Table 2.
Figure BDA0002531051960000091
Wherein, S: viscosity reducing synergistic composition in CO2Solubility in (1), g/L; m is0: mass of the gas phase sampling bottle before sampling, g; m is1: g, the mass of the sample and the gas phase sampling bottle before and after sampling; v: gas volume measurement, L.
Determination of carbon dioxide solubilization rate: firstly, weighing a certain amount of thick oil, placing the thick oil in a pressure kettle, opening a carbon dioxide sample injection valve and a gas sampling valve, purging the kettle to exhaust air by using carbon dioxide, and closing all valves. And starting a heating device to reach the formation temperature, regulating the pressure to an experimental design value, after stirring balance, slowly opening a sampling valve, taking out a small amount of liquid phase samples, keeping the pressure constant, measuring the amount of released gas, and calculating the mass percentage of the carbon dioxide in the thickened oil. Injecting a certain amount of the composition into a kettle through a high-pressure pump, calculating the mass percent of the carbon dioxide in the thick oil after the composition is added in the same operation, comparing the mass percent of the carbon dioxide in the thick oil before and after the composition is added in the same balance time, and calculating the dissolution increasing rate Y according to the formula (2) to the formula (4).
Figure BDA0002531051960000101
Figure BDA0002531051960000102
Figure BDA0002531051960000103
Wherein, Y: carbon dioxide solubilization rate,%; w* oil，g: the solubility of carbon dioxide in the crude oil of the target block without the viscosity-reducing synergistic composition, g/g; w0 oil，g: solubility of carbon dioxide in the target block crude oil, g/g, when the viscosity-reducing synergistic composition is added; z: taking Z as 1 as a carbon dioxide compression factor; r: gas state constant, R-8.314 mol-1.k-1(ii) a T: gas volume measurement temperature, K; p: gas volume measurement pressure, Pa; v: gas volume measurement, m3；m0: mass of liquid sampling bottle, g; m is1: the total mass g of the sampling sample and the liquid sampling bottle without adding the viscosity-reducing synergistic composition; m is2: total mass of sample and liquid sample bottle, g, when viscosity reducing synergistic composition is added. The error of the results of two parallel measurements does not exceed 1 percent.
Example 1 preparation of a viscosity-reducing synergistic composition E01
Adding 110.0 g (1 mol) of hydroquinone and 8.8 g of potassium hydroxide into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times by nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 350.9 g (6.05 mol) of propylene oxide, controlling the pressure to be less than or equal to 0.60MPa, adjusting the temperature to 160 ℃ after the reaction of the propylene oxide, and slowly introducing 291.6 g (4.05 mol) of butylene oxide to prepare the propylene oxide, wherein the pressure is less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain hydroquinone polyoxypropylene (6) polyoxybutylene (4) ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5And a is 3, b is 2, c is 0, d is 0, and j is 2)690.8 g, yield 92.6%.
② in a dry reaction bottle with a water diversion device, hydroquinone polyoxypropylene (6) polyoxybutylene (4) ether (R) is added in turn1＝R2＝H，R3＝CH3，R4＝C2H5A is 3, b is 2, c is 0, d is 0, j is 2 373.1 g (0.5 mol), fine potassium hydroxide 112.2 g (2.0 mol) and benzene 800 ml, heating and refluxing until the water amount reaches over 90% of the theoretical value, slowly dropping 1-bromo-n-octane 202.7 g (1.05 mol), continuing refluxing for 8 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, removing water layer, washing with saturated saline three times, removing lower layer water, and evaporating solvent benzene and unreacted 1-bromine n-octane under reduced pressure to obtain hydroquinone polyoxypropylene (6) polyoxybutylene (4) di-n-octyl ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Where a is 3, b is 2, c is 0, d is 0, and j is 2). Samples were taken for infrared spectroscopy, see FIG. 1.
③ tributyl citrate and the hydroquinone polyoxypropylene (6), polyoxybutylene (4) and di-n-octyl ether (R) obtained in the step (II) according to the mass ratio of 1: 41＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Mixing a-3, b-2, c-0, d-0 and j-2), and stirring uniformly to obtain the viscosity-reducing synergistic composition E01 shown in table 1.
Example 2 preparation of a viscosity-reducing synergistic composition E02
110.0 g (1 mol) of hydroquinone and boron trifluoride diethyl etherate are added into a three-neck flask with a stirring dropping funnel and stirred uniformly. When the temperature is raised to a certain temperature, 203.6 g (2.2 mol) of epichlorohydrin is slowly dripped, and after the dripping is finished, the solution is maintained for 2 hours. Vacuum distilling to remove unreacted epichlorohydrin, adding ethanol solution of sodium hydroxide, and stirring. Filtering to remove the generated sodium chloride, then distilling under reduced pressure to remove ethanol, water and the like, and filtering to remove the residual sodium chloride while the solution is hot to obtain the hydroquinone diglycidyl ether.
Secondly, 222.1 g (1 mol) of hydroquinone diglycidyl ether and 9.9 g of potassium hydroxide are added into a 2L pressure reactor provided with a stirring device, a vacuum system is started when the mixture is heated to 80-90 ℃, the mixture is dehydrated for 1 hour under high vacuum, then nitrogen is used for replacing for 3-4 times, the reaction temperature of the system is adjusted to 150 ℃, 359.6 g (6.2 mol) of propylene oxide is slowly introduced, and the pressure is controlled to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 80 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain hydroquinone hydroxyl polyoxypropylene (2) polyoxypropylene (6) ether (R)1＝R2＝H，R5＝CH3Where a is 0, b is 0, c is 3, d is 1, and j is 2)520.4 g, yield 91.3%.
Thirdly, hydroquinone hydroxyl polyoxypropylene (2) polyoxypropylene (6) ether (R) is added into a drying reaction bottle with a water diversion device in sequence1＝R2＝H，R5＝CH3A is 0, b is 0, c is 3, d is 1, j is 2 285.1 g (0.5 mol), fine sodium hydroxide 160.2 g (4.0 mol) and 600ml benzene, heating and refluxing are carried out until the amount of water brought out reaches more than 90% of the theoretical value, 287.8 g (2.1 mol) of 1-bromo n-butane is slowly dripped, and the refluxing is continued for 10 hours after the dripping is finished. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, removing water layer, washing with saturated saline three times, removing lower layer water, and evaporating solvent benzene and unreacted 1-bromon-butane under reduced pressure to obtain the formula
(I) Organic matter (R) shown1＝R2＝H，R5＝CH3，R6＝n-C4H9，a＝0，b＝0，c＝3，d＝1，j＝2)。
Fourthly, according to the mass ratio of 1: 0.5, the isomeric tridecanol 3PO2BO and the organic matter (R) shown in the formula (I) obtained in the third step1＝R2＝H，R5＝CH3，R6＝n-C4H9A is 0, b is 0, c is 3, d is 1, j is 2) and the mixture is stirred evenly to obtain the viscosity-reducing synergistic composition E02 shown in Table 1.
Example 3 preparation of a viscosity reducing synergistic composition E03
In the same manner as in example 1, a viscosity-reducing synergistic composition E03 was prepared, the composition of which is shown in Table 1.
Adding 318.0 g (1 mol) of hexadecylphenol, 5.9 g of potassium hydroxide and 2.5 g of potassium carbonate into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times by nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 176.9 g (3.05 mol) of propylene oxide, controlling the pressure to be less than or equal to 0.60MPa, and after the reaction of the propylene oxide is finished, slowly introducing 88.0 g (2.0 mol) of ethylene oxide to prepare the propylene oxide, wherein the pressure is less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain hexadecylphenol polyoxypropylene (3) polyoxyethylene (2) ether (R)1＝C16H33，R2＝H，R4＝CH3，R5H, 0, 3, 2, 0, 1, 555.6 g, 95.8% yield.
② adding hexadecyl phenol polyoxypropylene (3) polyoxyethylene (2) ether (R) into the pressure reaction kettle in turn1＝C16H33，R2＝H，R4＝CH3，R5H, 0 a, 3 b, 2 c, 0 d, 1 j, 290.0 g (0.5 mol) and 112.2 g (2.0 mol) of fine potassium hydroxide, heating to 100 to 110 ℃ for reaction, removing water produced during the reaction, and introducing 50.5 g (1.0 mol) of methyl chloride to continue the reaction for 4 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, and removing lower water layer to obtain hexadecylphenol polyoxypropylene (3) polyoxyethylene (2) methyl ether (R)1＝C16H33，R2＝H，R4＝CH3，R5＝H，R6＝CH3，a＝0，b＝3，c＝2，d＝0，j＝1)。
③ mixing the N-oleyl dipropylenetriamine and the hexadecyl phenol polyoxypropylene (3) polyoxyethylene (2) methyl ether (R) obtained in the step II according to the mass ratio of 1: 7.51＝C16H33，R2＝H，R4＝CH3，R6＝H，R6＝CH3Mixing a-0, b-3, c-2, d-0 and j-1), and stirring uniformly to obtain the viscosity-reducing synergistic composition E03 shown in table 1.
Example 4 preparation of a viscosity reducing synergistic composition E04
In the same manner as in example 1, a viscosity-reducing synergistic composition E04 was prepared, the composition of which is shown in Table 1.
Adding 166.0 g (1 mol) of p-tert-butyldiphenol and 8.2 g of potassium hydroxide into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times with nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 585.8 g (10.1 mol) of propylene oxide, and controlling the pressure to be less than or equal to 0.60 Mpa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain the p-tert-butyldiphenol polyoxypropylene (10) ether (R)1＝t-C4H9，R2＝H，R3＝CH3Where a is 5, b is 0, c is 0, d is 0, and j is 2)699.0 g, 93.7% yield.
② adding p-tert-butyldiphenol polyoxypropylene (10) ether (R) in sequence into a drying reaction bottle with a water-dividing device1＝t-C4H9，R2＝H，R3＝CH3A is 5, b is 0, c is 0, d is 0, j is 2 373.1 g (0.5 mol), fine potassium hydroxide 112.2 g (2.0 mol) and benzene 800 ml, heating and refluxing until the water amount reaches over 90% of the theoretical value, slowly dropping bromo-isooctane 202.7 g (1.05 mol), continuing refluxing for 8 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, removing lower layer water, and evaporating solvent benzene and unreacted bromo-isooctane under reduced pressure to obtain p-tert-butyldiphenol polyoxypropylene (10) diisooctyl ether (R)1＝t-C4H9，R2＝H，R3＝CH3，R6＝i-C8H17，a＝5，b＝0，c＝0，d＝0，j＝2)。
③ isoamyl alcohol is mixed according to the mass ratio of 1: 5: 0.2,Step (II) to obtain p-tert-butyl diphenol polyoxypropylene (10) diisooctyl ether (R)1＝t-C4H9，R2＝H，R3＝CH3，R6＝i-C8H17A ═ 5, b ═ 0, c ═ 0, d ═ 0, j ═ 2) and tert-butylbenzene were mixed and stirred uniformly to give adhesion-reducing synergistic composition E04, see table 1.
Example 5 preparation of a viscosity-reducing synergistic composition E05
In the same manner as in example 2, a viscosity-reducing synergistic composition E05 was prepared, the composition of which is shown in Table 1.
137.0 g (1 mol) of N, N-dimethylaminophenol and boron trifluoride diethyl etherate are added into a three-neck flask with a stirring dropping funnel and stirred uniformly. When the temperature is raised to a certain temperature, 101.8 g (1.1 mol) of epichlorohydrin is slowly dripped, and after the dripping is finished, the solution is maintained for 2 hours. Vacuum distilling to remove unreacted epichlorohydrin, adding ethanol solution of sodium hydroxide, and stirring. Filtering to remove the generated sodium chloride, then distilling under reduced pressure to remove ethanol, water and the like, and filtering to remove the residual sodium chloride while the solution is hot to obtain the N, N-dimethyl aminophenol glycidyl ether.
Adding 193.1 g (1 mol) of N, N-dimethyl aminophenol glycidyl ether and 15.7 g of potassium hydroxide into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times by nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 899.0 g (15.5 mol) of propylene oxide, and controlling the pressure to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 80 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain the N, N-dimethylaminophenol hydroxyl polyoxypropylene (1) polyoxypropylene (15) ether (R)1＝H，R2＝N(CH3)2，R3＝CH315 g, 0 b, 0 c, 1 d, 1 j) 992.8 g, yield 93.4%.
Thirdly, sequentially adding N, N-dimethyl aminophenol hydroxyl polyoxypropylene (1) polyoxypropylene (15) ether (R) into a pressure reaction kettle1＝H，R2＝N(CH3)2，R3＝CH3，a＝15，b＝0，c is 0, d is 1, j is 1)531.5 g (0.5 mol) and fine potassium hydroxide 112.2 g (2.0 mol), heating to 110-120 deg.C, removing water produced during reaction, charging 75.8 g (1.5 mol) of methane chloride, and continuing reaction for 3 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, and removing lower water layer to obtain organic substance (R) shown in formula (I)1＝H，R2＝N(CH3)2，R3＝CH3，R6＝CH3，a＝15，b＝0，c＝0，d＝1，j＝1)。
Fourthly, the cocamidopropyl dimethyl tertiary amine and the organic matter (R) shown in the formula (I) obtained in the third step are mixed according to the mass ratio of 1: 0.71＝H，R2＝N(CH3)2，R3＝CH3，R6＝CH3Mixing a-15, b-0, c-0, d-1 and j-1), and stirring uniformly to obtain the viscosity-reducing synergistic composition E05 shown in table 1.
Example 6 preparation of a viscosity reducing synergistic composition E06
In the same manner as in example 1, a viscosity-reducing synergistic composition E06 was prepared, the composition of which is shown in Table 1.
Adding 164.0 g (1 mol) of 4-tert-butyl-2-methylphenol, 11.8 g of potassium hydroxide and 5.2 g of potassium carbonate into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times by nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 899.0 g (15.5 mol) of propylene oxide, controlling the pressure to be less than or equal to 0.60MPa, adjusting the temperature to 140 ℃ after the reaction of the propylene oxide, slowly introducing 88.0 g (2.0 mol) of ethylene oxide to prepare the ethylene oxide, adjusting the temperature to 160 ℃ after the reaction of the ethylene oxide, slowly introducing 72.1 g (1.0 mol) of butylene oxide to prepare the ethylene oxide, and adjusting the pressure to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain 4-tert-butyl-2-methylphenol polyoxypropylene (15) polyoxyethylene (2) polyoxybutylene (1) ether (R)1＝CH3，R2＝t-C4H9，R3＝CH3，R4＝H，R5＝C2H515, 2, 1, 0, 1)1111.7 g, yield 93.1%.
② 4-tert-butyl-2-methylphenol polyoxypropylene (15), polyoxyethylene (2), polyoxybutylene (1) ether (R) are added in turn in a pressure reaction kettle1＝CH3，R2＝t-C4H9，R3＝CH3，R4＝H，R5＝C2H6The reaction is carried out by heating 597.1 g (0.5 mol) and 112.2 g (2.0 mol) of fine-particle potassium hydroxide (a is 15, b is 2, c is 1, d is 0, j is 1) to 100-110 deg.C, removing water generated during the reaction, and introducing 78.5 g (1.0 mol) of n-chloropropane to continue the reaction for 4 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, removing lower layer water to obtain 4-tert-butyl-2-methylphenol polyoxypropylene (15) polyoxyethylene (2) polyoxybutylene (1) n-propyl ether (R)1＝CH3，R2＝t-C4H9，R3＝CH3，R4＝H，R5＝C2H5，R6＝n-C3H7，a＝15，b＝2，c＝1，d＝0，j＝1)。
③ mixing the dodecylamine polyoxypropylene (7) ether and the 4-tert-butyl-2-methylphenol polyoxypropylene (15), the polyoxyethylene (2), the polyoxybutylene (1) and the n-propyl ether (R) obtained in the step II according to the mass ratio of 1: 1.21＝CH3，R2＝t-C4H9，R3＝CH3，R4＝H，R5＝C2H5，R6＝n-C3H7Mixing a-15, b-2, c-1, d-0 and j-1), and stirring uniformly to obtain the viscosity-reducing synergistic composition E06 shown in table 1.
Example 7 preparation of a viscosity reducing synergistic composition E07
In the same manner as in example 2, adhesion-reducing synergistic composition E07 was prepared, respectively, and its composition is shown in Table 1.
262.0 g (1 mol) of dodecylphenol and boron trifluoride diethyl etherate are added into a three-neck flask with a stirring dropping funnel and stirred uniformly. When the temperature is raised to a certain temperature, 101.8 g (1.1 mol) of epichlorohydrin is slowly dripped, and after the dripping is finished, the solution is maintained for 2 hours. Vacuum distilling to remove unreacted epichlorohydrin, adding ethanol solution of sodium hydroxide, and stirring. Filtering to remove the generated sodium chloride, then distilling under reduced pressure to remove ethanol, water and the like, and filtering to remove residual sodium chloride while the solution is hot to obtain the dodecylphenol glycidyl ether.
Adding 318.1 g (1 mol) of dodecylphenol glycidyl ether and 15.7 g of potassium hydroxide into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times with nitrogen, adjusting the reaction temperature of the system to 140 ℃, slowly introducing 134.2 g (3.05 mol) of ethylene oxide, and controlling the pressure to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 80 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain the dodecyl phenol hydroxyl polyoxypropylene (1) polyoxyethylene (3) ether (R)1＝C12H25，R2＝H，R4H, a ═ 0, b ═ 3, c ═ 0, d ═ 1, j ═ 1)416.3 g, yield 92.5%.
③ adding dodecyl phenol hydroxyl polyoxypropylene (1) polyoxyethylene (3) ether (R) into a pressure reaction kettle in sequence1＝C12H25，R2＝H，R4H, 0 a, 3 b, 0 c, 1 d, 1 j, 1)225.0 g (0.5 mol) and 112.2 g (2.0 mol) of fine potassium hydroxide were heated to 100 to 110 ℃ to react, water produced during the reaction was removed, and 117.8 g (1.5 mol) of chloroisopropyl alcohol was added to continue the reaction for 3.5 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, and removing lower water layer to obtain organic substance (R) shown in formula (I)1＝C12H25，R2＝H，R4＝H，R6＝i-C3H7，a＝0，b＝3，c＝0，d＝1，j＝1)。
Fourthly, the organic matter (R) shown in the formula (I) obtained in the third step is mixed with n-octanol according to the mass ratio of 1: 3: 0.51＝C12H25，R2＝H，R4＝H，R6＝i-C3H7A is 0, b is 3, c is 0, d is 1, j is 1) and dodecylbenzene, and the materials are uniformly stirred to obtain the viscosity-reducing synergistic composition E07 shown in Table 1.
Example 8 preparation of a viscosity reducing synergistic composition E08
In the same manner as in example 1, without first preparing a phenol ether compound, dodecylamine polyoxyethylene (2) polyoxypropylene (5) ether and benzene were mixed in a mass ratio of 1: 1, and the mixture was stirred uniformly to obtain a viscosity-decreasing synergistic composition E08, the composition of which is shown in Table 1.
Example 9 preparation of a viscosity reducing synergistic composition E09
In the same manner as in example 1, without first preparing a phenol ether compound, di-n-butyl succinate and n-octyl benzene ether were mixed in a mass ratio of 1: 2, and the mixture was stirred uniformly to obtain a viscosity-reducing synergistic composition E09, the composition of which is shown in Table 1.
Example 10 preparation of a viscosity reducing synergistic composition E10
In the same manner as in example 1, a viscosity-reducing synergistic composition E10 was prepared, the composition of which is shown in Table 1.
Adding 194.0 g (1 mol) of n-butyl p-hydroxybenzoate and 11.1 g of potassium carbonate into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times with nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 899.0 g (15.5 mol) of propylene oxide, and controlling the pressure to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain the p-butoxy acylphenol polyoxypropylene (15) ether (R)1＝H，R2＝COOC4H9-n，R5＝CH3And a is 0, b is 0, c is 15, d is 0, and j is 1)1020.4 g, with a yield of 95.9%.
② sequentially adding p-butoxy acyl phenol polyoxypropylene (15) ether (R) into a dry reaction bottle with a water-dividing device1＝H，R2＝COOC4H9-n，R5＝CH3A is 0, b is 0, c is 15, d is 0, j is 1 532.0 g (0.5 mol), fine particle potassium hydroxide 84.0 g (1.5 mol) and benzene 800 ml, heated and refluxed to the beltThe water amount reaches more than 90 percent of the theoretical value, 137.0 g (0.55 mol) of 1-bromon-dodecane is slowly dripped, and the reflux is continued for 8 hours after the dripping is finished. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, removing water layer, washing with saturated saline three times, removing lower layer water, and evaporating solvent benzene and unreacted 1-bromododecane under reduced pressure to obtain n-butoxy acylphenol polyoxypropylene (15) dodecanol ether (R)1＝H，R2＝COOC4H9-n，R5＝CH3，R6＝n-C12H25，a＝0，b＝0，c＝15，d＝0，j＝1)。
③ the n-amyl propionate and the n-butoxy acyl phenol polyoxypropylene (15) dodecanol ether (R) obtained in the step (c) are mixed according to the mass ratio of 1: 151＝H，R2＝COOC4H9-n，R5＝CH3，R6＝n-C12H25Mixing a-0, b-0, c-15, d-0 and j-1), and stirring uniformly to obtain the viscosity-reducing synergistic composition E10 shown in table 1.
Example 11 preparation of a viscosity reducing synergistic composition E11
In the same manner as in example 1, a viscosity-reducing synergistic composition E11 was prepared, the composition of which is shown in Table 1.
Adding 306.1 g (1 mol) of n-dodecyl p-hydroxybenzoate and 13.7 g of potassium carbonate into a 2L pressure reactor provided with a stirring device, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times with nitrogen, adjusting the reaction temperature of the system to 160 ℃, slowly introducing 511.2 g (7.1 mol) of butylene oxide, and controlling the pressure to be less than or equal to 0.60 MPa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and neutralization and dehydration are carried out after cooling to obtain the p-dodecyl-oxygen acyl phenol polyoxybutylene (7) ether (R)1＝H，R2＝COOC12H25-n，R5＝C2H5And a is 0, b is 0, c is 7, d is 0, and j is 1)767.9 g, yield 94.8%.
② sequentially adding p-dodecyl phenol polyoxybutylene (7) ether (R) into a pressure reaction kettle1＝H，R2＝COOC12H25-n，R5＝C2H5405.2 g (0.5 mol) of a-0, b-0, c-7, d-0, j-1 and 112.2 g (2.0 mol) of fine-particle potassium hydroxide are heated to 100 to 110 ℃ for reaction, water generated during the reaction is removed, and 64.5 g (1.0 mol) of monochloroethane is introduced for further reaction for 4 hours. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, removing water layer, washing with saturated saline three times, removing lower water layer to obtain p-dodecyl-phenol polyoxybutylene (7) ether (R)1＝H，R2＝COOC12H26-n，R6＝C2H5，R6＝C2H5，a＝0，b＝0，c＝7，d＝0，j＝1)。
③ isoamyl butyrate and the p-n-dodecoxyphenol polyoxybutylene (7) ether (R) obtained in the step (II) are mixed according to the mass ratio of 1: 1.5: 31＝H，R2＝COOC12H25-n，R5＝C2H5，R6＝C2H5A is 0, b is 0, c is 7, d is 0, j is 1) and the decaglycol benzoate, and the mixture is evenly stirred to obtain the viscosity-reducing synergistic composition E11 shown in Table 1.
Example 12 preparation of a viscosity reducing synergistic composition E12
The same procedure as in example 1 was followed to first prepare the single-chain organic phenol polyoxypropylene (3) polyoxybutylene (2) n-octyl ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17And a is 3, b is 2, c is 0, d is 0 and j is 1), tributyl citrate is mixed with the mixture according to the mass ratio of 1: 4, and the mixture is uniformly stirred to obtain the viscosity-reducing synergistic composition E12 shown in Table 1.
Single-chain organic phenol polyoxypropylene (3) polyoxybutylene (2) n-octyl ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Preparation of a ═ 3, b ═ 2, c ═ 0, d ═ 0, j ═ 1):
[ 94.0 g (1 mol) of p-phenol was charged into a 2L pressure reactor equipped with a stirrerAnd 4.4 g of potassium hydroxide, heating to 80-90 ℃, starting a vacuum system, dehydrating for 1 hour under high vacuum, then replacing for 3-4 times by nitrogen, adjusting the reaction temperature of the system to 150 ℃, slowly introducing 175.2 g (3.02 mol) of propylene oxide, controlling the pressure to be less than or equal to 0.60Mpa, after the reaction of the propylene oxide is finished, adjusting the temperature to 160 ℃, and slowly introducing 146.2 g (2.03 mol) of butylene oxide to prepare the potassium hydroxide, wherein the pressure is less than or equal to 0.60 Mpa. After the reaction is finished, the temperature is reduced to 90 ℃, low-boiling-point substances are removed in vacuum, and after cooling, neutralization and dehydration are carried out to obtain the phenol polyoxypropylene (3) polyoxybutylene (2) ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5And a is 3, b is 2, c is 0, d is 0, and j is 1)398.4 g, with a yield of 96.7%.
② in a dry reaction bottle with a water diversion device, phenol polyoxypropylene (3) polyoxybutylene (2) ether (R) is added in turn1＝R2＝H，R3＝CH3，R4＝C2H5A is 3, b is 2, c is 0, d is 0, j is 1)206.1 g (0.5 mol), fine particle potassium hydroxide 112.2 g (2.0 mol) and benzene 800 ml, heating and refluxing until the water amount brought out reaches more than 90% of the theoretical value, slowly dripping 101.4 g (0.525 mol) of 1-bromo-n-octane, and continuing refluxing for 8 hours after dripping off. Cooling, pouring the reaction solution into water, adjusting pH to acidity with 10% saline, separating water layer, washing with saturated saline three times, removing lower layer water, and evaporating solvent benzene and unreacted 1-bromine n-octane under reduced pressure to obtain phenol polyoxypropylene (3) polyoxybutylene (2) n-octyl ether (R)1＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17，a＝3，b＝2，c＝0，d＝0，j＝1)。
Example 13 preparation of a viscosity reducing synergistic composition E13
The same procedure as in example 12 was followed, first of all, to prepare a single-chain organic compound (j ═ 1), and tributyl citrate and the phenol polyoxypropylene (3) polyoxybutylene (2) n-octyl ether (R) were added in a mass ratio of 1: 101＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Mixing a-3, b-2, c-0, d-0 and j-1), and stirring uniformly to obtain the viscosity-reducing synergistic composition E13 shown in table 1. By comparing with example 12, the present inventors have found that by adjusting the ratio of the fatty synergist and the organic compound represented by formula (1), an approximate viscosity-reducing synergistic result can be achieved.
Figure BDA0002531051960000201
Figure BDA0002531051960000211
[ COMPARATIVE EXAMPLE 1 ]
The same procedure as in example 1, except that E01 was replaced with tributyl citrate (TBC) in equal amounts, the performance tests were also performed, and the results are shown in Table 2, Table 3 and FIG. 6.
[ COMPARATIVE EXAMPLE 2 ]
The procedure of example 1 is followed, except that the same amount of hydroquinone polyoxypropylene (6) polyoxybutylene (4) di-n-octyl ether (R) is used1＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Where a is 3, b is 2, c is 0, d is 0, and j is 2) instead of E01, the performance test was performed in the same manner, and the results are shown in table 2, table 3, and fig. 6.
[ COMPARATIVE EXAMPLE 3 ]
The same procedure as in example 1, except that tributyl citrate and the hydroquinone polyoxypropylene (6) polyoxybutylene (4) di-n-octyl ether (R) obtained in step (ii) are mixed in a mass ratio of 1: 0.021＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Mixing a-3, b-2, c-0, d-0 and j-2), stirring uniformly to obtain the viscosity-reducing synergistic composition E14, and performing the performance test in the same way, wherein the results are shown in Table 2, Table 3 and FIG. 6.
[ COMPARATIVE EXAMPLE 4 ]
The process of example 1 was followed except thatTributyl citrate and hydroquinone polyoxypropylene (6), polyoxybutylene (4) and di-n-octyl ether (R) obtained in the step (II) according to the mass ratio of 1: 501＝R2＝H，R3＝CH3，R4＝C2H5，R6＝n-C8H17Mixing a-3, b-2, c-0, d-0 and j-2), stirring uniformly to obtain the viscosity-reducing synergistic composition E15, and performing the performance test in the same way, wherein the results are shown in Table 2, Table 3 and FIG. 6.
[ COMPARATIVE EXAMPLE 5 ]
The procedure of example 1 was followed except that in the publication of CN107828402A, a chemical additive E16 comprising propyl p-methoxybenzoate and a copolymer of methacrylic acid-styrene-vinyl acetate in a mass ratio of 4: 1 was used in place of E01, and the results were shown in Table 2, Table 3 and FIG. 6.
[ Experimental example 1 ] solubility experiment of viscosity-reducing synergistic composition in carbon dioxide
A250 mL high temperature high pressure phase equilibrium reactor was cleaned with petroleum ether and dried, the air in the reactor was purged with 100mL/min carbon dioxide, and then 10g of the adhesion-reducing synergistic composition was pumped into the equilibrium reactor using a high pressure infusion pump. Opening a carbon dioxide sample injection valve, slowly injecting the carbon dioxide in the high-pressure storage tank into the balance kettle, opening a constant-temperature oil bath, respectively adjusting the temperature and the pressure in the kettle to 90 ℃ and 15MPa, and stirring and balancing for more than 2 hours until the pressure fluctuation is not more than 1% in 5 min. Connecting a gas sampling bottle to a balance kettle, connecting a gas flowmeter to a gas outlet of the gas sampling bottle, discharging 600-1000 mL of gas sample mixed with the viscosity-reducing synergistic composition at a speed of 100-200 mL/min, condensing the viscosity-reducing synergistic composition in the gas-phase sampling bottle through throttling action, and directly passing the gas-phase carbon dioxide through a gas mass flowmeter. And (3) after the sample is collected, the gas sampling bottle is detached and placed under the conditions of normal temperature and normal pressure, the residual gas is discharged, the mass of the gas phase sampling bottle is weighed, and meanwhile, the reading of the gas mass flowmeter is recorded. The solubility S was calculated according to the formula (1), and the results are shown in Table 2.
[ Experimental example 2 ] experiments on solubilization efficiency of carbon dioxide
Cleaning and drying 250mL of high-temperature high-pressure phase equilibrium kettle by using petroleum ether, weighing 25g (50 ℃, the viscosity of 69877.2mPa & s) of crude oil of a target block in the high-temperature high-pressure phase equilibrium kettle, purging and exhausting air in the kettle by using 100mL/min of carbon dioxide, opening a carbon dioxide sample injection valve, slowly injecting the carbon dioxide in a high-pressure storage tank into the equilibrium kettle, opening a constant-temperature oil bath, respectively adjusting the temperature and the pressure in the kettle to 90 ℃ and 15MPa, and stirring and balancing for more than 2 hours until the pressure fluctuation is not more than 1% in 5 min. Connecting a liquid phase sampling bottle to a balance kettle, connecting a gas flowmeter to an outlet of the liquid phase sampling bottle, slowly opening a liquid phase sampling valve, taking out a liquid phase product dissolved with carbon dioxide, condensing crude oil in the sampling bottle through throttling action, calculating the volume through a gas mass flowmeter if a gas phase directly escapes, ending sampling until the measured volume is 15 mL-20 mL (the liquid sample is about 0.01-0.1 g at the moment), and recording an actual gas measurement value, namely the volume of the dissolved carbon dioxide in the liquid phase. And (3) placing the liquid phase sampling bottle under the conditions of normal temperature and normal pressure, discharging residual gas, and weighing the mass of the residual gas. Then, adding the viscosity-reducing synergistic composition with different dosages according to the mass of the carbon dioxide into a kettle by using a high-pressure infusion pump, calculating the mass of the carbon dioxide by using a PR equation according to parameters such as temperature, pressure and volume in the kettle (about 100g under the experimental condition and about 50L under the standard state), repeating the steps, recording data, and calculating the carbon dioxide dissolution rate Y according to the formulas (2) to (4), wherein the results are shown in figures 3 to 6 and table 3, and the data in table 3 are values of the carbon dioxide dissolution rate Y at 1%, 2% and 4% dosages obtained from the fitted curves of figures 3 to 6.
TABLE 2
Figure BDA0002531051960000241
TABLE 3
Figure BDA0002531051960000251

Claims (13)

1. A thickened oil viscosity-reducing synergistic composition comprises at least one of organic matters shown as a formula (I) and a fat synergist:
Figure FDA0002531051950000011
in the formula (I), R1And R2Independently selected from hydrogen, C1～C32A hydrocarbon group of1～C32Substituted hydrocarbyl, ester, hydroxyl, amino or alkoxy groups of (a); and/or, R3、R4And R5Each independently selected from hydroxy, hydrogen or alkyl; r6Is selected from C1～C24Or C is a hydrocarbon group1～C24Substituted hydrocarbyl groups of (a); and/or, a is 0-50, b is 0-50, c is 0-50, and a, b and c are not 0 at the same time; and/or, d ═ 0 or 1; and/or, j ═ 0, 1, or 2.
2. The thickened oil viscosity-reducing synergistic composition as claimed in claim 1, wherein the fatty synergist is at least one selected from fatty alcohol, fatty alcohol ether, fatty amine ether and fatty acid ester;
preferably, the fatty alcohol is selected from C1～C18The alcohol of (1); and/or, the fatty alcohol ether is selected from C1～C18Alcohol ethers of (1); and/or the fatty amine is selected from C1～C24An amine of (a); and/or the fatty amine ether is selected from C1～C24Amine polyether of (a); and/or the ether in the fatty alcohol ether and the fatty amine ether is at least one of polyoxyethylene ether, polyoxypropylene ether and polyoxybutylene ether; and/or the fatty acid ester is C1～C18At least one of acid esters;
more preferably, the fatty synergist is selected from C1～C12Fatty alcohol of (2), C1～C12Fatty alcohol ether of (C)1～C18Fatty amine of (2), C1～C18Fatty amine ether of (C)1～C12At least one fatty acid ester.
3. The thickened oil viscosity-reducing synergistic composition as claimed in claim 1, characterized in that, in the formula (I),
R1and R2Each independently selected from hydrogen and C1～C28A hydrocarbon group of1～C28Substituted hydrocarbyl, alkoxy, ester, amine or hydroxyl groups; preferably, the alkoxy group is OR7，R7Is (CHR)0)eH，R0Is hydrogen, methyl or ethyl, e is any integer of 1-12; and/or the ester group is COOR8，R8Is (CHR'0)fH，R’0Is hydrogen, methyl or ethyl, and f is any integer of 1-18; more preferably, R1And R2Selected from hydrogen, C1～C18A hydrocarbon group of1～C18Substituted hydrocarbyl of (2), COO (CHR'0)fH or amino, R'0Is hydrogen or methyl, f is an integer of 1-12; and/or
R3、R4And R5Each independently selected from hydroxy, hydrogen or C1～C8Alkyl of (3), preferably from hydroxy, hydrogen or C1～C4More preferably from hydroxy, hydrogen or C1～C2Alkyl groups of (a); and/or
R6Is selected from C1～C24Is preferably selected from C1～C20More preferably from C1～C16A hydrocarbon group of (1).
4. The thickened oil viscosity-reducing synergistic composition as claimed in claim 1, wherein in the formula (I), a is 0-30, b is 0-30, c is 0-30, and a, b and c are not 0 at the same time.
5. The thickened oil viscosity-reducing synergistic composition as claimed in any one of claims 1 to 4, wherein the mass ratio of the fat synergistic agent to the organic matter represented by the formula (I) in the composition is 1 (0-200) and does not contain 0, preferably 1 (0.1-50), and more preferably 1 (0.1-20).
6. A method for preparing the thickened oil viscosity-reducing synergistic composition as claimed in any one of claims 1 to 5, which comprises: obtaining an organic matter shown in a formula (I), and then mixing the organic matter with a fat synergist to obtain the thickened oil viscosity-reducing composition; wherein, when j is 1 or 2, the organic compound represented by formula (I) is obtained as follows:
step 1, taking a compound shown as a formula (II), optionally reacting with a halogenated epoxy compound, and carrying out aftertreatment to obtain a glycidyl ether intermediate;
step 2, in the presence of a catalyst, reacting the compound shown in the formula (II) or the glycidyl ether intermediate with an epoxy compound to obtain a polyether intermediate product shown in the formula (III);
step 3, reacting the polyether intermediate product with a blocking agent in the presence of a catalyst to obtain an organic matter shown in a formula (I);
Figure FDA0002531051950000021
wherein, in formula (II) and formula (III), j is 1 or 2.
7. The process according to claim 6, wherein, in formula (II) and formula (III):
R1and R2Each independently selected from hydrogen and C1～C32Or C is a hydrocarbon group1～C32The substituted hydrocarbyl, ester, hydroxyl, amino or alkoxy of (A) is preferably selected from hydrogen, C1～C28A hydrocarbon group of1～C28Substituted hydrocarbyl, alkoxy, ester, amine or hydroxyl groups; and/or the presence of a gas in the gas,
preferably, the alkoxy group is OR7，R7Is (CHR)0)eH，R0Is hydrogen, methyl or ethyl, e is any integer of 1-12; and/or the presence of a gas in the gas,
the ester group is COOR8，R8Is (CHR'0)fH，R’0Is hydrogen, methyl or ethyl, and f is any integer of 1-18; and/or
More preferably, R1And R2Selected from hydrogen, C1～C18A hydrocarbon group of1～C18Substituted hydrocarbyl of (2), COO (CHR'0)fH or amino, R'0Is hydrogen or methyl, f is an integer of 1-12; and/or
R3、R4And R5Each independently selected from hydroxy, hydrogen or alkyl, preferably from hydroxy, hydrogen or C1～C8More preferably from hydroxy, hydrogen or C1～C4Most preferably selected from hydroxy, hydrogen or C1～C2Alkyl groups of (a); and/or
a is 0-50, b is 0-50, c is 0-50, preferably a is 0-30, b is 0-30, c is 0-30, and a, b and c are not 0 at the same time;
d is 0 or 1.
8. The production method according to claim 6, wherein, in step 1,
the halogenated epoxy compound is selected from at least one of epichlorohydrin, epoxy chlorobutane and epoxy chloropentane, and is preferably epichlorohydrin; and/or
The post-treatment comprises an open loop treatment: and adding an alkali solution for ring opening treatment to obtain the glycidyl ether intermediate.
9. The production method according to claim 6,
in step 2, the catalyst is an alkaline catalyst, preferably at least one of potassium hydroxide, anhydrous potassium carbonate, sodium hydroxide and sodium bicarbonate; and/or
In step 2, the epoxy compound is selected from at least one of ethylene oxide, propylene oxide, butylene oxide, pentylene oxide, hexylene oxide, heptylene oxide and octylene oxide, preferably at least one of ethylene oxide, propylene oxide and butylene oxide; and/or
In step 3, the catalyst is selected from at least one of alkali metals, alkali metal hydroxides, and alkali metal carbonates, preferably at least one selected from sodium hydroxide, potassium hydroxide, sodium carbonate, and potassium carbonate.
10. The method according to claim 6, wherein in step 3, the end-capping agent is X1R6Wherein, in the step (A),
X1selected from hydroxy, halogen or alkoxy, preferably from hydroxy, halogen or C1～C8More preferably from hydroxy, Cl, Br, or C1～C5Most preferably selected from hydroxy, Cl, CH3O or C2H5O; and/or
R6Is selected from C1～C24Is preferably selected from C1～C20More preferably from C1～C16A hydrocarbon group of (1).
11. The preparation method according to any one of claims 6 to 10, wherein in step 3, the molar ratio of the polyether intermediate product to the catalyst to the end-capping reagent is 1 (1 to 10): 1 to 5, preferably 1 (1 to 5): 1 to 4, wherein the molar amount of the polyether intermediate product is calculated as the molar amount of the hydroxyl groups therein, the molar amount of the catalyst is calculated as the molar amount of the molecules thereof, and the molar amount of the end-capping reagent is calculated as the molar amount of the X groups therein1Based on the molar amount of (a).
12. Use of the thickened oil viscosity-reducing synergistic composition according to any one of claims 1 to 5 or the thickened oil viscosity-reducing synergistic composition obtained by the preparation method according to any one of claims 6 to 11 in thickened oil viscosity reduction, preferably at a reservoir temperature of 60 to 100 ℃ and a crude oil viscosity of 30,000 to 100,000 mpa.s.
13. The use of claim 12, wherein the slug of the viscosity building composition is injected into the thick oil sequentially with the slug of carbon dioxide, or the slug of the viscosity building composition is injected into the thick oil after the thick oil viscosity building composition is dissolved in the carbon dioxide.
CN202010520565.8A 2020-06-09 2020-06-09 Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof Active CN113773824B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN202010520565.8A CN113773824B (en) 2020-06-09 2020-06-09 Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN202010520565.8A CN113773824B (en) 2020-06-09 2020-06-09 Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof

Publications (2)

Publication Number Publication Date
CN113773824A true CN113773824A (en) 2021-12-10
CN113773824B CN113773824B (en) 2023-04-07

Family

ID=78834937

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202010520565.8A Active CN113773824B (en) 2020-06-09 2020-06-09 Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof

Country Status (1)

Country Link
CN (1) CN113773824B (en)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116333713A (en) * 2023-03-28 2023-06-27 陕西延长石油(集团)有限责任公司研究院 Liquid carbon dioxide oil washing agent and preparation method thereof

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4828029A (en) * 1987-12-14 1989-05-09 Irani Cyrus A Solubilizing surfactants in miscible drive solvents
US20060199742A1 (en) * 2005-03-02 2006-09-07 Arisz Petrus Wilhelmus F Water-soluble, low substitution hydroxyethylcellulose, derivatives thereof, process of making, and uses thereof
CN105257264A (en) * 2015-10-14 2016-01-20 中国石油天然气股份有限公司 Method for improving carbon dioxide displacement yield by using surfactants
CN106398675A (en) * 2015-07-30 2017-02-15 中国石油化工股份有限公司 Emulsification viscosity reduction agent, preparation method and applications thereof, and thick oil emulsification viscosity reduction method
CN107828401A (en) * 2017-06-08 2018-03-23 中国石油化工股份有限公司 One kind enhancing CO2Dissolve each other, reduce the oil driving additive of viscosity of crude with crude oil
CN110484228A (en) * 2018-05-15 2019-11-22 中国石油化工股份有限公司 The method that viscous crude visbreaking agent and its application and viscous crude drop stick

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4828029A (en) * 1987-12-14 1989-05-09 Irani Cyrus A Solubilizing surfactants in miscible drive solvents
US20060199742A1 (en) * 2005-03-02 2006-09-07 Arisz Petrus Wilhelmus F Water-soluble, low substitution hydroxyethylcellulose, derivatives thereof, process of making, and uses thereof
CN106398675A (en) * 2015-07-30 2017-02-15 中国石油化工股份有限公司 Emulsification viscosity reduction agent, preparation method and applications thereof, and thick oil emulsification viscosity reduction method
CN105257264A (en) * 2015-10-14 2016-01-20 中国石油天然气股份有限公司 Method for improving carbon dioxide displacement yield by using surfactants
CN107828401A (en) * 2017-06-08 2018-03-23 中国石油化工股份有限公司 One kind enhancing CO2Dissolve each other, reduce the oil driving additive of viscosity of crude with crude oil
CN110484228A (en) * 2018-05-15 2019-11-22 中国石油化工股份有限公司 The method that viscous crude visbreaking agent and its application and viscous crude drop stick

Non-Patent Citations (3)

* Cited by examiner, † Cited by third party
Title
LEI BAO等: "Synthesis of a Series of Anionic Surfactants Derived from NP and their Properties as Emulsifiers for Reducing Viscosity of Highly Viscous Oil via Formation of O/W Emulsions", 《JOURNAL OF SURFACTANTS AND DETERGENTS》 *
董晓红等: "封端聚醚的应用研究进展", 《精细与专用化学品》 *
赵福麟: "《油田化学》", 30 September 2010, 中国石油大学出版社 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116333713A (en) * 2023-03-28 2023-06-27 陕西延长石油(集团)有限责任公司研究院 Liquid carbon dioxide oil washing agent and preparation method thereof
CN116333713B (en) * 2023-03-28 2024-04-02 陕西延长石油(集团)有限责任公司研究院 Liquid carbon dioxide oil washing agent and preparation method thereof

Also Published As

Publication number Publication date
CN113773824B (en) 2023-04-07

Similar Documents

Publication Publication Date Title
CN113340928B (en) Experimental device and method for developing shale oil through supercritical CO2/H2O mixed fluid throughput
CN105257264A (en) Method for improving carbon dioxide displacement yield by using surfactants
CN111909679B (en) Preparation method and application of composition for reducing minimum miscible pressure of carbon dioxide and crude oil based on aerosol surfactant
CN101945972A (en) Handle the method for hydrocarbon containing formation with the fluorinated anionic surfactant composition
CN107828402B (en) Improve deep viscous crude CO2Chemical additive for recovery ratio in gas flooding process
CN113773824B (en) Thickened oil viscosity-reducing synergistic composition and preparation method and application thereof
CN106556506A (en) The device of flow pattern in measurement supercritical carbon dioxide fracturing fracture
CN103468238A (en) Preparation method and application of novel high-efficient acidification corrosion inhibitor
CN107828401B (en) Enhanced CO2Oil displacement additive capable of mutual dissolving with crude oil and reducing viscosity of crude oil
CN104449641A (en) Adjustor for reducing minimum miscible pressure of CO2 non-miscible flooding and application method thereof
CN110231253B (en) CO (carbon monoxide)2Experimental test method for competitive dissolution in oil-water mixed system
CN108059952A (en) A kind of degradable shielding protection agent and its preparation method and application
CN111778007B (en) Preparation method of seawater-based interpenetrating network polymer gel oil displacement agent
CN110655605A (en) Preparation method of novel reverse temperature-sensitive gel oil displacement agent
CN114753818B (en) Method for improving yield of thickened oil huff-puff well
CN106590564B (en) Temperature-resistant salt-resistant low-tension foam flooding composition and preparation method and application thereof
CN110724511B (en) Super-amphiphobic oil displacement material and preparation method thereof
CN102827595A (en) High temperature profile control agent injected with steam
CN114538822B (en) High-temperature gel channeling sealing agent and preparation method and application thereof
CN115873579B (en) Viscous oil viscosity-reducing wash oil agent and preparation method and application thereof
CN117946016A (en) Triazole aryl polyether compound and CO2Gas-soluble viscosity reducer and thickened oil CO2Cold recovery method for improving recovery ratio
CN113881417B (en) Chemical agent composition containing sorbitan polyether carboxylate, preparation method thereof and CO reduction method thereof 2 Method for driving out minimum miscible pressure
CN103554463A (en) Alkenyl alkyl phenol polyoxyethylene ether and preparation method thereof
CN114479049B (en) Triphenylmethane polyether carboxylic acid esterAnd composition, preparation method and super-thick oil CO thereof 2 Mining method
CN110184042B (en) Oil displacement agent for regulating, expanding and washing low-permeability oil reservoir and application process thereof

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
GR01 Patent grant
GR01 Patent grant