CN107987867B - Microemulsion extracting agent for separating heavy oil ore and use method thereof - Google Patents

Abstract

The invention relates to a microemulsion extractant for separating heavy oil ore and a use method thereof, the microemulsion extractant is formed by mixing three components of a eutectic solvent, a low-polyhydric alcohol and a weak polar solvent, wherein the eutectic solvent comprises the following components: low polyhydric alcohol: the mass ratio of the weak polar solvent is (1-2): (1-2): (2-4) the microemulsion is a anhydrous surfactant-free microemulsion, and the microemulsion extractant has the advantages of high thermodynamic stability, low surface tension, high solubilizing ability, easiness in recovery and reusability. The method provided by the invention can be applied to the aspect of extracting the asphalt in the heavy oil deposit, and has the advantages of high extraction efficiency, good asphalt product quality, less solid entrainment, simple extraction process and mild conditions.

Description

Microemulsion extracting agent for separating heavy oil ore and use method thereof

Technical Field

The invention relates to the technical field of heavy oil separation from heavy oil ores, in particular to a microemulsion extracting agent for heavy oil ore separation and a use method thereof.

Background

Heavy oil deposits, a generic term for a class of unconventional energy sources, include oil shale, oil sands, oil sludge, heavy oil, and the like.

Oil shale is a sedimentary rock containing solid organic matter within the framework of its inorganic minerals. The organic matter is mainly kerogen, is insoluble in petroleum solvent, and also contains a small amount of asphaltene. The oil shale is isolated from air and heated to about 500 ℃, and kerogen of the oil shale is pyrolyzed to generate shale oil, water, semicoke and dry distillation gas. The pyrolysis product shale oil is similar to natural petroleum, can be used as bunker fuel after being blended, and can obtain light oil products such as gasoline and diesel oil through processes such as hydrofining and the like.

As an important unconventional energy source, the oil shale has huge reserves, and the amount of the oil shale resources in the world is about 10 trillion tons according to incomplete statistics. Converted to about 5000 million tons of shale oil, which is 2 times more than the global oil resource (about 2700 million tons). The resource reserves of the Chinese oil shale are about 7199 hundred million tons, the resource reserves are converted into about 476 million tons of shale oil, and the technology recoverable reserves are 30 million tons. As a supplementary energy source of petroleum, the oil shale has wide development prospect.

The oil sludge is oil-containing sludge formed by a large amount of crude oil or oil products and soil, water or other impurities due to accidents, running, leakage, natural sedimentation and the like in the processes of oil exploration, exploitation, refining, tank cleaning, storage and transportation. Depending on the cause, sludge is generally classified into: oil sludge on the ground, oil sludge at the bottom of a tank, ground oil spill, oil-containing sludge in an oil refinery and the like. Wherein, the tank bottom oil sludge generally contains about 25 percent of water and 5 percent of inorganic matters such as silt and the like, and the rest 70 percent of hydrocarbon; by proper separation technology, the recovery rate of the hydrocarbon can reach more than 98 percent, and the recovery and utilization value is high. According to statistics, the total annual output of the oil sludge of the victory oil field is 116.27kt, and the oil sludge generated by each large oil field in China is expected to be up to millions of tons each year; the oil content of the oil sludge is 10-30%, the water content is 20-50%, and about more than ten thousand tons of crude oil are deposited in the oil sludge every year according to the average oil content of 20%, so that a great deal of waste of oil resources is caused.

Volatile components of petroleum in the oil sludge enter the atmosphere to pollute the air; the petroleum in the oil sludge enters the water body along with the rainwater, so that serious pollution is caused, and the ecological system of the water is damaged; the petroleum in the oil sludge enters the soil and can harm microorganisms of the soil and a soil plant ecosystem; more seriously, many of the harmful substances in crude oil are mutagenic and carcinogenic, and can bring serious harm to human health through direct and indirect ways. Therefore, the economic, environment-friendly and practical treatment method and device are developed, the petroleum in the oil sludge is fully recovered, the residual oil amount in the treated soil reaches the national specified standard, and the economic and environmental benefits are good.

The oil sand is a general term for a mixture of detritus or rock on the surface layer of the earth crust and water and thickened oil or asphalt contained in the detritus or rock, has a huge storage amount, and is an important potential petroleum resource in the world at present. In general, the oil sand contains heavy oil such as bitumen in an amount of 5 to 30% by mass. Over 90% of the world's oil sands are distributed in north america, primarily the united states and canadian regions; there are also billions of oil sands in the southeast region of indonesia, with great potential for development. Under the conditions of increasing international petroleum demand and high petroleum price, the thickened oil asphalt resource enriched in oil sand is developed, can be used as a substitute of petroleum resources, and has wide market prospect and economic benefit.

Due to its high viscosity and strong affinity, conventional hot alkaline water washing methods have difficulty extracting bitumen from oil sands. Solvent extraction methods which have high recovery efficiency, mild operating conditions for oleophilic ores and good applicability are mainly adopted at present. However, the current solvent extraction method has some problems, such as high content of mineral entrainment, large using amount of solvent, and high energy consumption in solvent distillation recovery caused by multi-stage solvent extraction.

The gap of the supply and demand of petroleum in China increases year by year, and the contradiction of the supply and the demand of the petroleum exists for a long time. The development and utilization of oil sand, oil shale, oil sludge and other heavy oil mine resources replace part of conventional energy sources, and the energy pressure of China is relieved, so that the method is a direction encouraged by national policies in future.

Disclosure of Invention

The first purpose of the invention is to provide a microemulsion extractant for separating heavy oil ores, which is a surfactant-I-type microemulsion without water and surfactant, and the extractant has the advantages of high thermodynamic stability, low surface tension, high solubilizing ability, easy recovery and reutilization.

The second purpose of the invention is to provide a method for separating heavy oil ore by using the microemulsion, which has the advantages of high extraction efficiency, good asphalt product quality, less solid entrainment, simple extraction process and mild conditions.

In order to achieve the purpose, the invention adopts the technical scheme that:

a microemulsion extractant for separating heavy oil ores is characterized in that: the eutectic solvent is formed by mixing three components of a eutectic solvent, a low-polyhydric alcohol and a weak polar solvent, wherein the eutectic solvent comprises the following components in percentage by weight: low polyhydric alcohol: the mass ratio of the weak polar solvent is (1-2): (1-2): (2-4);

the eutectic solvent is generated by the reaction of amino acid ionic liquid and urea, and the molar ratio of the amino acid ionic liquid to the urea is 1: (2-4), wherein the weak polar solvent is an aromatic hydrocarbon solvent or a chain hydrocarbon solvent.

Also, the weakly polar solvent is toluene, xylene, n-heptane or cyclohexane.

Furthermore, the amino acid is tryptophan, lysine, phenylalanine or histidine.

And the lower alcohol is methanol, ethanol or propanol.

And the amino acid ionic liquid is prepared from amino acid and strong acid containing halogen.

Further, the strong acid containing a halogen is hydrochloric acid, hydrobromic acid, or tetrafluoroboric acid.

And the amino acid ionic liquid is prepared from amino acid and tetrafluoroboric acid, and the molar ratio of the amino acid to the tetrafluoroboric acid is 1: (0.7-1.5).

Also, the preparation method of the eutectic solvent includes the steps of:

⑴ dispersing amino acid in water, adding tetrafluoroboric acid solution, stirring to react, and rotary evaporating to obtain amino acid ionic liquid;

⑵ mixing the amino acid ionic liquid and urea uniformly, heating and reacting to obtain eutectic solvent.

A method for separating heavy oil ore by using microemulsion comprises the following steps:

⑴ configuring the microemulsion of claim 1;

⑵ mixing and extracting the microemulsion extractant and the heavy oil mine, and separating the extracted mixture to obtain an oil phase layer, a microemulsion layer and a solid residue layer, wherein the mass ratio of the microemulsion to the heavy oil mine is (3-5):1, the extraction temperature is 20-50 ℃, and the extraction time is 5-60 min.

Also, the heavy oil deposits include oil sands, heavy oil, oil shale, or oil sludge.

Compared with the prior art, the invention has the beneficial effects that:

1. the microemulsion extractant for separating heavy oil ores provided by the invention is a anhydrous surfactant-free microemulsion, takes a eutectic solvent as a hydrophilic phase, takes a weak polar solvent as a lipophilic phase, and replaces a surfactant with low-polyhydric alcohol to stabilize the emulsion, and has the advantages of stable thermodynamics, easy recovery and reutilization.

2. The invention also provides a method for separating heavy oil ore by using the microemulsion extractant, which has the advantages of high extraction efficiency, good asphalt product quality, less solid entrainment, simple extraction process and mild conditions.

Drawings

FIG. 1 is a 1H-NMR chart of a eutectic solvent provided in example 1 of the present invention;

FIG. 2 is a process flow diagram of a process for heavy oil-ore separation using the microemulsion of the present invention.

(1) A weakly polar solvent; (2) a lower alcohol; (3) a eutectic reagent; (4) heavy oil deposits; (5) an extraction device; (6) extracting the materials; (7) a separation device; (8) an upper oil phase; (9) an evaporator; (10) a weakly polar solvent (11) bitumen; (12) a microemulsion phase; (13) solid residue on the lower layer; (14) a water washing device; (15) cleaning the sand grains.

Detailed Description

The technical solutions of the present invention will be described clearly and completely with reference to the following specific embodiments and accompanying drawings, and it is to be understood that the described embodiments are only a part of the embodiments of the present invention, and not all of them. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

The existing solvent extraction method has some problems, such as high content of mineral entrainment, large solvent consumption, and high energy consumption in solvent distillation and recovery due to multi-stage solvent extraction.

The invention provides a microemulsion extractant for separating heavy oil ores, which comprises a eutectic solvent, low-polyhydric alcohol and a weak polar solvent. Wherein the eutectic solvent is mainly prepared from amino acid ionic liquid and urea. The amino acid ionic liquid is used as a hydrogen bond acceptor and reacts with urea through a hydrogen bond to form a novel eutectic solvent. The extractant provided by the invention uses the eutectic solvent as a hydrophilic phase, uses the weak polar solvent as a lipophilic phase, and uses the low-polyol to replace the surfactant to stabilize the emulsion, is a surfactant-I-type microemulsion without water and surfactant, and has the advantages of high thermodynamic stability, low surface tension, high solubilizing capability, easiness in recovery and reusability.

As an alternative embodiment of the present invention, the molar ratio of the eutectic solvent, the low-polyol and the weakly polar solvent is (1-2): (1-2): (2-4). The molar ratio of the eutectic solvent, the low-polyol and the less polar solvent is typically, but not limited to: 1:1:2, 1:1:3, 1:1:4, 2:1:2, 2:1:3, 2:1:4, 1:2:2, 1:2:3, 1:2:4, or 2:2: 3.

As an alternative embodiment of the invention, the amino acid ionic liquid is mainly prepared from amino acid and strong acid containing halogen, and the strong acid containing halogen can provide a hydrogen bond acceptor for the amino acid ionic liquid and further form a hydrogen bond with urea. The strong halogen-containing acid is typically, but not limited to, hydrochloric acid, hydrobromic acid, or tetrafluoroboric acid.

As an alternative embodiment of the invention, the amino acid is tryptophan, lysine, phenylalanine, or histidine.

As an alternative embodiment of the present invention, the molar ratio of the amino acid ionic liquid to urea in the eutectic solvent is 1: (2-4). The molar ratio of the amino acid ionic liquid to the urea influences the melting point and the viscosity of the eutectic solvent, and the molar ratio of the amino acid ionic liquid to the urea is too high or too low, so that the prepared eutectic solvent has high melting point and high viscosity. The molar ratio of ionic liquid to urea is typically, but not limited to, 1:2, 1:2.1, 1:2.2, 1:2.3, 1:2.4, 1:2.5, 1:2.6, 1:2.7, 1:2.8, 1:2.9, 1:3, 1:3.1, 1:3.2, 1:3.3, 1:3.4, 1:3.5, 1:3.6, 1:3.7, 1:3.8, 1:3.9, or 1: 4.

As a preferred embodiment of the present invention, the molar ratio of the amino acid ionic liquid to urea in the eutectic solvent is 1:3, the eutectic solvent prepared by adopting the molar ratio has low melting point, low viscosity and wider application range.

In a preferred embodiment of the present invention, the amino acid ionic liquid is mainly prepared from an amino acid and tetrafluoroboric acid. The amino acid example liquid prepared by using the amino acid and the tetrafluoroboric acid not only can provide a hydrogen bond acceptor, but also has a low melting point.

As an alternative embodiment of the invention, the molar ratio of amino acid to tetrafluoroboric acid is 1: (0.7-1.5), the molar ratio of amino acid to aqueous tetrafluoroborate solution is typically, but not limited to: 1: 0.7, 1:0.8, 1:0.9, 1:1.0, 1:1.1, 1:1.2, 1:1.3, 1:1.4 or 1: 1.5. As a preferred embodiment of the present invention, the molar ratio of amino acid to tetrafluoroboric acid is 1:1, the conversion rate of the reaction is high, and the yield of the obtained amino acid ionic liquid is high.

The preparation method of the eutectic solvent comprises the following steps:

⑴ dispersing amino acid in water, adding tetrafluoroboric acid solution, stirring to react, and rotary evaporating to obtain amino acid ionic liquid;

⑵ mixing the amino acid ionic liquid and urea uniformly, heating and reacting to obtain eutectic solvent.

Mixing the eutectic solvent, the low-polyhydric alcohol and the weak polar solvent, and standing until the mixture is divided into two phases uniformly, thus obtaining the microemulsion extractant. The extracting agent provided by the invention is thermodynamically stable and is easy to recycle.

The invention provides a method for separating heavy oil ores by using the microemulsion, which is characterized in that an extracting agent is added into the heavy oil ores for extraction.

As an optional embodiment of the invention, the mass ratio of the microemulsion extractant to the heavy oil deposit is (3-5):1, the mass ratio of the extractant to the heavy oil deposit is too high, the dosage of the extractant is too much, and the economic cost is high; the dosage of the extractant is too small, and the extraction effect is not good. The mass ratio of extractant to heavy oil deposit is typically, but not limited to: 3:1, 3.1:1, 3.2:1, 3.3:1, 3.4:1, 3.5:1, 3.6:1, 3.7:1, 3.8:1, 3.9:1, 4:1, 4.1:1, 4.2:1, 4.3:1, 4.4:1, 4.5:1, 4.6:1, 4.7:1, 4.8:1, 4.9:1, or 5: 1.

As an alternative embodiment of the invention, the extraction temperature is 20-50 ℃. The extraction temperature is normal temperature extraction, the temperature is too high, an external heating source is needed, and the production cost is increased; the temperature is too low, the extraction effect is poor, and the extraction time is long. Typical but non-limiting extraction temperatures are: 20 ℃, 21 ℃, 22 ℃, 23 ℃, 24 ℃, 25 ℃, 26 ℃, 27 ℃, 28 ℃, 29 ℃, 30 ℃, 31 ℃, 32 ℃, 33 ℃, 34 ℃, 35 ℃, 36 ℃, 37 ℃, 38 ℃, 39 ℃, 40 ℃, 41 ℃, 42 ℃, 43 ℃, 44 ℃, 45 ℃, 46 ℃, 47 ℃, 48 ℃, 49 ℃ or 50 ℃.

As an alternative embodiment of the invention, the extraction time is from 5 to 60 min. The extraction time is too short, the extraction is incomplete, and the extraction effect is poor; the extraction time is too long, the process cycle is long, and the extraction economy is poor. Typical but non-limiting extraction times are: 5min, 6min, 7min, 8min, 9min, 10min, 12min, 14min, 16min, 18min, 20min, 22min, 24min, 26min, 28min, 30min, 35min, 40min, 45min, 50min, 55min or 60 min.

As an alternative embodiment of the present invention, the centrifugation rate is 5000-. The centrifugal speed is slow, the centrifugal time is short (or the sedimentation time is short), the separation is incomplete, and the separation effect is poor; long centrifugation time (or long sedimentation time), long process cycle and poor economical efficiency. The centrifugation rate is not limited to: 5000rpm, 5500rpm, 6000rpm, 6500rpm or 7000 rpm; centrifugation times are typically, but not limited to: 5min, 6min, 7min, 8min, 9min or 10min (or settling time typically but not limited to: 30min, 32min, 34min, 36min, 38min, 40min, 42min, 44min, 46min, 48min, 50min, 52min, 54min, 56min, 58min or 60 min).

The microemulsion extracting agent provided by the invention can be widely applied to the aspect of separating asphalt from heavy oil ore, and has the advantages of high extraction efficiency, good asphalt product quality, less solid entrainment, simple extraction process and mild conditions.

Example 1

5mol of tryptophan were added according to 1: dispersing 2(V: V) in water, adding 5mol of tetrafluoroboric acid aqueous solution, mixing, stirring at 25 ℃ for reacting for 18h, and rotationally evaporating at 80 ℃ for 10h to obtain wine red liquid ionic liquid; and mixing 1mol of ionic liquid and 3mol of urea, and stirring and reacting at 80 ℃ for 4 hours to obtain a yellow-brown liquid, namely the tryptophan tetrafluoroborate/urea eutectic reagent. The 1H-NMR chart of the eutectic reagent prepared in example 1 is shown in FIG. 1, and in FIG. 1, (a) is the 1H-NMR chart of tryptophan, (b) is the 1H-NMR chart of tryptophan tetrafluoroborate, (c) is the 1H-NMR chart of tryptophan tetrafluoroborate/urea, and (d) is the 1H-NMR chart of urea. The generation of the ionic liquid can be confirmed by comparing (a) and (b) in fig. 1, and the generation of the hydrogen bond can be confirmed by comparing (c) and (d) in fig. 1, and the eutectic reagent is successfully synthesized.

Example 2

5mol of histidine were added as 1: dispersing 2(V: V) in water, adding 4mol of tetrafluoroboric acid aqueous solution, mixing, stirring at 20 ℃ for reaction for 12h, and rotationally evaporating at 70 ℃ for 8h to obtain wine red liquid ionic liquid; and mixing 1mol of ionic liquid and 2mol of urea, and stirring and reacting at 70 ℃ for 6 hours to obtain a yellow-brown liquid, namely the histidine tetrafluoroborate/urea eutectic reagent.

Example 3

5mol of tryptophan were added according to 1: dispersing 2(V: V) in water, adding 6mol of hydrobromic acid aqueous solution, mixing, stirring at 30 ℃ for reaction for 24h, and rotationally evaporating at 90 ℃ for 12h to obtain wine red liquid ionic liquid; and mixing 1mol of ionic liquid and 4mol of urea, and stirring and reacting at 90 ℃ for 3 hours to obtain a yellow brown liquid, namely the tryptophan hydrobromide/urea eutectic reagent.

Example 4

5g of the tryptophan tetrafluoroborate/urea eutectic solvent provided in example 1 was weighed out, 5g of ethanol and 10g of toluene were added, and the mixture was mixed to form the extractant (about 12.5g for the lower microemulsion phase and about 7.5g for the upper toluene phase).

5g of Indonesia oil sand (the oil content of Indonesia oil sand is 28%) is put into an extraction container, the prepared extractant is added under stirring, and extraction is carried out for 30min under the condition of continuous stirring. After centrifugal separation, an upper layer extraction oil phase, a middle layer microemulsion phase and a lower layer sand grain are obtained. FIG. 2 is a schematic process flow diagram for extracting bitumen from oil sands using the extractant of the present invention.

Distilling the extracted oil phase to separate out solvent toluene to obtain asphalt oil; adding the distilled and recovered toluene into the middle-layer microemulsion phase, and recycling the toluene; the sand grains in the lower layer are washed by a small amount of water and can be discharged. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 93%.

The extracting agent provided by the invention can be widely applied to the aspect of separating asphalt from heavy oil ore, and has the advantages of high extraction efficiency, good asphalt product quality, less solid entrainment, easy recovery and reutilization.

Example 5

Example 5 differs from example 4 in that 5g of the tryptophan tetrafluoroborate/urea eutectic solvent provided in example 1 was weighed out, 7.5g propanol and 15g xylene were added, mixed to form an extractant (about 16g lower microemulsion phase and about 11.5g upper toluene phase) and used to extract 5g of tank bottom sludge (67% oil content of the tank bottom sludge). The remaining steps were the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 92%.

Example 6

Example 5 differs from example 4 in that 5g of the histidine tetrafluoroborate/urea eutectic solvent provided in example 1 was weighed out, 10g methanol and 15g cyclohexane were added, mixed to form an extractant (about 19.5g lower microemulsion phase and about 10.5g upper cyclohexane phase) and used to extract 5g of heavy oil. The remaining steps were the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 91%.

Example 7

Example 7 differs from example 4 in that 5g of the lysine tetrafluoroborate/urea eutectic solvent provided in example 1 was weighed out, 20g of ethanol and 20g of n-heptane were added, and after mixing, the extractant (about 31.5g for the lower microemulsion phase and about 13.5g for the upper n-heptane phase) was formed and used to extract 5g of oil shale (oil shale has an oil content of 6%). The remaining steps were the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to reach 87%.

As can be seen from the comparison between examples 4 to 6 and example 7, the mass ratio of the eutectic solvent, the low-alcohol and the weak-polar solvent is (1-2): (1-2): (2-4), the extraction effect of separating the asphalt from the heavy oil deposit is good, and the recovery rate of the asphalt is 93%.

Example 8

Example 8 differs from example 4 in that example 8 employs the tryptophan hydrobromide/urea eutectic reagent provided in example 3. The remaining procedure was the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 90%.

Example 9

Example 9 differs from example 4 in that 20g of the Indonesia oil sand (oil content of the Indonesia oil sand is 28%) are taken in example 9, and the remaining procedure is the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 85%.

Comparative example

Comparative example 1 differs from example 4 in that the extractant used was a mixture of 10g of the ionic liquid emimBF4 and 10g of toluene, the remaining procedure being the same as in example 4. According to the test result, the extraction agent can lead the recovery rate of the asphalt oil to be 83 percent. The microemulsion extracting agent for separating heavy oil and ore provided by the invention has the advantages of high extraction efficiency of asphalt in oil sand, good asphalt product quality, less solid entrainment, simple extraction process and mild reaction conditions.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims (10)

1. A microemulsion extractant for separating heavy oil ores is characterized in that: the eutectic solvent is formed by mixing three components of a eutectic solvent, a low-polyhydric alcohol and a weak polar solvent, wherein the eutectic solvent comprises the following components in percentage by weight: low polyhydric alcohol: the mass ratio of the weak polar solvent is (1-2): (1-2): (2-4);

the eutectic solvent is generated by the reaction of amino acid ionic liquid and urea, and the molar ratio of the amino acid ionic liquid to the urea is 1: (2-4), wherein the weak polar solvent is an aromatic hydrocarbon solvent or a chain hydrocarbon solvent.

2. The microemulsion extractant for heavy oil mine separation of claim 1, characterized in that: the weak polar solvent is toluene, xylene or n-heptane.

3. The microemulsion extractant for heavy oil mine separation of claim 1, characterized in that: the amino acid is tryptophan, lysine, phenylalanine or histidine.

4. The microemulsion extractant for heavy oil mine separation of claim 1, characterized in that: the lower alcohol is methanol, ethanol or propanol.

5. The microemulsion extractant for heavy oil mine separation of claim 1, characterized in that: the amino acid ionic liquid is prepared from amino acid and strong acid containing halogen.

6. The microemulsion extractant for heavy oil mine separation of claim 5, characterized in that: the strong acid containing halogen is hydrochloric acid, hydrobromic acid or tetrafluoroboric acid.

7. The microemulsion extractant for heavy oil mine separation of claim 6, characterized in that: the amino acid ionic liquid is prepared from amino acid and tetrafluoroboric acid, wherein the molar ratio of the amino acid to the tetrafluoroboric acid is 1: (0.7-1.5).

8. The microemulsion extractant for heavy oil ore separation according to claim 1 or 5, characterized in that: the preparation method of the eutectic solvent comprises the following steps:

⑴ dispersing amino acid in water, adding tetrafluoroboric acid solution, stirring to react, and rotary evaporating to obtain amino acid ionic liquid;

⑵ mixing the amino acid ionic liquid and urea uniformly, heating and reacting to obtain eutectic solvent.

9. A method for separating heavy oil ore by using microemulsion is characterized by comprising the following steps:

⑴ configuring the microemulsion of claim 1;

⑵ mixing and extracting the microemulsion extractant and the heavy oil mine, and separating the extracted mixture to obtain an oil phase layer, a microemulsion layer and a solid residue layer, wherein the mass ratio of the microemulsion to the heavy oil mine is (3-5):1, the extraction temperature is 20-50 ℃, and the extraction time is 5-60 min.

10. The method for heavy oil deposit separation with microemulsions according to claim 9, wherein said heavy oil deposit comprises oil sands, heavy oils, oil shales or oil sludge.

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