CN112625731B - System and method for separating oil product by eutectic solvent - Google Patents

System and method for separating oil product by eutectic solvent Download PDF

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CN112625731B
CN112625731B CN201910947870.2A CN201910947870A CN112625731B CN 112625731 B CN112625731 B CN 112625731B CN 201910947870 A CN201910947870 A CN 201910947870A CN 112625731 B CN112625731 B CN 112625731B
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aromatic hydrocarbon
tower
eutectic solvent
solvent
eutectic
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CN112625731A (en
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宋奇
郑均林
王宗霜
姜向东
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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China Petroleum and Chemical Corp
Sinopec Shanghai Research Institute of Petrochemical Technology
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
    • C10G21/06—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents characterised by the solvent used
    • C10G21/12—Organic compounds only
    • C10G21/16—Oxygen-containing compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1055—Diesel having a boiling range of about 230 - 330 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1048—Middle distillates
    • C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °C
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/30—Aromatics

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

The invention relates to a system and a method for separating oil products by using a eutectic solvent, belonging to the field of separation of polycyclic aromatic hydrocarbons in petroleum or petroleum fractions. The system for separating oil products by using the eutectic solvent comprises the following units: a non-aromatic hydrocarbon removing tower A, an aromatic hydrocarbon separation tower B, a monocyclic aromatic hydrocarbon separation tower C and a polycyclic aromatic hydrocarbon separation tower D; the system can separate oil products into three major components, namely non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon. Moreover, the system can also comprise a regeneration tower E of the eutectic solvent and a regeneration tower F of the eutectic solvent of the extracting agent, and can realize continuous separation and regeneration of the extracting agent.

Description

System and method for separating oil product by eutectic solvent
Technical Field
The invention relates to the field of separation of polycyclic aromatic hydrocarbons in petroleum or petroleum fractions, and further relates to a system and a method for separating oil products by using a eutectic solvent.
Background
The quality of oil products such as coking gasoline diesel oil, catalytic diesel oil, heavy diesel oil and the like is poor, and the oil products can be used by further conversion. Due to the complex components, the oil products are directly sent into a reactor for conversion, so that the conversion target is not strong, and over-conversion and over-hydrogen consumption are easily caused. Meanwhile, the conversion difficulty of each component in the oil product is different, so that light hydrocarbon is easily excessively cracked, polycyclic aromatic hydrocarbon is easily formed after monocyclic aromatic hydrocarbon is converted again, and the resource utilization rate is not high. Because the raw material components are widely distributed, the general catalyst is more easily subjected to carbon deposition inactivation, so that the service life of the catalyst is shortened. Thus, separation prior to conversion can greatly improve efficiency.
The solvent extraction and extraction rectification technology developed in the existing industry has better separation effect and is widely applied, but has the problems of high energy consumption, easy deterioration of the extraction solvent, easy corrosion of the device and the like, and has still room for improvement in the technology. In addition, effective separation of monocyclic and polycyclic aromatic hydrocarbons still presents certain difficulties. Therefore, the development of a novel efficient green extraction solvent and the improvement of the separation efficiency of aromatic hydrocarbon are the development directions in the future.
The Deep Eutectic Solvent (DES) is used as a novel green solvent, has the properties similar to those of ionic liquid, extremely low volatility and stable physical properties, and shows excellent dissolving and separating capacity for various organic mixture systems. The eutectic solvent used in the separation process is generally formed by hydrogen bond acceptor (such as organic salt choline chloride, quaternary ammonium salt, quaternary phosphonium salt, etc.) and hydrogen bond donor (such as urea, hexylene glycol, sorbitol, butylene glycol, malic acid, amino acid, glucose, etc.) through hydrogen bond interaction, and thus has strong polarity. Eutectic solvents can also achieve a certain specific functional property by designing different combinations of hydrogen bond acceptors and hydrogen bond donors. Compared with the traditional ionic liquid, the eutectic solvent generally has polarity, is simple to prepare, has weak corrosivity, and can be biodegraded. Due to the excellent characteristics, the eutectic solvent has the tendency of replacing the traditional organic solvent and ionic liquid for chemical separation, has good application prospect in the extraction and separation of aromatic hydrocarbon and alkane mixtures, and is greatly concerned. The authors found that the shorter the alkyl chain on the quaternary ammonium salt, the more advantageous it was to separate toluene, than the DES which had been reported in the literature for tetraethylammonium chloride with levulinic acid and ethylene glycol and was used to separate toluene/heptane mixed systems (Wang Y, hou Y C, wu W Z, et al. Patent CN107311833A describes the separation of toluene/cyclohexane systems using a DES of tetrabutylammonium bromide with levulinic acid or ethylene glycol. However, the effect of polycyclic aromatic hydrocarbon separation is unclear. In addition, the eutectic solvent is used as an extracting agent to operate in a batch rectifying tower, cannot operate continuously, and has no solvent regeneration system.
In the existing literature, relevant reports are rarely found on the simultaneous separation of three major components of non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon of oil products, and particularly, the separation of polycyclic aromatic hydrocarbon and monocyclic aromatic hydrocarbon mostly needs to be carried out by means of rectification and the like, so that the energy consumption is high and the efficiency is low. Meanwhile, under the heating temperature, the polycyclic aromatic hydrocarbon is easy to continue to generate side reactions such as condensation and the like, so that the quality of the polycyclic aromatic hydrocarbon is worse. Therefore, the continuous and stable operation of the polycyclic aromatic hydrocarbon cannot be met by directly adopting a distillation or rectification mode. In addition, how to realize continuous separation and regeneration of the extracting agent after the polycyclic aromatic hydrocarbon is extracted by the eutectic solvent is also a problem to be solved.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a system for separating oil products by using a eutectic solvent, and particularly relates to a system and a method for separating oil products by using the eutectic solvent. The system can separate oil products into three major components, namely non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon.
One of the purposes of the invention is to provide a system for separating oil products by eutectic solvent, which can comprise the following units: a non-aromatic hydrocarbon removing tower A, an aromatic hydrocarbon separation tower B, a monocyclic aromatic hydrocarbon separation tower C and a polycyclic aromatic hydrocarbon separation tower D; the following connection relations can be included among the units:
wherein, an outlet of the non-aromatic hydrocarbon removing tower A is connected with an inlet at the bottom of the aromatic hydrocarbon separation tower B, and an outlet at the top of the aromatic hydrocarbon separation tower B is connected with an inlet at the bottom of the monocyclic aromatic hydrocarbon separation tower C;
an outlet of the monocyclic aromatic hydrocarbon separation tower C is connected with an inlet of the polycyclic aromatic hydrocarbon separation tower D;
introducing a eutectic solvent X and an oil product into the non-aromatic hydrocarbon removing tower A, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting the obtained non-aromatic hydrocarbon, pumping out the obtained non-aromatic hydrocarbon, allowing the rest mixed aromatic hydrocarbon and a mixed material flow of the eutectic solvent X to enter the aromatic hydrocarbon separation tower B, performing an extraction process with a solvent S, extracting to form a material flow of the eutectic solvent X and the solvent S and a mixed aromatic hydrocarbon material flow, allowing the mixed aromatic hydrocarbon material flow to enter the monocyclic aromatic hydrocarbon separation tower C to contact with the eutectic solvent Y, completing the liquid-liquid extraction process, extracting the formed monocyclic aromatic hydrocarbon material flow, allowing the formed mixed material flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon to enter the polycyclic aromatic hydrocarbon separation tower D to contact with the solvent S, and forming and extracting polycyclic aromatic hydrocarbon at the tower top; the remaining eutectic solvent Y forms a mixture stream effluent with solvent S.
The extraction positions of non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon respectively extracted by the non-aromatic hydrocarbon removing tower A, the monocyclic aromatic hydrocarbon separating tower C and the polycyclic aromatic hydrocarbon separating tower D are any position of the tower surface, and are preferably selected from the tower top or the tower side.
Preferably, the system may further include a eutectic solvent regenerator column E and a eutectic solvent regenerator column F;
an outlet of the polycyclic aromatic hydrocarbon separation tower D is connected with an inlet of the eutectic solvent regeneration tower E, and an outlet of the regeneration tower E is connected with an inlet of the monocyclic aromatic hydrocarbon separation tower C; an outlet of the regeneration tower E is connected with an inlet of the polycyclic aromatic hydrocarbon separation tower D;
an outlet of the aromatic hydrocarbon separation tower B is connected with an inlet of the eutectic solvent regeneration tower F;
an outlet of the eutectic solvent regeneration tower F is connected with an inlet of the non-aromatic hydrocarbon removing tower A;
the flow of the eutectic solvent X and the solvent S flows out of the aromatic separation tower B and enters a eutectic solvent regeneration tower F for flash evaporation to extract the solvent S and obtain the regenerated eutectic solvent X at the same time, and the flow returns to the dearomatization tower A for recycling;
and a mixed material flow formed by the eutectic solvent Y and the solvent S flows out of the tower D, enters the eutectic solvent regeneration tower E, is subjected to flash evaporation, the extracted solvent S returns to the polycyclic aromatic hydrocarbon separation tower D for use, and the regenerated eutectic solvent Y returns to the monocyclic aromatic hydrocarbon separation tower C for recycling.
The oil product is selected from one or more of heavy gasoline, light diesel oil, catalytic diesel oil, heavy diesel oil, coker gasoline and coker diesel oil; the non-aromatic hydrocarbon in the oil product is one or more of C1-C20 straight chain, branched chain alkane and cyclane.
The eutectic solvent X may comprise a hydrogen bond acceptor and a hydrogen bond donor; the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1: 0.5-1:8;
wherein the content of the first and second substances,
the hydrogen bond acceptor is selected from one or more of tetraethyl ammonium halide, tetrabutyl ammonium halide, choline chloride, betaine, methyl triethyl ammonium halide, tetraphenyl phosphonium halide, methyl triphenyl phosphonium halide, ethyl triphenyl phosphonium halide and butyl triphenyl phosphonium halide; preferably one or more of tetrabutylammonium halide, methyltriethylammonium halide, tetraphenylphosphonium halide, methyltriphenylphosphonium halide, ethyltriphenylphosphonium halide and butyltriphenylphosphonium halide;
the hydrogen bond donor is selected from one or more of urea, citric acid, succinic acid, propionic acid, acetic acid, ethylene glycol, propylene glycol, glycerol, xylitol, glucose, levulinic acid, tributyl phosphate, dimethylformamide, morpholine, oxalic acid and lactic acid; preferably one or more of succinic acid, levulinic acid, tributyl phosphate, dimethylformamide, lactic acid and propionic acid.
The preparation method of the eutectic solvent X may include the steps of:
and mixing and stirring the hydrogen bond acceptor and the hydrogen bond donor at the temperature of 20-180 ℃, preferably 20-120 ℃, and more preferably 20-85 ℃ uniformly according to the using amount to obtain the hydrogen bond acceptor and the hydrogen bond donor.
The eutectic solvent Y may comprise a hydrogen bond acceptor and a hydrogen bond donor, a lewis acid salt; the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1: 0.5-1:8;
the mass of the Lewis acid salt is 0.1-20% of the total mass of the eutectic solvent, and preferably 0.1-8%;
wherein the content of the first and second substances,
the hydrogen bond acceptor is selected from one or more of tetraethyl ammonium halide, tetrabutyl ammonium halide, choline chloride, betaine, methyl triethyl ammonium halide, tetraphenyl phosphonium halide, methyl triphenyl phosphonium halide, ethyl triphenyl phosphonium halide and butyl triphenyl phosphonium halide; the hydrogen bond acceptor is preferably one or more of tetrabutyl ammonium halide, methyltriethyl ammonium halide, tetraphenyl phosphonium halide, methyltriphenyl phosphonium halide, ethyltriphenyl phosphonium halide and butyltriphenyl phosphonium halide;
the hydrogen bond donor is selected from one or more of urea, citric acid, succinic acid, propionic acid, acetic acid, ethylene glycol, propylene glycol, glycerol, xylitol, glucose, levulinic acid, tributyl phosphate, dimethylformamide, morpholine, oxalic acid and lactic acid; the donor is preferably one or more of succinic acid, levulinic acid, tributyl phosphate, dimethylformamide, lactic acid and propionic acid;
the Lewis acid salt is selected from SnCl 2 ,SnCl 4 ,ZnCl 2 ,GeCl 2 ,InCl 3 ,GaCl 3 ,FeCl 2 ,FeCl 3 ,LaCl 3 ,CuCl 2 ,DyCl 3 ,CrCl 3 ,CrCl 2 ,La(OTf) 3 And YbCl 3 One or more of (a); preferably SnCl 2 ,SnCl 4 ，LaCl 3 ,ZnCl 2 、CrCl 3 ,CrCl 2 ,GaCl 3 One or more of (a).
The solvent S can be one of water, methanol, ethyl acetate and butyl acetate.
The preparation method of the eutectic solvent Y may include the steps of:
and mixing and stirring the hydrogen bond acceptor, the hydrogen bond donor and the Lewis acid salt uniformly at the temperature of between 20 and 180 ℃, preferably between 20 and 120 ℃, and more preferably between 20 and 85 ℃ according to the using amount to obtain the hydrogen bond acceptor-hydrogen bond donor-Lewis acid salt.
Another object of the present invention is to provide a method for oil separation by eutectic solvent in the system, which comprises the following steps:
1) Respectively introducing an oil product and a eutectic solvent X into the non-aromatic hydrocarbon removing tower A, carrying out a reverse contact liquid-liquid extraction process in the non-aromatic hydrocarbon removing tower A, extracting non-aromatic hydrocarbon from the non-aromatic hydrocarbon removing tower A, and feeding a mixture flow of the residual mixed aromatic hydrocarbon and the eutectic solvent X into the aromatic hydrocarbon separation tower B;
2) In the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from an inlet at one side, the solvent S enters from the other side of the aromatic hydrocarbon separation tower B, the mixed aromatic hydrocarbon and the solvent S are contacted in the tower, and the mixed aromatic hydrocarbon material flow is formed after extraction and flows out to enter the single-ring aromatic hydrocarbon separation tower C;
the mixture of the residual eutectic solvent X and the solvent S flows out through the bottom outlet of the aromatic separation tower B;
3) After entering the inlet of the monocyclic aromatic hydrocarbon separation tower C, the mixed aromatic hydrocarbon material flow contacts with a eutectic solvent Y in the tower C to complete the liquid-liquid extraction process, the formed monocyclic aromatic hydrocarbon material flow is extracted, and the rest of the mixed material flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows out to enter the polycyclic aromatic hydrocarbon separation tower D;
4) After entering the polycyclic aromatic hydrocarbon separation tower D, the mixture flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon contacts with the solvent S, and the formed polycyclic aromatic hydrocarbon is extracted; and the rest mixture flow of the eutectic solvent Y and the solvent S flows out of the polycyclic aromatic hydrocarbon separation tower D.
Preferably, the first and second electrodes are formed of a metal,
the mixture flow of the eutectic solvent X and the solvent S flowing out of the aromatic hydrocarbon separation tower B enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; simultaneously obtaining a regenerated eutectic solvent X, and returning the material flow to the non-aromatic removal tower A for recycling;
and after the mixture flow of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E and is subjected to flash evaporation, the solvent S formed at the tower top returns to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y formed at the tower bottom returns to the monocyclic aromatic hydrocarbon separation tower C for recycling.
The extraction positions of non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon respectively extracted by the non-aromatic hydrocarbon removing tower A, the monocyclic aromatic hydrocarbon separating tower C and the polycyclic aromatic hydrocarbon separating tower D are any position of the tower surface, and are preferably selected from the tower top or the tower side.
Most preferably, the system is used for a method for separating oil products by eutectic solvent, and comprises the following steps:
i) Respectively introducing an oil product and a eutectic solvent X into the non-aromatic hydrocarbon removing tower A, carrying out a liquid-liquid extraction process of reverse contact between the oil product and the eutectic solvent X in the tower, extracting non-aromatic hydrocarbon from the top of the tower, and feeding a mixture flow of the residual mixed aromatic hydrocarbon and the eutectic solvent X into an aromatic hydrocarbon separation tower B;
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side of the aromatic hydrocarbon separation tower B, the solvent S enters from the top side of the aromatic hydrocarbon separation tower B, the mixed aromatic hydrocarbon and the solvent S are contacted in the tower B, and the mixed aromatic hydrocarbon material flow is formed after extraction and flows out from the outlet at the top of the aromatic hydrocarbon separation tower B and enters the monocyclic aromatic hydrocarbon separation tower C;
the mixture of the residual eutectic solvent X and the solvent S flows out from the bottom outlet of the aromatic separation tower B and enters the eutectic solvent regeneration tower F;
iii) The mixed aromatic hydrocarbon material flow enters from the bottom side of the monocyclic aromatic hydrocarbon separation tower C and contacts with a eutectic solvent Y entering from the top side of the tower to finish the liquid-liquid extraction process, and monocyclic aromatic hydrocarbon material flow is formed at the top of the tower and is extracted; a mixture flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows out from an outlet at the bottom of the monocyclic aromatic hydrocarbon separation tower C and enters the polycyclic aromatic hydrocarbon separation tower D;
iv) the mixture flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, and returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling;
v) after the mixture flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon enters the polycyclic aromatic hydrocarbon separation tower D, the mixture flow contacts with a solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture flow of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E;
vi) after the mixture flow of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E and is subjected to flash evaporation, the solvent S formed at the top of the tower returns to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y formed at the bottom of the tower returns to the monocyclic aromatic hydrocarbon separation tower C for recycling.
Wherein the content of the first and second substances,
the aromatic hydrocarbon separation tower B and the eutectic solvent regeneration tower E are filled with the solvent S, and the injection volume of the solvent S can be 0.2 to 10 times, preferably 0.5 to 5 times of the volume of the eutectic solvent filled in the tower. (the multiple is applicable to both the B tower and the E tower)
The overhead pressure of the A-F separation tower can be 20-1500 kPa. Preferably, the ABCD four column pressure ranges from 90 to 1500kPa, more preferably from 90 to 800kPa, and the EF column pressure is preferably from 20 to 90kPpa.
The temperature of the non-aromatic hydrocarbon removing tower A and the monocyclic aromatic hydrocarbon separating tower C can be 10-120 ℃, and preferably 10-60 ℃.
The temperature of the aromatic hydrocarbon separation tower B and the temperature of the polycyclic aromatic hydrocarbon separation tower D are both 10-100 ℃, preferably 10-50 ℃.
The temperatures of the eutectic solvent regeneration tower E and the eutectic solvent regeneration tower F are both 10-300 ℃, preferably the temperature of the eutectic solvent regeneration tower E is 30-120 ℃, and the temperature of the eutectic solvent regeneration tower F is 60-150 ℃.
The volume ratio of the eutectic solvent X to the oil to be extracted in the tower A is 1/0.2-1/50, preferably 1/0.2-1/10, and further preferably 1/0.2-1/5; the volume ratio of the eutectic solvent Y to the oil to be extracted in the C tower is 1/0.2-1/50, preferably 1/0.2-1/20, and more preferably 1/0.2-1/5.
The technical scheme of the application discloses a technological process capable of continuously extracting and separating non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon, and oil can be separated into non-aromatic hydrocarbon, monocyclic aromatic hydrocarbon and polycyclic aromatic hydrocarbon through separation towers A-D and regeneration towers E and F of an extracting agent; and can realize continuous separation and regeneration of the extracting agent. The intermittent operation mode is avoided, the operation cost is lower in comparison, the leakage problem of eutectic solvent and organic materials in the intermittent mode is avoided, and the overall economy and environmental protection performance are improved to a great extent.
Drawings
FIG. 1 is a flow chart of aromatic separation in the system for oil separation by eutectic solvent according to the present invention; wherein, A is a non-aromatic hydrocarbon removing tower, B is an aromatic hydrocarbon separation tower, C is a monocyclic aromatic hydrocarbon separation tower, D is a polycyclic aromatic hydrocarbon separation tower, E is a eutectic solvent regeneration tower, and F is a eutectic solvent regeneration tower; 1.2, 3, 4, 5, 6, 7, 8, 9, 10, 11 and 12 are pipelines respectively; s is a solvent S; x is a supplemental low cosolvent X; y is a supplemental low co-solvent Y.
Detailed Description
The following detailed description of the embodiments of the present invention is provided, but it should be noted that the scope of the present invention is not limited by the embodiments, but is defined by the appended claims.
[ example 1 ] A method for producing a polycarbonate
The system for separating the oil product by the eutectic solvent is built, and specifically comprises the following steps:
the system for separating oil products by using the eutectic solvent comprises the following units: a non-aromatic hydrocarbon removing tower A, an aromatic hydrocarbon separation tower B, a monocyclic aromatic hydrocarbon separation tower C, a polycyclic aromatic hydrocarbon separation tower D, a eutectic solvent regeneration tower E and a eutectic solvent regeneration tower F; the units are built according to the following connection relation:
wherein, an outlet of the non-aromatic hydrocarbon removing tower A is connected with an inlet of the bottom of the aromatic hydrocarbon separation tower B through a pipeline 4, and an outlet of the top of the aromatic hydrocarbon separation tower B is connected with an inlet of the bottom of the monocyclic aromatic hydrocarbon separation tower C through a pipeline 5;
the outlet at the bottom of the monocyclic aromatic hydrocarbon separation tower C is connected with the inlet of the polycyclic aromatic hydrocarbon separation tower D through a pipeline 8;
an outlet of the polycyclic aromatic hydrocarbon separation tower D is connected with an inlet of the eutectic solvent regeneration tower E through a pipeline 11, and an outlet of the bottom of the regeneration tower E is connected with an inlet of the monocyclic aromatic hydrocarbon separation tower C through a pipeline 12; an outlet at the top of the eutectic solvent regeneration tower E is connected with an inlet of the polycyclic aromatic hydrocarbon separation tower D through a pipeline 9;
an outlet at the bottom of the aromatic hydrocarbon separation tower B is connected with an inlet of the eutectic solvent regeneration tower F through a pipeline 6; and the bottom outlet of the eutectic solvent regeneration tower F is connected with the inlet of the non-aromatic hydrocarbon removing tower A.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass.
The specific separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is methyl triphenyl phosphonium bromide/levulinic acid, the molar ratio of the methyl triphenyl phosphonium bromide to the levulinic acid is 1/3, and the components are mixed and stirred uniformly at 60 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B is water.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; a mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D; the eutectic solvent Y used was methyltriphenylphosphonium bromide/levulinic acid in a molar ratio of 1/3. At the same time, snCl is added into the eutectic solvent Y 2 Adding 1.2% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/3.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is water;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, after flash evaporation, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y is formed at the bottom of the tower and returned to the tower C for recycling.
After separation, the obtained non-aromatic, monocyclic and polycyclic oil products account for the total mass of the raw oil respectively as follows: non-aromatic hydrocarbon 43.97%, monocyclic aromatic hydrocarbon 40.95% and polycyclic aromatic hydrocarbon 15.00%.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 30 30 30 30 30 60
Operating pressure/kPa 100 100 100 100 90 80
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1 1
[ example 2 ]
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is tetraphenylphosphonium chloride/dimethylformamide with the molar ratio of 1/5, and the components are mixed and stirred uniformly at 30 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/0.2.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B is water.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the inlet on the side of the tower bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the inlet on the side of the tower top in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the tower top is extracted from a pipeline 7; the material flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower enters the polycyclic aromatic hydrocarbon separation tower D through a pipeline 8. The eutectic solvent Y used was methyltriphenylphosphonium bromide/dimethylformamide in a molar ratio of 1/5. At the same time, snCl is added into the eutectic solvent Y 2 Adding the eutectic solvent Y with the mass accounting for 0.5 percent of the total mass of the eutectic solvent Y, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/1.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; the regenerated eutectic solvent X is obtained at the bottom of the tower, the material flow returns to the dearomatization tower A again for recycling, and the solvent S is water;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the rest mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, after flash evaporation, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y is formed at the bottom of the tower and returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: 8978 percent of non-aromatic hydrocarbon, 8978 percent of zxft 8978 percent, 40.62 percent of monocyclic aromatic hydrocarbon and 14.85 percent of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 10 30 30 30 30 60
Operating pressure/kPa 100 200 100 100 20 80
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1 1
[ example 3 ]
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after heavy diesel oil of a certain refinery is adopted as a raw material and subjected to hydrocracking, an analysis result shows that the quality composition of the catalyst diesel oil hydrocracking oil is 35% of non-aromatic hydrocarbon, 38% of monocyclic aromatic hydrocarbon and 27% of polycyclic aromatic hydrocarbon. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is tetrabutylammonium chloride/lactic acid with the molar ratio of 1/5, and the components are mixed and stirred uniformly at 40 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B was butyl acetate.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D. The eutectic solvent Y is tetraphenylphosphonium chloride/lactic acid in a molar ratio of 1/2. At the same time, snCl is added into the eutectic solvent Y 4 And adding 2% of eutectic solvent Y by mass, and mixing and stirring the three components uniformly at 60 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/3.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is butyl acetate;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use after flash evaporation, and the eutectic solvent Y formed at the bottom of the tower is returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: 34.81 percent of non-aromatic hydrocarbon, 37.54 percent of monocyclic aromatic hydrocarbon and 26.89 percent of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 30 30 10 30 30 60
Operation ofpressure/kPa 200 100 500 100 40 20
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 0.5 3
[ example 4 ]
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by using coking diesel oil of a certain refinery, an analysis result shows that the quality composition of the catalyst diesel oil hydrocracking oil is 31% of non-aromatic hydrocarbon, 35% of monocyclic aromatic hydrocarbon and 34% of polycyclic aromatic hydrocarbon. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is tetrabutyl ammonium chloride/succinic acid with the molar ratio of 1/3, and the components are mixed and stirred uniformly at 80 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow and the solvent S are contacted in the tower B, the mixed aromatic hydrocarbon material flow is formed after extraction, the mixed aromatic hydrocarbon material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the residual mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B was ethyl acetate.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the inlet on the side of the tower bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the inlet on the side of the tower top in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the tower top is extracted from a pipeline 7; the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D. The eutectic solvent Y is methyl triphenyl phosphonium bromide/succinic acid, and the molar ratio of the methyl triphenyl phosphonium bromide to the succinic acid is 1/0.5. Simultaneously, feCl is added into the eutectic solvent Y 3 Adding 1% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 80 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/3.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is ethyl acetate;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, after flash evaporation, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y is formed at the bottom of the tower and returned to the tower C for recycling.
After separation, the obtained non-aromatic, monocyclic and polycyclic oil products account for the total mass of the raw oil respectively as follows: 30.89% of non-aromatic hydrocarbon, 34.85% of monocyclic aromatic hydrocarbon and 4736% of polycyclic aromatic hydrocarbon, namely 33.95%.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 25 25 25 25 50 80
Operating pressure/kPa 100 200 100 100 60 50
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1 5
[ example 5 ] A method for producing a polycarbonate
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is ethyl triphenyl phosphonium chloride/succinic acid, the molar ratio of the ethyl triphenyl phosphonium chloride to the succinic acid is 1/1, and the components are mixed and stirred uniformly at the temperature of 20 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B is water.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D. The eutectic solvent Y is ethyl triphenyl phosphonium chloride/lactic acid, and the molar ratio of the ethyl triphenyl phosphonium chloride to the lactic acid is 1/5. Meanwhile, laCl is added into the eutectic solvent 3 And adding 2.5% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/5.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; the regenerated eutectic solvent X is obtained at the bottom of the tower, the material flow returns to the dearomatization tower A again for recycling, and the solvent S is water;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8, enters the polycyclic aromatic hydrocarbon separation tower D, contacts with the solvent S, and forms the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, after flash evaporation, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y is formed at the bottom of the tower and returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: 3238% of non-aromatic hydrocarbon, 3262% of monocyclic aromatic hydrocarbon and 14.96% of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 40 50 50 50 80 80
Operating pressure/kPa 100 100 100 100 60 60
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1.5 1.5
[ example 6 ]
The same system as in example 1 was used.
The method for separating oil products by using the eutectic solvent specifically comprises the following steps:
after the raw material adopts light diesel oil of a certain refinery to carry out hydrocracking, the analysis result shows that the quality composition of the diesel oil hydrocracking oil of the catalyst comprises 39% of non-aromatic hydrocarbon, 39% of monocyclic aromatic hydrocarbon and 22% of polycyclic aromatic hydrocarbon. The separation process is as follows:
i) Introducing a raw oil product into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbons from a tower top pipeline 3, and allowing a residual mixture of mixed aromatic hydrocarbons and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is tetraphenylphosphonium bromide/propionic acid, the molar ratio of the tetraphenylphosphonium bromide to the propionic acid is 1/0.5, and the components are mixed and stirred uniformly at 40 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters a regeneration tower F of the eutectic solvent X from a tower bottom pipeline 6. The solvent S entering from the top side of column B was butyl acetate.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; the stream of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower enters the polycyclic aromatic hydrocarbon separation tower D through a pipeline 8. The eutectic solvent Y used was methyltriethylamine chloride/levulinic acid in a molar ratio of 1/3. Meanwhile, gaCl is added into the eutectic solvent Y 3 Adding 1.5% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/0.2.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is butyl acetate;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use after flash evaporation, and the eutectic solvent Y formed at the bottom of the tower is returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: the non-aromatic hydrocarbon accounts for 38.95 percent, the monocyclic aromatic hydrocarbon accounts for 39.00 percent, and the polycyclic aromatic hydrocarbon accounts for 21.50 percent.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 25 25 25 25 50 120
Operating pressure/kPa 100 100 800 100 40 60
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1.2 1.2
[ example 7 ] A method for producing a polycarbonate
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is methyl triethyl amine chloride/levulinic acid, the molar ratio of the methyl triethyl amine chloride to the levulinic acid is 1/8, and the components are mixed and stirred uniformly at 50 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent X to the inlet raw oil of the tower A is 1/1.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B is methanol.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; a mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D; the eutectic solvent Y is methyl triethyl amine chloride/tributyl phosphate with the molar ratio of 1/1. At the same time, crCl is added into the eutectic solvent Y 2 Adding eutectic solvent Y in the amount of 1 wt% and mixing at 50 deg.c to obtain eutectic solvent YAnd a melting solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/1.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is methanol;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the rest mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use after flash evaporation, and the eutectic solvent Y formed at the bottom of the tower is returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: 43.64 percent of non-aromatic hydrocarbon, 40.62 percent of monocyclic aromatic hydrocarbon and 14.71 percent of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 60 50 60 50 100 150
Operating pressure/kPa 100 700 100 100 80 90
The volume of S solvent entering the columns B and D is compared with the volume of eutectic solvent entering the bottom of the column B as shown in the following table.
B D
Volume ratio V S solvent /V DES of B column 1.2 1.2
[ example 8 ]
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is methyl triphenyl phosphonium/lactic acid, the molar ratio of the methyl triphenyl phosphonium to the lactic acid is 1/3, and the components are mixed and stirred uniformly at the temperature of 60 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent X to the inlet raw oil of the tower A is 1/3.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B was butyl acetate.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; a mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon formed at the bottom of the tower flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D; the eutectic solvent Y is tetrabutylammonium chloride/succinic acid, and the molar ratio of the tetrabutylammonium chloride to the succinic acid is 1/1. At the same time, at the above-mentioned lowZnCl is added into a eutectic solvent Y 2 And adding 3% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/3.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the bottom of the tower, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is butyl acetate;
v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the rest mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use after flash evaporation, and the eutectic solvent Y formed at the bottom of the tower is returned to the tower C for recycling.
After separation, the obtained non-aromatic, single-ring and multi-ring oil products account for the total mass of the raw oil respectively as follows: 43.78% of non-aromatic hydrocarbon, 40.67% of monocyclic aromatic hydrocarbon and 14.80% of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 30 30 30 30 50 80
Operating pressure/kPa 100 100 100 100 40 40
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1.2 1.2
[ example 9 ]
The same system as in example 1 was used.
The method for separating oil products by using eutectic solvent specifically comprises the following steps:
after the raw material is subjected to hydrocracking by adopting catalytic diesel oil of a certain refinery, an analysis result shows that the catalytic diesel oil hydrocracking oil comprises 44% of non-aromatic hydrocarbons, 41% of monocyclic aromatic hydrocarbons and 15% of polycyclic aromatic hydrocarbons by mass. The separation process is as follows:
i) Introducing raw oil into the non-aromatic hydrocarbon removing tower A through a pipeline 2, introducing a eutectic solvent X into the tower A through a pipeline 1, performing a liquid-liquid extraction process of reverse contact in the tower A, extracting non-aromatic hydrocarbon from a tower top pipeline 3, and allowing a mixture of the residual mixed aromatic hydrocarbon and the eutectic solvent X to flow into an aromatic hydrocarbon separation tower B through a pipeline 4; the eutectic solvent X is methyl triethyl amine chloride/levulinic acid, the molar ratio of the methyl triethyl amine chloride to the levulinic acid is 1/3, and the components are mixed and stirred uniformly at 50 ℃ to obtain the eutectic solvent X. The ratio of the added eutectic solvent X to the inlet raw oil of the tower A is 1/5.
ii) in the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X enters from the bottom side, the solvent S enters from the top side of the tower B, the mixed aromatic hydrocarbon material flow is formed after the extraction by contacting the mixed aromatic hydrocarbon material flow and the solvent S in the tower B, the mixed material flow flows out from the top of the tower B through a pipeline 5 and enters a monocyclic aromatic hydrocarbon separation tower C, and the rest mixed material flow of the eutectic solvent X and the solvent S enters the eutectic solvent regeneration tower F from a tower bottom pipeline 6. The solvent S entering from the top side of column B is water.
iii) The mixed aromatic hydrocarbon flow enters the monocyclic aromatic hydrocarbon separation tower C from the side inlet at the bottom of the tower C through a pipeline 5, and contacts with a eutectic solvent Y entering from the side inlet at the top of the tower in the tower C to finish the liquid-liquid extraction process, and a monocyclic aromatic hydrocarbon flow formed at the top of the tower is extracted from a pipeline 7; the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon is formed at the bottom of the towerThe stream enters the polycyclic aromatic hydrocarbon separation column D via line 8. The eutectic solvent Y used was butyltriphenylphosphonium chloride/levulinic acid in a molar ratio of 1/3. At the same time, crCl is added into the eutectic solvent Y 2 And adding 5% of eutectic solvent Y by mass, and mixing and stirring the components uniformly at 50 ℃ to obtain the eutectic solvent Y. The volume ratio of the eutectic solvent Y entering the tower C to the inlet oil of the tower C is 1/3.
iv) the mixture of the eutectic solvent X and the solvent S flows through a pipeline 6 and enters the eutectic solvent regeneration tower F for flash evaporation, and the solvent S is extracted from the tower top; obtaining a regenerated eutectic solvent X at the tower top, returning the material flow to the non-aromatic hydrocarbon removing tower A for recycling, wherein the solvent S is water; v) the mixture of the eutectic solvent Y and the polycyclic aromatic hydrocarbon flows through a pipeline 8 and enters the polycyclic aromatic hydrocarbon separation tower D, and then contacts with the solvent S to form the polycyclic aromatic hydrocarbon at the tower top and is extracted; the mixture of the residual eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11;
vi) the mixture of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E through a pipeline 11, after flash evaporation, the solvent S is extracted from the top of the tower and returned to the polycyclic aromatic hydrocarbon separation tower D for use, and the eutectic solvent Y is formed at the bottom of the tower and returned to the tower C for recycling.
After separation, the obtained oil products account for the total mass of the raw oil respectively as follows: 43.60 percent of non-aromatic hydrocarbon, 8978 percent of monocyclic aromatic hydrocarbon and 14.70 percent of polycyclic aromatic hydrocarbon.
The operating pressure and operating temperature of each column are as follows.
A B C D E F
Operating temperature/. Degree.C 30 30 30 30 50 60
Operating pressure/kPa 100 100 100 100 20 30
The volume of S solvent entering the B and D towers and the volume of eutectic solvent entering the bottom of the B tower are shown below.
B D
Volume ratio V S solvent /V DES of B column 1.2 1.2

Claims (27)

1. A system for separating oil products by eutectic solvent is characterized by comprising the following units: a non-aromatic hydrocarbon removing tower A, an aromatic hydrocarbon separation tower B, a monocyclic aromatic hydrocarbon separation tower C and a polycyclic aromatic hydrocarbon separation tower D;
wherein, an outlet of the non-aromatic hydrocarbon removing tower A is connected with an inlet of the aromatic hydrocarbon separation tower B, and an outlet of the aromatic hydrocarbon separation tower B is connected with an inlet of the monocyclic aromatic hydrocarbon separation tower C;
an outlet of the monocyclic aromatic hydrocarbon separation tower C is connected with an inlet of the polycyclic aromatic hydrocarbon separation tower D;
the method comprises the following steps of performing liquid-liquid extraction on a eutectic solvent X and an oil product in a non-aromatic hydrocarbon removing tower A, extracting the non-aromatic hydrocarbon obtained after extraction, feeding the rest of mixed aromatic hydrocarbon and a mixed material flow of the eutectic solvent X into an aromatic hydrocarbon separation tower B, performing an extraction process on the mixed material flow and the solvent S to form a material flow of the eutectic solvent X and the solvent S and a mixed aromatic hydrocarbon material flow, feeding the mixed aromatic hydrocarbon material flow into a monocyclic aromatic hydrocarbon separation tower C to contact with a eutectic solvent Y to form monocyclic aromatic hydrocarbon material flow, extracting, feeding the formed mixed material flow of the eutectic solvent Y and polycyclic aromatic hydrocarbon into a polycyclic aromatic hydrocarbon separation tower D to contact with the solvent S to form polycyclic aromatic hydrocarbon, extracting, and feeding the rest of the eutectic solvent Y and the solvent S together to form a mixed material flow and flowing out;
the eutectic solvent X comprises a hydrogen bond acceptor and a hydrogen bond donor; the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1 to 0.1 to 1; the hydrogen bond acceptor is selected from one or more of tetraethyl ammonium halide, tetrabutyl ammonium halide, choline chloride, betaine, methyl triethyl ammonium halide, tetraphenyl phosphonium halide, methyl triphenyl phosphonium halide, ethyl triphenyl phosphonium halide and butyl triphenyl phosphonium halide; the hydrogen bond donor is selected from one or more of urea, citric acid, succinic acid, propionic acid, acetic acid, ethylene glycol, propylene glycol, glycerol, xylitol, glucose, levulinic acid, tributyl phosphate, dimethylformamide, morpholine, oxalic acid and lactic acid;
the eutectic solvent Y comprises a hydrogen bond acceptor, a hydrogen bond donor and a Lewis acid salt; the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1 to 0.1 to 1, and the mass of the Lewis acid salt is 0.1 to 20 percent of the total mass of the eutectic solvent Y; the hydrogen bond acceptor is selected from one or more of tetraethyl ammonium halide, tetrabutyl ammonium halide, choline chloride, betaine, methyl triethyl ammonium halide, tetraphenyl phosphonium halide, methyl triphenyl phosphonium halide, ethyl triphenyl phosphonium halide and butyl triphenyl phosphonium halide; the hydrogen bond donor is selected from one or more of urea, citric acid, succinic acid, propionic acid, acetic acid, ethylene glycol, propylene glycol, glycerol, xylitol, glucose, levulinic acid, tributyl phosphate, dimethylformamide, morpholine, oxalic acid and lactic acid; the Lewis acid salt is selected from SnCl 2 , SnCl 4 , ZnCl 2 , GeCl 2 , InCl 3 , GaCl 3 , FeCl 2 , FeCl 3 , LaCl 3 , CuCl 2 , DyCl 3 , CrCl 3 , CrCl 2 , La(OTf) 3 And YbCl 3 One or more of (a);
the solvent S is selected from one of water, methanol, ethyl acetate and butyl acetate.
2. The system for separating oil products by eutectic solvent according to claim 1, characterized by comprising a eutectic solvent regenerator E and a eutectic solvent regenerator F;
an outlet of the polycyclic aromatic hydrocarbon separation tower D is connected with an inlet of the eutectic solvent regeneration tower E, and an outlet of the eutectic solvent regeneration tower E is connected with an inlet of the monocyclic aromatic hydrocarbon separation tower C; an outlet of the eutectic solvent regeneration tower E is connected with an inlet of the polycyclic aromatic hydrocarbon separation tower D;
an outlet of the aromatic hydrocarbon separation tower B is connected with an inlet of the eutectic solvent regeneration tower F;
an outlet of the eutectic solvent regeneration tower F is connected with an inlet of the non-aromatic hydrocarbon removing tower A;
the material flow of the eutectic solvent X and the solvent S flows out of the aromatic hydrocarbon separation tower B, enters a eutectic solvent regeneration tower F for flash evaporation, the solvent S is extracted, meanwhile, the regenerated eutectic solvent X is obtained, and the regenerated eutectic solvent X returns to the non-aromatic hydrocarbon removal tower A for recycling;
and the mixture flow of the eutectic solvent Y and the solvent S enters the eutectic solvent regeneration tower E, after flash evaporation, the extracted solvent S returns to the polycyclic aromatic hydrocarbon separation tower D for use, and the regenerated eutectic solvent Y returns to the monocyclic aromatic hydrocarbon separation tower C for recycling.
3. The system for separating oil products by eutectic solvent according to claim 1 or 2, characterized in that:
the oil product is selected from one or more of heavy gasoline, light diesel oil, catalytic diesel oil, heavy diesel oil, coker gasoline and coker diesel oil; the non-aromatic hydrocarbon in the oil product is one or more of C1-C20 straight chain, branched chain alkane and cyclane.
4. The system for separating oil products by eutectic solvent according to claim 1 or 2, wherein:
in the eutectic solvent X, the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1.
5. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent X, the hydrogen bond acceptor is selected from one or more of tetrabutyl ammonium halide, methyltriethyl ammonium halide, tetraphenyl phosphonium halide, methyltriphenyl phosphonium halide, ethyltriphenyl phosphonium halide and butyltriphenyl phosphonium halide.
6. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent X, the hydrogen bond donor is selected from one of succinic acid, levulinic acid, tributyl phosphate, dimethylformamide, lactic acid and propionic acid.
7. The system for separating oil products by eutectic solvent according to claim 1 or 2, characterized in that:
in the eutectic solvent Y, the molar ratio of the hydrogen bond acceptor to the hydrogen bond donor is 1:0.5 to 1.
8. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent Y, the mass of the Lewis acid salt is 0.1-8% of the total mass of the eutectic solvent Y.
9. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent Y, the hydrogen bond acceptor is selected from one or more of tetrabutyl ammonium halide, methyltriethyl ammonium halide, tetraphenyl phosphonium halide, methyltriphenylphosphonium halide, ethyltriphenylphosphonium halide and butyltriphenylphosphonium halide.
10. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent Y, the hydrogen bond donor is selected from one of succinic acid, levulinic acid, tributyl phosphate, dimethylformamide, lactic acid and propionic acid.
11. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
in the eutectic solvent Y, the Lewis acid salt is selected from SnCl 2 , SnCl 4 ，LaCl 3 , ZnCl 2 、CrCl 3 , CrCl 2 , GaCl 3 One or more of (a).
12. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
the preparation method of the eutectic solvent X comprises the following steps:
and mixing the hydrogen bond acceptor and the hydrogen bond donor at 20-180 ℃.
13. The system for separating oil products by eutectic solvent according to claim 12, characterized in that:
the preparation method of the eutectic solvent X comprises the following steps:
and mixing the hydrogen bond acceptor and the hydrogen bond donor at 20-120 ℃.
14. The system for separating oil products by eutectic solvent according to claim 1, characterized in that:
the preparation method of the eutectic solvent Y may include the steps of:
and mixing the hydrogen bond acceptor, the hydrogen bond donor and the Lewis acid salt at the temperature of 20-180 ℃.
15. The system for separating oil products by eutectic solvent according to claim 14, wherein:
the preparation method of the eutectic solvent Y may include the steps of:
and mixing the hydrogen bond acceptor, the hydrogen bond donor and the Lewis acid salt at the temperature of 20-120 ℃.
16. A method of eutectic solvent separation of oil products according to any one of claims 1 to 15, characterized by comprising the steps of:
1) Respectively introducing an oil product and a eutectic solvent X into the non-aromatic hydrocarbon removing tower A, carrying out liquid-liquid extraction on the oil product and the eutectic solvent X in the non-aromatic hydrocarbon removing tower A, extracting non-aromatic hydrocarbon, and allowing a mixture flow of the residual mixed aromatic hydrocarbon and the eutectic solvent X to enter the aromatic hydrocarbon separation tower B;
2) In the aromatic hydrocarbon separation tower B, the mixed material flow of the mixed aromatic hydrocarbon and the eutectic solvent X is contacted with a solvent S in the tower, and the mixed aromatic hydrocarbon material flow formed after extraction enters the monocyclic aromatic hydrocarbon separation tower C; the rest mixed material flow of the eutectic solvent X and the solvent S flows out of the aromatic separation tower B;
3) In the monocyclic aromatic hydrocarbon separation tower C, the mixed aromatic hydrocarbon material flow is contacted with a eutectic solvent Y to finish the liquid-liquid extraction process, the formed monocyclic aromatic hydrocarbon material flow is extracted, and the rest of the mixed material flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon enters the polycyclic aromatic hydrocarbon separation tower D;
4) After entering the polycyclic aromatic hydrocarbon separation tower D, the mixed material flow of the eutectic solvent Y and the polycyclic aromatic hydrocarbon contacts with a solvent S to form the polycyclic aromatic hydrocarbon and is extracted; and the rest mixture flow of the eutectic solvent Y and the solvent S flows out of the polycyclic aromatic hydrocarbon separation tower D.
17. The method for oil separation by eutectic solvent according to claim 16, characterized by comprising the steps of:
the mixture flow of the eutectic solvent X and the solvent S flowing out of the aromatic hydrocarbon separation tower B enters a eutectic solvent regeneration tower F for flash evaporation to extract the solvent S; simultaneously, the regenerated eutectic solvent X is obtained and returns to the non-aromatic hydrocarbon removing tower A for recycling;
and the mixture flow of the eutectic solvent Y and the solvent S enters a eutectic solvent regeneration tower E and is subjected to flash evaporation to form the solvent S which returns to the polycyclic aromatic hydrocarbon separation tower D for use, and the formed eutectic solvent Y returns to the monocyclic aromatic hydrocarbon separation tower C for recycling.
18. The method for oil separation by eutectic solvent according to claim 17, characterized in that:
and injecting a solvent S into the aromatic hydrocarbon separation tower B and the eutectic solvent regeneration tower E, wherein the injection volume of the solvent S is 0.2 to 10 times of the volume of the eutectic solvent in the tower.
19. The method for oil separation by eutectic solvent according to claim 18, characterized in that:
and injecting a solvent S into the aromatic hydrocarbon separation tower B and the eutectic solvent regeneration tower E, wherein the injection volume of the solvent S is 0.5 to 5 times of the volume of the eutectic solvent in the tower.
20. The method for eutectic solvent separation of oil according to claim 17, wherein:
the tower top pressure of the non-aromatic hydrocarbon removing tower A, the aromatic hydrocarbon separation tower B, the monocyclic aromatic hydrocarbon separation tower C, the polycyclic aromatic hydrocarbon separation tower D, the eutectic solvent regeneration tower E and the eutectic solvent regeneration tower F is 20-1500 kPa.
21. The method for oil separation by eutectic solvent according to claim 20, characterized in that:
the tower top pressure of the non-aromatic hydrocarbon removing tower A, the aromatic hydrocarbon separating tower B, the monocyclic aromatic hydrocarbon separating tower C and the polycyclic aromatic hydrocarbon separating tower D is 90-800kPa, and the tower top pressure of the eutectic solvent regenerating tower E and the eutectic solvent regenerating tower F is 20-90 kPa.
22. The method for eutectic solvent separation of oil according to claim 16, wherein:
the temperature of the non-aromatic hydrocarbon removing tower A and the temperature of the monocyclic aromatic hydrocarbon separating tower C are 10 to 120 ℃;
the temperature of the aromatic hydrocarbon separation tower B and the temperature of the polycyclic aromatic hydrocarbon separation tower D are both 10-100 ℃.
23. The method for oil separation by eutectic solvent according to claim 22, characterized in that:
the temperature of the non-aromatic hydrocarbon removing tower A and the temperature of the monocyclic aromatic hydrocarbon separating tower C are 10 to 60 ℃;
the temperature of the aromatic hydrocarbon separation tower B and the polycyclic aromatic hydrocarbon separation tower D is 10 to 50 ℃.
24. The method for oil separation by eutectic solvent according to claim 17, characterized in that:
the temperature of the eutectic solvent regeneration tower E and the temperature of the eutectic solvent regeneration tower F are both 10-300 ℃.
25. The method for oil separation by eutectic solvent according to claim 24, characterized in that:
the temperature of the eutectic solvent regeneration tower E is 30-120 ℃, and the temperature of the eutectic solvent regeneration tower F is 60-150 ℃.
26. The method for oil separation by eutectic solvent according to claim 16, characterized in that:
the volume ratio of the eutectic solvent X to the oil to be extracted in the dearomatization tower A is 1/0.2 to 1/50; the volume ratio of the eutectic solvent Y to the oil to be extracted in the monocyclic aromatic separation tower C is 1/0.2-1/50.
27. The method for oil separation by eutectic solvent according to claim 26, characterized in that:
the volume ratio of the eutectic solvent X to the oil to be extracted in the dearomatization tower A is 1/0.2 to 1/10;
the volume ratio of the eutectic solvent Y to the oil to be extracted in the monocyclic aromatic separation tower C is 1/0.2-1/20.
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