CN110041167A - A kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture - Google Patents
A kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture Download PDFInfo
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- CN110041167A CN110041167A CN201910348177.3A CN201910348177A CN110041167A CN 110041167 A CN110041167 A CN 110041167A CN 201910348177 A CN201910348177 A CN 201910348177A CN 110041167 A CN110041167 A CN 110041167A
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- extractive distillation
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- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 238000000895 extractive distillation Methods 0.000 title claims abstract description 77
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000000203 mixture Substances 0.000 title claims abstract description 30
- 238000000926 separation method Methods 0.000 title claims abstract description 21
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims abstract description 27
- 238000011084 recovery Methods 0.000 claims abstract description 22
- 235000019441 ethanol Nutrition 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 238000000605 extraction Methods 0.000 claims abstract description 12
- 239000000126 substance Substances 0.000 claims abstract description 6
- 238000010992 reflux Methods 0.000 claims description 17
- 239000002904 solvent Substances 0.000 claims description 15
- 238000010438 heat treatment Methods 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 4
- 230000005494 condensation Effects 0.000 claims description 4
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 3
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims 1
- 239000000463 material Substances 0.000 abstract description 6
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- FMYHFHVAPZDDPJ-UHFFFAOYSA-N ethanol;ethyl acetate;hydrate Chemical compound O.CCO.CCOC(C)=O FMYHFHVAPZDDPJ-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 229920006221 acetate fiber Polymers 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 2
- 230000001070 adhesive effect Effects 0.000 description 2
- 239000011248 coating agent Substances 0.000 description 2
- 238000000576 coating method Methods 0.000 description 2
- 239000000835 fiber Substances 0.000 description 2
- 239000004434 industrial solvent Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 244000099147 Ananas comosus Species 0.000 description 1
- 235000007119 Ananas comosus Nutrition 0.000 description 1
- 239000001856 Ethyl cellulose Substances 0.000 description 1
- ZZSNKZQZMQGXPY-UHFFFAOYSA-N Ethyl cellulose Chemical compound CCOCC1OC(OC)C(OCC)C(OCC)C1OC1C(O)C(O)C(OC)C(CO)O1 ZZSNKZQZMQGXPY-UHFFFAOYSA-N 0.000 description 1
- 235000016623 Fragaria vesca Nutrition 0.000 description 1
- 240000009088 Fragaria x ananassa Species 0.000 description 1
- 235000011363 Fragaria x ananassa Nutrition 0.000 description 1
- 240000008790 Musa x paradisiaca Species 0.000 description 1
- 235000018290 Musa x paradisiaca Nutrition 0.000 description 1
- VMHLLURERBWHNL-UHFFFAOYSA-M Sodium acetate Chemical compound [Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004581 coalescence Methods 0.000 description 1
- 239000003086 colorant Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000013329 compounding Methods 0.000 description 1
- 239000006071 cream Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000686 essence Substances 0.000 description 1
- 229920001249 ethyl cellulose Polymers 0.000 description 1
- 235000019325 ethyl cellulose Nutrition 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 238000011027 product recovery Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 239000005060 rubber Substances 0.000 description 1
- 238000009938 salting Methods 0.000 description 1
- 239000001632 sodium acetate Substances 0.000 description 1
- 235000017281 sodium acetate Nutrition 0.000 description 1
- 235000013599 spices Nutrition 0.000 description 1
- 229920003051 synthetic elastomer Polymers 0.000 description 1
- 239000005061 synthetic rubber Substances 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
- 235000015041 whisky Nutrition 0.000 description 1
Classifications
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Crystallography & Structural Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture and suitable for the device of this method.This method is using ethylene glycol as extractant, ethyl acetate, alcohol and water mixture initially enters first extractive distillation column and is separated, tower top obtains ethyl acetate product, materials at bottom of tower enters second extractive distillation column and is separated, overhead extraction alcohol product, the mixture of tower bottom extractant and water enters extractant recovery tower, and water is recycled after tower bottom extraction from overhead extraction, extractant.This method has many advantages, such as simple process, and the product purity of ethyl acetate and ethyl alcohol is high after separation, used ethylene glycol extractant can break simultaneously three binary azeotropic points in system and a ternary azeotropic point, be easily recycled, chemical thermal stability it is good.
Description
Technical field
Field is isolated and purified more particularly to a kind of ternary separation of extractive distillation ethyl acetate-the invention belongs to chemical industry
The method of ethanol-water mixture.
Background technique
Ethyl acetate is also known as ethyl acetate, is a kind of widely used fine chemical product, with excellent dissolubility, fastly
Stemness, it is widely used, it is a kind of important Organic Chemicals and fabulous industrial solvent, is widely used in acetate fiber, second
In the production process of base fiber, chlorinated rubber, vinyl, acetate fiber resin, synthetic rubber, coating and paint etc..It is led
Purposes is wanted to have: as industrial solvent, for coating, adhesive, ethyl cellulose, artificial leather, malthoid colorant, staple fibre etc.
In product;As adhesive, for printing the production of ink, olivet;As extractant, produced for medicine, organic acid etc.
The production of product;Main original as spice material, for the fragrance such as the fruit essences such as pineapple, banana, strawberry and whiskey, cream
Material.
Currently, widely used ethyl acetate preparation method is at a certain temperature to be esterified acetic acid and ethyl alcohol
Reaction forms ethyl acetate, alcohol and water mixture, needs to isolate and purify it after reaction.However, in ethyl acetate-
There are three binary azeotropic points and a ternary azeotropic point in ethanol-water mixture, system separating difficulty is larger.
Chinese patent CN108358754A disclose a kind of separating alcohol, ethyl acetate and aqueous mixtures process and
System, this method is by pretreater, coalescence phase-splitter and weight-removing column come separating alcohol, ethyl acetate and water.Chinese patent
CN102070445B discloses a kind of purification process of ethyl acetate, and this method uses water to carry out recycling ethyl acetate as extractant
And ethyl alcohol.It is mixed that Chinese patent CN100575332C discloses a kind of salting, compounding, extracting, rectifying separating acetic acid ethyl ester-alcohol-water
The method for closing liquid, this method isolate ethyl acetate and second by the way that 10~20% sodium acetate progress composite extraction and rectification is added
Alcohol.The problems such as there is separating technology complexity in above-mentioned separation method, not easy to operate, and product recovery rate is low, and separation purity is not high.
The present invention is by the method for ternary extracting rectifying, the characteristics of can change azeotropic mixture relative volatility using extractant
Realize the separation of ethyl acetate, ethyl alcohol and aqueous mixtures.There are three binary azeotropic points according to containing in mixture to be separated by the present invention
The characteristics of with a ternary azeotropic point, separates ethyl acetate first with an extractive distillation column, then recycles
Separation of ethanol is finally realized the recycling of extractant by two extractive distillation columns using extractant recovery tower, and the present invention has
The advantages that product purity of ethyl acetate and ethyl alcohol is high after simple process, separation, used extractant ethylene glycol can be simultaneously
Break three binary azeotropic points and a ternary azeotropic point, be easily recycled, chemical thermal stability it is good.
Summary of the invention
[technical problems to be solved]
The object of the present invention is to provide a kind of devices of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture.
It is a further object to provide use described device separating acetic acid ethyl ester-ethanol-water mixture method.
It is a further object to provide described devices in separating acetic acid ethyl ester-ethanol-water mixture purposes.
[technical solution]
The present invention is achieved through the following technical solutions.
A kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture, it is characterised in that this method is made
Device mainly includes following part:
Extractive distillation column (T1), extractive distillation column (T2), extractant recovery tower (T3), return tank (D1), return tank (D2),
Return tank (D3), condenser (C1), condenser (C2), condenser (C3), reboiler (R1), reboiler (R2), reboiler (R3),
Cooler (E);Wherein reboiler (R1), reboiler (R2), reboiler (R3) are connected to extractive distillation column (T1), extraction
Rectifying column (T2) and extractant recovery tower (T3) tower bottom, condenser (C1) and return tank (D1) are connected to extractive distillation column in turn
(T1) tower top, condenser (C2) and return tank (D2) are connected to extractive distillation column (T2) tower top, condenser (C3) and reflux in turn
Tank (D3) is connected to extractive distillation column (T3) tower top in turn, and cooler (E) is connected in extractant circulation logistics;
This method mainly comprises the steps that
(1) ethyl acetate, alcohol and water mixture initially enters extractive distillation column (T1), and from extractive distillation column (T1)
After the extractant contact that portion enters, through efficiently separating, extractive distillation column (T1) overhead vapours is through condenser (C1) condensation, return tank
(D1) after collecting, a part of logistics is flowed back at the top of extractive distillation column (T1), and another part logistics is adopted as ethyl acetate product
Out, extractive distillation column (T1) tower base stream a part enters back into extractive distillation column (T1), another portion after reboiler (R1) heating
Point logistics enters extractive distillation column (T2);
(2) after extractive distillation column (T1) tower base stream enters extractive distillation column (T2), and from the top extractive distillation column (T2)
After the extractant contact of entrance, through efficiently separating, extractive distillation column (T2) overhead vapours is through condenser (C2) condensation, return tank
(D2) after collecting, a part of logistics is flowed back at the top of extractive distillation column (T2), and another part logistics is produced as alcohol product, extraction
Extractive distillation column (T2), another part object are entered back into after taking rectifying column (T2) tower base stream a part to enter reboiler (R2) heating
Stream enters extractant recovery tower (T3);
(3) extractive distillation column (T2) tower base stream enters extractant recovery tower (T3), through efficiently separating, extractant recovery tower
(T3) for overhead vapours after condenser (C3) condensation, return tank (D3) are collected, a part of logistics flows back into extractive distillation column (T3)
Top, another part logistics are that the water of high-purity directly produces, and extractant recovery tower (T3) tower base stream a part enters boils again
It is entered back into extractant recovery tower (T3) after device (R3) heating, another part logistics produces the extractant of high-purity through cooler (E)
It is delivered to extractive distillation column (T1) after cooling and extractive distillation column (T2) is recycled.
In accordance with another preferred embodiment of the present invention, it is characterised in that the operating pressure of the extractive distillation column (T1) is
1atm absolute pressure, theoretical cam curve are 35~60 pieces, and the feed entrance point of ethyl acetate, alcohol and water mixture is the 20th~35 piece, extraction
Taking agent feed entrance point is the 3rd~7 piece, reflux ratio 0.2-0.9, and the operating pressure of extractive distillation column (T2) is 1atm absolute pressure, reason
It is 40~55 pieces by the number of plates, feed entrance point is the 20th~40 piece, and extractant feed position is the 3rd~6 piece, reflux ratio 0.4
~1.2, the operating pressure of extractant recovery tower (T3) is 0.2atm absolute pressure, and theoretical cam curve is 16~35 pieces, and feed entrance point is
8th~20 piece, reflux ratio is 0.7~1.5.
In accordance with another preferred embodiment of the present invention, it is characterised in that the extractant is ethylene glycol.
In accordance with another preferred embodiment of the present invention, it is characterised in that the extractant total amount and ethyl acetate-ethanol-
Aqueous mixtures mass ratio, i.e. solvent ratio are 1.5~5.
In accordance with another preferred embodiment of the present invention, it is characterised in that the Solvent quantity of the extractive distillation column (T1)
It is 3.5~7.3 with the ratio between the Solvent quantity of extractive distillation column (T2).
In accordance with another preferred embodiment of the present invention, it is characterised in that isolated ethyl acetate, alcohol and water mixture can
To be mixed with arbitrary proportion.
In accordance with another preferred embodiment of the present invention, it is characterised in that the purity of ethyl acetate is 99.83% after separation
~99.90% (mass fraction), the purity of ethyl alcohol are 99.83%~99.90% (mass fraction), and the purity of water is 99.90%
~99.95% (mass fraction).
[beneficial effect]
The present invention compared with prior art, mainly have it is following the utility model has the advantages that
(1) this method separating acetic acid ethyl ester-ethanol-water mixture is taken, two kinds of high purity products is obtained, solves acetic acid
Ethyl ester-alcohol-water forms three binary azeotropic points and a ternary azeotropic point is difficult to the problem of separating.
(2) this method has many advantages, such as simple process, and the product purity of ethyl acetate and ethyl alcohol is high after separation, used
Extractant ethylene glycol can break three binary azeotropic points and a ternary azeotropic point simultaneously, be easily recycled, chemical thermal stability
It is good.
Detailed description of the invention
Fig. 1 is the process flow chart of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture of the invention.
In figure, T1- extractive distillation column;T2- extractive distillation column;T3- extractant recovery tower;D1, D2, D3- return tank; C1,
C2, C3- condenser;R1, R2, R3- reboiler;E- cooler.
Specific embodiment
Below with reference to embodiment, the present invention is further illustrated, but the present invention is not limited to embodiments.
Embodiment 1:
Feed rate is 1000kg/h, in charging containing ethyl acetate 10% (mass fraction), ethyl alcohol 20% (mass fraction),
Water 70% (mass fraction).Extractive distillation column (T1) number of theoretical plate is 35 pieces, the feed position of ethyl acetate, alcohol and water mixture
It is set to the 20th piece, extractant feed position is the 3rd piece, reflux ratio 0.2, and extractive distillation column (T2) number of theoretical plate is 40 pieces, into
Material position is set to the 20th piece, and extractant feed position is the 3rd piece, reflux ratio 0.4, and extractant recovery tower (T3) number of theoretical plate is 16
Block, feed entrance point are the 8th piece, reflux ratio 0.7, and the flow of extractant ethylene glycol is 1500kg/h (solvent ratio is 1.5), extraction
The ratio between Solvent quantity and the Solvent quantity of extractive distillation column (T2) of rectifying column (T1) are 3.5, ethyl acetate after separation
Purity is 99.83% (mass fraction), and the purity of ethyl alcohol is 99.83% (mass fraction), and the purity of water is 99.90% (quality
Score).
Embodiment 2:
Feed rate is 1000kg/h, in charging containing ethyl acetate 30% (mass fraction), ethyl alcohol 30% (mass fraction),
Water 40% (mass fraction).Extractive distillation column (T1) number of theoretical plate is 60 pieces, the feed position of ethyl acetate, alcohol and water mixture
It is set to the 35th piece, extractant feed position is the 7th piece, reflux ratio 0.9, and extractive distillation column (T2) number of theoretical plate is 55 pieces, into
Material position is set to the 40th piece, and extractant feed position is the 6th piece, reflux ratio 1.2, and extractant recovery tower (T3) number of theoretical plate is 35
Block, feed entrance point are the 20th piece, reflux ratio 1.5, and the flow of extractant ethylene glycol is 5000kg/h (solvent ratio is 5), extraction
The ratio between Solvent quantity and the Solvent quantity of extractive distillation column (T2) of rectifying column (T1) are 7.3, ethyl acetate after separation
Purity is 99.90% (mass fraction), and the purity of ethyl alcohol is 99.90% (mass fraction), and the purity of water is 99.95% (quality
Score).
Embodiment 3:
Feed rate is 1000kg/h, in charging containing ethyl acetate 50% (mass fraction), ethyl alcohol 20% (mass fraction),
Water 30% (mass fraction).Extractive distillation column (T1) number of theoretical plate is 48 pieces, the feed position of ethyl acetate, alcohol and water mixture
It is set to the 27th piece, extractant feed position is the 5th piece, reflux ratio 0.5, and extractive distillation column (T2) number of theoretical plate is 50 pieces, into
Material position is set to the 30th piece, and extractant feed position is the 4th piece, reflux ratio 0.8, and extractant recovery tower (T3) number of theoretical plate is 28
Block, feed entrance point are the 15th piece, reflux ratio 1.2, and the flow of extractant ethylene glycol is 3000kg/h (solvent ratio is 3), extraction
The ratio between Solvent quantity and the Solvent quantity of extractive distillation column (T2) of rectifying column (T1) are 4.5, ethyl acetate after separation
Purity is 99.87% (mass fraction), and the purity of ethyl alcohol is 99.87% (mass fraction), and the purity of water is 99.93% (quality
Score).
Claims (7)
1. a kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture, it is characterised in that this method is used
Device mainly include following part:
Extractive distillation column (T1), extractive distillation column (T2), extractant recovery tower (T3), return tank (D1), return tank (D2), reflux
Tank (D3), condenser (C1), condenser (C2), condenser (C3), reboiler (R1), reboiler (R2), reboiler (R3), cooling
Device (E);Wherein reboiler (R1), reboiler (R2), reboiler (R3) are connected to extractive distillation column (T1), extractive distillation column
(T2) and extractant recovery tower (T3) tower bottom, condenser (C1) and return tank (D1) are connected to extractive distillation column (T1) tower in turn
Top, condenser (C2) and return tank (D2) are connected to extractive distillation column (T2) tower top, condenser (C3) and return tank (D3) in turn
It is connected to extractive distillation column (T3) tower top in turn, cooler (E) is connected in extractant circulation logistics;
This method mainly comprises the steps that
(1) ethyl acetate, alcohol and water mixture initially enters extractive distillation column (T1), with from the extractive distillation column top (T1) into
After the extractant contact entered, through efficiently separating, extractive distillation column (T1) overhead vapours is through condenser (C1) condensation, return tank (D1)
After collection, a part of logistics is flowed back at the top of extractive distillation column (T1), and another part logistics is produced as ethyl acetate product, extraction
Rectifying column (T1) tower base stream a part is taken to enter back into extractive distillation column (T1), another part logistics after reboiler (R1) heating
Into extractive distillation column (T2);
(2) after extractive distillation column (T1) tower base stream enters extractive distillation column (T2), enter with from the extractive distillation column top (T2)
Extractant contact after, through efficiently separating, extractive distillation column (T2) overhead vapours through condenser (C2) condense, return tank (D2) receive
After collection, a part of logistics is flowed back at the top of extractive distillation column (T2), and another part logistics is produced as alcohol product, extracting rectifying
Tower (T2) tower base stream a part enters back into extractive distillation column (T2) after entering reboiler (R2) heating, and another part logistics enters
Extractant recovery tower (T3);
(3) extractive distillation column (T2) tower base stream enters extractant recovery tower (T3), through efficiently separating, extractant recovery tower (T3)
After overhead vapours is condensed through condenser (C3), return tank (D3) is collected, a part of logistics is flowed back at the top of extractive distillation column (T3),
Another part logistics is that the water of high-purity directly produces, and extractant recovery tower (T3) tower base stream a part enters reboiler (R3)
It is entered back into after heating extractant recovery tower (T3), another part logistics produces the extractant of high-purity after cooler (E) is cooling
It is delivered to extractive distillation column (T1) and extractive distillation column (T2) is recycled.
2. a kind of method of ternary separation of extractive distillation ethyl acetate, alcohol and water mixture according to claim 1,
The operating pressure for being characterized in that the extractive distillation column (T1) is 1atm absolute pressure, and theoretical cam curve is 35~60 pieces, ethyl acetate-
The feed entrance point of ethanol-water mixture be the 20th~35 piece, extractant feed position be the 3rd~7 piece, reflux ratio be 0.2~
0.9, the operating pressure of extractive distillation column (T2) is 1atm absolute pressure, and theoretical cam curve is 40~55 pieces, feed entrance point is the 20th~
40 pieces, extractant feed position is the 3rd~6 piece, and reflux ratio is 0.4~1.2, and the operating pressure of extractant recovery tower (T3) is
0.2atm absolute pressure, theoretical cam curve are 16~35 pieces, and feed entrance point is the 8th~20 piece, and reflux ratio is 0.7~1.5.
3. according to the method described in claim 1, it is characterized in that the extractant is ethylene glycol.
4. according to the method described in claim 1, it is characterized in that the extractant total amount is mixed with ethyl acetate, alcohol and water
The ratio between amount of substance, i.e. solvent ratio are 1.5~5.
5. according to the method described in claim 1, it is characterized in that Solvent quantity and the extraction of the extractive distillation column (T1)
The ratio between Solvent quantity of rectifying column (T2) is 3.5~7.3.
6. according to the method described in claim 1, it is characterized in that isolated ethyl acetate, alcohol and water mixture can be to appoint
The mixing of meaning ratio.
7. according to the method described in claim 1, it is characterized in that separation after ethyl acetate purity be 99.83%~
99.90% (mass fraction), the purity of ethyl alcohol are 99.83%~99.90% (mass fraction), the purity of water is 99.90%~
99.95% (mass fraction).
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Cited By (5)
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CN112125802A (en) * | 2020-09-29 | 2020-12-25 | 中国石油大学胜利学院 | Extractive distillation separation system and method for ethyl acetate-isopropanol-water mixture |
CN114191837A (en) * | 2021-12-07 | 2022-03-18 | 大连理工大学 | Device and method for separating methanol-benzene-acetonitrile azeotrope system by extractive distillation |
CN115093326A (en) * | 2022-06-28 | 2022-09-23 | 青岛科技大学 | Method for separating ethyl acetate-ethanol-butanone mixture by extraction pressure swing distillation |
CN115340443A (en) * | 2022-08-03 | 2022-11-15 | 青岛科技大学 | Method for separating isopropanol-water-ethanol mixture by thermal coupling extractive distillation |
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