CN113248378A - A kind of system of extracting and rectifying methyl acetate and ethanol and using method thereof - Google Patents
A kind of system of extracting and rectifying methyl acetate and ethanol and using method thereof Download PDFInfo
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- CN113248378A CN113248378A CN202110599595.7A CN202110599595A CN113248378A CN 113248378 A CN113248378 A CN 113248378A CN 202110599595 A CN202110599595 A CN 202110599595A CN 113248378 A CN113248378 A CN 113248378A
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 120
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 title claims abstract description 58
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000000895 extractive distillation Methods 0.000 claims abstract description 71
- 238000000605 extraction Methods 0.000 claims description 28
- 239000003795 chemical substances by application Substances 0.000 claims description 22
- 239000000203 mixture Substances 0.000 claims description 22
- 238000010992 reflux Methods 0.000 claims description 16
- 239000002904 solvent Substances 0.000 claims description 14
- 239000001257 hydrogen Substances 0.000 claims description 12
- 229910052739 hydrogen Inorganic materials 0.000 claims description 12
- 238000001704 evaporation Methods 0.000 claims description 11
- 230000008020 evaporation Effects 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 8
- 239000001763 2-hydroxyethyl(trimethyl)azanium Substances 0.000 claims description 6
- 235000019743 Choline chloride Nutrition 0.000 claims description 6
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims description 6
- 239000004202 carbamide Substances 0.000 claims description 6
- 229960003178 choline chloride Drugs 0.000 claims description 6
- SGMZJAMFUVOLNK-UHFFFAOYSA-M choline chloride Chemical compound [Cl-].C[N+](C)(C)CCO SGMZJAMFUVOLNK-UHFFFAOYSA-M 0.000 claims description 6
- 230000005496 eutectics Effects 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 238000011084 recovery Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 3
- 230000005494 condensation Effects 0.000 claims description 3
- 238000000926 separation method Methods 0.000 abstract description 9
- 239000000126 substance Substances 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 150000001875 compounds Chemical group 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- KJTLSVCANCCWHF-UHFFFAOYSA-N Ruthenium Chemical compound [Ru] KJTLSVCANCCWHF-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- KYKAJFCTULSVSH-UHFFFAOYSA-N chloro(fluoro)methane Chemical compound F[C]Cl KYKAJFCTULSVSH-UHFFFAOYSA-N 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- TVZPLCNGKSPOJA-UHFFFAOYSA-N copper zinc Chemical compound [Cu].[Zn] TVZPLCNGKSPOJA-UHFFFAOYSA-N 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 125000004494 ethyl ester group Chemical group 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229920001568 phenolic resin Polymers 0.000 description 1
- 239000005011 phenolic resin Substances 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 229920001225 polyester resin Polymers 0.000 description 1
- 239000004645 polyester resin Substances 0.000 description 1
- 235000019260 propionic acid Nutrition 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229910052703 rhodium Inorganic materials 0.000 description 1
- 239000010948 rhodium Substances 0.000 description 1
- MHOVAHRLVXNVSD-UHFFFAOYSA-N rhodium atom Chemical compound [Rh] MHOVAHRLVXNVSD-UHFFFAOYSA-N 0.000 description 1
- 229910052707 ruthenium Inorganic materials 0.000 description 1
- 125000000391 vinyl group Chemical group [H]C([*])=C([H])[H] 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/58—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
- C07C29/84—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation by extractive distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C67/00—Preparation of carboxylic acid esters
- C07C67/48—Separation; Purification; Stabilisation; Use of additives
- C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
- C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
本发明提出了一种萃取精馏醋酸甲酯和乙醇的系统，包括萃取精馏塔和与其连接的第一冷凝器，述第一冷凝器连接有采出管并通过回流管与萃取精馏塔连接；萃取精馏塔通过出料管与闪蒸罐连接，出料管上设有与萃取精馏塔连通的再沸器，闪蒸罐通过经流管与所述萃取精馏塔连接，经流管上设有换热器，闪蒸罐连接有第二冷凝器。本发明通过采用单塔精馏和闪蒸罐操作实现了二元最低共沸物中组分的高纯度分离，工艺简单易行，达到了分离后的醋酸甲酯纯度高达99.0%~99.6%，乙醇纯度高达99.0%~99.6%；并且经过闪蒸罐的闪蒸，使萃取剂实现了回收再利用，降低了分离成本。The invention proposes a system for extractive rectification of methyl acetate and ethanol, comprising an extractive rectification column and a first condenser connected with it. connection; the extractive distillation tower is connected with the flash tank through a discharge pipe, the discharge pipe is provided with a reboiler connected with the extractive distillation tower, and the flash tank is connected with the extractive distillation tower through a flow pipe, A heat exchanger is provided on the flow pipe, and a second condenser is connected to the flash tank. The invention realizes the high-purity separation of the components in the binary minimum azeotrope by adopting single-column rectification and flash tank operation, the process is simple and feasible, and the purity of the separated methyl acetate is as high as 99.0%-99.6%. The purity of ethanol is as high as 99.0%~99.6%; and after flashing in the flash tank, the extractant can be recycled and reused, reducing the cost of separation.
Description
Technical Field
The invention relates to the technical field of rectification separation, in particular to a system for extracting and rectifying methyl acetate and ethanol and a using method thereof.
Background
Methyl acetate, also known as methyl acetate (C3H6O2), is a colorless, transparent, odorous liquid with a density approaching that of water, up to 0.92 kg/L. Methyl acetate is slightly soluble in water, can be mixed with most of organic solutions, has relatively high dissolving power, can effectively dissolve vinyl, epoxy, polyester and phenolic resin substances, can replace ethyl ester, acetone, chlorofluorocarbon and other substances to a certain extent, and has higher practicability.
Methyl acetate can be used for preparing various chemical products, and is a very common organic chemical product raw material. The methyl acetate can be used for preparing ethanol, and the C-O bond and the C-C bond can be adsorbed and dissociated by noble metal catalysts such as ruthenium, rhodium, palladium and the like to prepare the ethanol; or the C-O bond is selectively hydrogenated to prepare the ethanol by adopting a copper-based or copper-zinc catalyst.
The standard boiling points of methyl acetate and ethanol at atmospheric pressure are 57.1 ℃ and 78.3 ℃, the two compounds form binary minimum azeotrope when the ethanol composition is 3.1wt%, the azeotropic temperature is 57.0 ℃, and the two compounds can not be efficiently separated by using the traditional separation method.
Disclosure of Invention
Aiming at the technical problems, the invention provides a system for extracting and rectifying methyl acetate and ethanol and a using method thereof.
In order to achieve the purpose, the technical scheme of the invention is realized as follows:
a system for extracting and rectifying methyl acetate and ethanol and a using method thereof comprise an extraction rectifying tower and a flash tank, wherein an extraction outlet of the extraction rectifying tower is connected with a first condenser capable of controlling condensation reflux quantity, a discharge end of the first condenser is connected with an extraction pipe and a return pipe, and the other end of the return pipe is connected with the extraction rectifying tower; the discharge gate of extraction rectifying column pass through the discharging pipe with the feed end of flash tank is connected, be equipped with on the discharging pipe with the reboiler of extraction rectifying column intercommunication, the discharge gate of flash tank through the flow tube with the charge door of extraction rectifying column is connected, be equipped with the heat exchanger on the flow tube, the extraction end of flash tank is connected with the second condenser.
Preferably, the number of the plates of the extractive distillation column is 31-41.
Preferably, the reflux ratio of the extractive distillation tower is 0.2-4.0: 1.
The use method of the system for extracting and rectifying methyl acetate and ethanol comprises the following steps:
s1, adding a mixture of methyl acetate and ethanol into the extractive distillation tower from a feed inlet of the extractive distillation tower, adding an extracting agent into the extractive distillation tower from a feed inlet of the extractive distillation tower, allowing the extracted methyl acetate to enter the first condenser through a production outlet at the top of the extractive distillation tower for reflux and production, wherein the reflux ratio is 0.2-4.0: 1, and allowing tower kettle material flow to enter the flash tank through a discharge outlet;
s2, carrying out flash evaporation on tower bottom material flow of the extractive distillation tower in the flash evaporation tank, and collecting ethanol after the ethanol flash evaporation is condensed from the top of the flash evaporation tank through the second condenser;
and S3, conveying the residual extractant in the flash tank to the extractive distillation column from the feed inlet of the extractive distillation column after the heat exchange of the flowing pipe and the heat exchanger, and simultaneously adding fresh extractant from the feed inlet of the extractive distillation column to mix with the residual extractant.
Preferably, the operating pressure of the extraction and rectification tower is 101kPa, the tower top temperature is 56-58 ℃, and the tower bottom temperature is 101-103 ℃.
Preferably, the operating pressure of the flash tank is 10-50 kPa, and the flash temperature is 100-180 ℃.
Preferably, the position of the feed inlet on the extractive distillation tower corresponds to 8-25 trays of the extractive distillation tower; and the position of the feed inlet on the extractive distillation tower corresponds to 1-5 tower plates of the extractive distillation tower.
Preferably, the extracting agent is a hydrogen bond acceptor choline chloride and a hydrogen bond donor urea according to a molar ratio of 1: 2 to form a eutectic solvent.
Preferably, the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.7-1.2: 1.
preferably, the mass fractions of methyl acetate and ethanol in the mixture of methyl acetate and ethanol are 96.9wt% and 3.1wt%, respectively.
The invention has the beneficial effects that:
1. the high-purity separation of the components in the binary minimum azeotrope is realized by adopting single-tower rectification and flash tank operation, and the process is simple and easy to implement;
2. the purity of the separated methyl acetate is as high as 99.0-99.6%, and the purity of the ethanol is as high as 99.0-99.6%;
3. the extractant is recycled through flash evaporation of the flash tank, and the separation cost is reduced.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic structural diagram of the present invention.
In the figure: 1-an extractive distillation tower, 2-a flash tank, 3-a first condenser, 4-a return pipe, 5-an extraction pipe, 6-a discharge pipe, 7-a reboiler, 8-a flow pipe, 9-a heat exchanger and 10-a second condenser.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be obtained by a person skilled in the art without inventive effort based on the embodiments of the present invention, are within the scope of the present invention.
As shown in fig. 1, the system for extractive distillation of methyl acetate and ethanol according to the embodiment of the present invention includes an extractive distillation column 1 and a flash tank 2, wherein the upper portion of the extractive distillation column 1 is provided with a feed inlet 103, the middle portion of the extractive distillation column 1 is provided with a feed inlet 104, the top portion of the extractive distillation column is provided with a feed outlet 102, the bottom portion of the extractive distillation column 1 is provided with a discharge outlet 101, the feed outlet 102 of the extractive distillation column 1 is connected with a first condenser 3 capable of controlling condensation reflux amount, the discharge end of the first condenser 3 is connected with a feed outlet pipe 5 and a return pipe 4, and the other end of the return pipe 4 is connected with the extractive distillation column 1; the discharge port 101 of the extraction and rectification tower 1 is connected with the feed end of the flash tank 2 through a discharge pipe 6, the discharge pipe 6 is provided with a reboiler 7 communicated with the extraction and rectification tower 1, the discharge port 201 of the flash tank 2 is connected with the feed port 103 of the extraction and rectification tower 1 through a flow pipe 8, and the flow pipe 8 is provided with a heat exchanger 9; the extraction end of the flash tank 2 is connected with a second condenser 10.
Preferably, the number of the plates of the extractive distillation column 1 is 31-41.
Preferably, the reflux ratio of the extractive distillation column 1 is 0.2-4.0: 1.
The use method of the system for extracting and rectifying methyl acetate and ethanol comprises the following steps:
s1, adding a mixture of methyl acetate and ethanol into the extractive distillation tower 1 from a feed inlet 104 of the extractive distillation tower 1, adding an extracting agent into the extractive distillation tower 1 from a feed inlet 103 of the extractive distillation tower 1, allowing the extracted methyl acetate to enter the first condenser 3 through a discharge outlet 102 of the extractive distillation tower top 1 for reflux and extraction, wherein the reflux ratio is 0.2-4.0: 1, and allowing tower bottom material flow to enter the flash tank 2 through a discharge outlet 101;
s2, carrying out flash evaporation on tower bottom material flow of the extraction and rectification tower 1 in the flash evaporation tank 2, and condensing the flash-evaporated ethanol from the top of the flash evaporation tank 2 through the second condenser 10 and then extracting the ethanol;
s3, conveying the residual extracting agent in the flash tank 2 to the extractive distillation column 1 from the feed inlet 103 of the extractive distillation column 1 after passing through the flow pipe 8 and exchanging heat by the heat exchanger 9, and simultaneously adding fresh extracting agent from the feed inlet 103 of the extractive distillation column 1 to mix with the residual extracting agent.
Preferably, the operating pressure of the extractive distillation column 1 is 101kPa, the temperature at the top of the column is 56-58 ℃, and the temperature at the bottom of the column is 101-103 ℃.
Preferably, the operating pressure of the flash tank 2 is 10-50 kPa, and the flash temperature is 100-180 ℃.
Preferably, the position of the feed inlet 104 on the extractive distillation column 1 corresponds to 8-25 trays of the extractive distillation column 1; the position of the feed inlet 103 on the extractive distillation column 1 corresponds to 1-5 tower plates of the extractive distillation column 1.
Preferably, the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.7-1.2: 1.
preferably, the mass fractions of methyl acetate and ethanol in the mixture of methyl acetate and ethanol are 96.9wt% and 3.1wt%, respectively.
Example 1:
the number of the tower plates of the extraction rectifying tower 1 is 31 (the number of the tower plates is counted from top to bottom), the extracting agent is a mixture of hydrogen bond acceptor choline chloride and hydrogen bond donor urea according to the molar ratio of 1: 2 the eutectic solvent formed is added from the 3 rd plate with the flow rate of 8500 kg/h; the mixture of methyl acetate and ethanol is added from the 10 th plate, the flow rate is 10000kg/h, and the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.85: 1, the components of which are 3.1wt percent of ethanol and 96.9wt percent of methyl acetate; the extractive distillation column 1 was operated at 101kPa with a top temperature of 56 ℃ and a bottom temperature of 101 ℃ and a top reflux ratio of 2: 1.
The pressure of the flash tank 2 is 10kPa, the flash temperature is 100 ℃, the mass fraction of methyl acetate after separation is 99.6%, the mass fraction of ethanol is 99.6%, the recovery rate of the solvent is 99.99%, and the mass fraction of the solvent is 99.99%.
Example 2:
the number of the tower plates of the extraction rectifying tower 1 is 31 (the number of the tower plates is counted from top to bottom), the extracting agent is a mixture of hydrogen bond acceptor choline chloride and hydrogen bond donor urea according to the molar ratio of 1: 2 the eutectic solvent formed is added from the 5 th plate with a flow rate of 8500 kg/h; the mixture of methyl acetate and ethanol is added from the 10 th plate, the flow rate is 10000kg/h, and the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.85: 1, the components of which are 3.1wt percent of ethanol and 96.9wt percent of methyl acetate; the extractive distillation column 1 was operated at 101kPa with a top temperature of 56 ℃ and a bottom temperature of 101 ℃ and a top reflux ratio of 1: 1.
The pressure of the flash tank 2 is 30kPa, the flash temperature is 140 ℃, the mass fraction of the separated methyl acetate is 99.5%, the mass fraction of the ethanol is 99.6%, the recovery rate of the solvent is 99.99%, and the mass fraction of the solvent is 99.99%.
Example 3:
the number of the tower plates of the extraction rectifying tower 1 is 31 (the number of the tower plates is counted from top to bottom), the extracting agent is a mixture of hydrogen bond acceptor choline chloride and hydrogen bond donor urea according to the molar ratio of 1: 2 the eutectic solvent formed is added from the 3 rd plate with the flow rate of 8500 kg/h; the mixture of methyl acetate and ethanol is fed from the 20 th plate, the flow rate is 10000kg/h, and the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.85: 1, the components of which are 3.1wt percent of ethanol and 96.9wt percent of methyl acetate; the extractive distillation column 1 was operated at 101kPa with a top temperature of 57 ℃ and a bottom temperature of 102 ℃ and a top reflux ratio of 0.5: 1.
The pressure of the flash tank 2 is 40kPa, the flash temperature is 140 ℃, the mass fraction of methyl acetate after separation is 99.0%, the mass fraction of ethanol is 99.3%, the recovery rate of the solvent is 99.99%, and the mass fraction of the solvent is 99.99%.
Example 4:
the number of the tower plates of the extraction rectifying tower 1 is 31 (the number of the tower plates is counted from top to bottom), the extracting agent is a mixture of hydrogen bond acceptor choline chloride and hydrogen bond donor urea according to the molar ratio of 1: 2 the eutectic solvent formed is added from the 3 rd plate with the flow rate of 8500 kg/h; the mixture of methyl acetate and ethanol is added from the 10 th plate, the flow rate is 10000kg/h, and the feeding mass ratio of the extracting agent to the feeding liquid of the mixture of methyl acetate and ethanol is 0.85: 1, the components of which are 3.1wt percent of ethanol and 96.9wt percent of methyl acetate; the extractive distillation column 1 was operated at 101kPa with a top temperature of 58 ℃ and a bottom temperature of 103 ℃ and a top reflux ratio of 0.8: 1.
The pressure of the flash tank 2 is 20kPa, the flash temperature is 120 ℃, the mass fraction of methyl acetate after separation is 99.3%, the mass fraction of ethanol is 99.6%, the recovery rate of the solvent is 99.99%, and the mass fraction of the solvent is 99.99%.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (10)
1. The system for extracting and rectifying methyl acetate and ethanol is characterized by comprising an extraction and rectification tower (1) and a flash tank (2), wherein a recovery port (102) of the extraction and rectification tower (1) is connected with a first condenser (3) capable of controlling condensation reflux amount, a discharge end of the first condenser (3) is connected with a recovery pipe (5) and a return pipe (4), and the other end of the return pipe (4) is connected with the extraction and rectification tower (1); discharge gate (101) of extraction rectifying column (1) pass through discharging pipe (6) with the feed end of flash tank (2) is connected, be equipped with on discharging pipe (6) with reboiler (7) of extraction rectifying column (1) intercommunication, discharge gate (201) of flash tank (2) through flow tube (8) with charge door (103) of extraction rectifying column (1) are connected, be equipped with heat exchanger (9) on flow tube (8), the extraction end of flash tank (2) is connected with second condenser (10).
2. The system for the extractive distillation of methyl acetate and ethanol according to claim 1, wherein the number of the plates of the extractive distillation column (1) is 31-41.
3. The system for the extractive distillation of methyl acetate and ethanol according to claim 2, wherein the reflux ratio of the extractive distillation column (1) is 0.2-4.0: 1.
4. The use method of the system for the extractive distillation of methyl acetate and ethanol as claimed in any one of claims 1 to 3, characterized by comprising the following steps:
s1, adding a mixture of methyl acetate and ethanol into the extractive distillation tower (1) from a feed inlet (104) of the extractive distillation tower (1), adding an extracting agent into the extractive distillation tower (1) from a feed inlet (103) of the extractive distillation tower (1), allowing the extracted methyl acetate to enter the first condenser (3) through a discharge outlet (102) of the extractive distillation tower top (1) for reflux and discharge, wherein the reflux ratio is 0.2-4.0: 1, and allowing tower kettle material flow to enter the flash tank (2) through a discharge outlet (101);
s2, carrying out flash evaporation on tower bottom material flow of the extractive distillation tower (1) in the flash evaporation tank (2), and condensing the flash-evaporated ethanol from the top of the flash evaporation tank (2) through the second condenser (10) and then extracting the condensed flash-evaporated ethanol;
s3, conveying the residual extracting agent in the flash tank (2) to the extractive distillation column (1) from a feed inlet (103) of the extractive distillation column (1) after passing through the flow pipe (8) and being subjected to heat exchange by the heat exchanger (9), and simultaneously adding fresh extracting agent from the feed inlet (103) of the extractive distillation column (1) to mix with the residual extracting agent.
5. The use method of the system for the extractive distillation of methyl acetate and ethanol according to claim 4, wherein the operating pressure of the extractive distillation tower (1) is 101kPa, the tower top temperature is 56-58 ℃, and the tower bottom temperature is 101-103 ℃.
6. The use method of the system for the extractive distillation of methyl acetate and ethanol according to claim 5, wherein the operating pressure of the flash tank (2) is 10-50 kPa, and the flash temperature is 100-180 ℃.
7. The system for the extractive distillation of methyl acetate and ethanol and the use method thereof according to any one of claims 4 to 6, wherein the feed inlet (104) is positioned on the extractive distillation tower (1) and corresponds to 8 to 25 tower plates of the extractive distillation tower (1); the position of the feed inlet (103) on the extractive distillation tower (1) corresponds to 1-5 tower plates of the extractive distillation tower (1).
8. The use method of the system for the extractive distillation of methyl acetate and ethanol according to claim 7, wherein the extracting agent is a hydrogen bond acceptor choline chloride and a hydrogen bond donor urea in a molar ratio of 1: 2 to form a eutectic solvent.
9. The use method of the system for the extractive distillation of methyl acetate and ethanol according to claim 8, wherein the feed mass ratio of the extracting agent to the feed liquid of the mixture of methyl acetate and ethanol is 0.7-1.2: 1.
10. the use method of the system for the extractive distillation of methyl acetate and ethanol according to claim 9, wherein the mass fractions of methyl acetate and ethanol in the mixture of methyl acetate and ethanol are 96.9wt% and 3.1wt%, respectively.
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