CN109851499A - A kind of method and device using benzene in azeotropic distillation separation vinylacetate - Google Patents

A kind of method and device using benzene in azeotropic distillation separation vinylacetate Download PDF

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CN109851499A
CN109851499A CN201811581098.9A CN201811581098A CN109851499A CN 109851499 A CN109851499 A CN 109851499A CN 201811581098 A CN201811581098 A CN 201811581098A CN 109851499 A CN109851499 A CN 109851499A
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column
tower
benzene
purification
vinylacetate
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CN109851499B (en
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张敏华
余英哲
耿中峰
陈毅飞
时锋
董秀芹
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Tianjin University
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Tianjin University
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Abstract

The present invention discloses a kind of method and device thereof using benzene in azeotropic distillation separation vinylacetate.Using methanol, water, ethyl alcohol, propyl alcohol, any one or more of mixture of butanol as entrainer, the benzene in vinylacetate is separated through azeotropic distillation;The benzene content in vinylacetate is set to drop to 1ppm or less.It realizes the device using benzene in azeotropic distillation separation vinylacetate, mainly includes azeotropy rectification column, purifying column, azeotropic distillation tower top condenser, azeotropy rectification column return tank of top of the tower, azeotropy rectification column tower top return pump, azeotropic distillation tower reboiler, azeotropic distillation tower bottoms pump, purifying column overhead condenser, purification column overhead aftercooler, purification column overhead phase separation tank, purifying column tower top return pump, purification tower reboiler, purification tower bottoms pump.This separation system structure is simple, and involved knockout tower is atmospheric tower, and operating cost is low, safety and environmental protection.This method is efficient, energy saving, can effectively remove from micro to the impurity benzene of constant rank.

Description

A kind of method and device using benzene in azeotropic distillation separation vinylacetate
Technical field
The present invention relates to chemical industry azeotropic distillation separation technology fields more particularly to a kind of utilization azeotropic distillation to separate acetic acid second The method and device of benzene in enester.
Background technique
Vinyl acetate (VAC), also referred to as vinylacetate are one of maximum Organic chemical products of yield in the world, can To be copolymerized by self-polymerization or with other monomers, polyvinyl alcohol (PVA), vinyl acetate-ethylene copolymer can be generated (EVA), polyvinyl acetate (PVAC), vinyl acetate-the polymer such as vinyl chloride copolymer (EVC).The purposes of these products is very Extensively, be typically used for the cementing agent of bonding agent, paper or fabric, paint, ink, leather processing, emulsifier, water-solubility membrane, Soil conditioner etc. is widely used in the fields such as chemical industry, weaving, light industry, papermaking, building, automobile.
Under the energy pattern of the oil-poor few more coals of gas of China, the producing vinyl acetate by acetylene method technique based on coal feedstock exists The country has huge advantage, but due to process characteristic, can contain impurity benzene in Synthesizing Vinyl Acetate from Acetylene ester product.Impurity benzene Presence will limit the subsequent product conversion of vinylacetate, the downstream product of especially influence vinyl acetate enter medical treatment, Food products market.Traditional rectifying means cannot effectively remove impurity benzene in vinyl acetate, therefore, can there is an urgent need to research and develop one kind The method for separating benzene in vinylacetate.
Patent CN 105418423A has invented the de- benzene method of purification and device of a kind of n-propyl acetate.This method will contain The n-propyl acetate product of benzene removes light component containing benzene after mixing with water in lightness-removing column, produces product from tower reactor.In this method For the boiling-point difference of the separation product n-propyl acetate and benzene that are related to away from bigger, separating difficulty is small;In addition, this method is in separation process In do not consider the later separation and regeneration of entrainer, there are biggish raw material and energy wastes;Also, the separation raw material of this method Middle benzene content is higher, cannot achieve the purpose that separate micro-benzene, the benzene content in products obtained therefrom can not be lower than 1ppm.
Patent CN 106187771A discloses a kind of using alkane as micro in extractant extraction and separation vinylacetate The method of benzene.This method is using one or more mixtures of the alkane of carbon atom number 10-18 as extractant, through extracting rectifying To separate the micro-benzene in vinylacetate.Although this method can satisfy separation requirement, but in separation process into material One or more alkane are introduced as extractant, new exogenous impurity is introduced into raw material flow stock, makes the impurity in product Component is more complicated.Meanwhile the extractant additional amount that this method requires is larger, considers the high cost of itself of extractant and larger Waste increases the production cost of product.In addition, the regenerator in the separation system is operated using rectification under vacuum, increase Equipment investment and operating cost.
It is, thus, sought for it is a kind of deviate from low cost, process is simple, removal effect is good method remove in vinyl acetate Impurity benzene.
Summary of the invention
The purpose of the present invention is overcome the deficiencies of the prior art and provide a kind of to utilize methanol, water, ethyl alcohol, propyl alcohol, butanol Separation method of one or more mixtures as entrainer as benzene in entrainer removing vinylacetate, this method can make mesh Benzene content in mark product vinylacetate drops to 1ppm or less.Another object of the present invention is to provide utilize methanol, water, second Alcohol, propyl alcohol, butanol one or more mixtures as entrainer separation vinylacetate in micro-benzene separator, this is System is suitable for the above method.
First technical solution of the invention is: a method of using benzene in azeotropic distillation separation vinylacetate, adopt It uses any one or more of mixture of methanol, water, ethyl alcohol, propyl alcohol, butanol as entrainer, separates acetic acid through azeotropic distillation Benzene in vinyl acetate.
The method specifically includes following steps:
1) containing the vinylacetate of benzene, methanol, water, ethyl alcohol, propyl alcohol or butanol one or more mixtures as altogether Boiling agent enters in tower from azeotropy rectification column lower part;
2) pass through azeotropic separation, at azeotrope a part from overhead extraction, another part adds with secondary for benzene and azeotropic dosage form The methanol that adds, water, ethyl alcohol, propyl alcohol, butanol the entrainers of one or more mixtures be uniformly mixed, then add polymerization inhibitor, It is back to tower top, the extraction of azeotropy rectification column tower reactor is free of the vinylacetate product of benzene;
3) the vinylacetate product in the step 2) without benzene enters purifying column purification;
4) pass through purifying column rectification and purification, in tower lower part side take-off vinyl acetate product;
5) purification column overhead obtains the vinyl acetate containing light component impurity, water-oil separating, aqueous-phase reflux to azeotropic distillation Column overhead, oily phase a part are back to purification column overhead, and another part is back to azeotropy rectification column lower part and follows again as charging Ring azeotropic separation;
6) purifying column tower bottoms draws battery limit (BL) impurities removal.
When present invention progress vinylacetate takes off benzene purification, benzene content is lower than in finally obtained vinylacetate product 1ppm。
One or more mixing of the methanol, water, ethyl alcohol, propyl alcohol, butanol that are added in step 2) of the present invention through tower top The mass ratio of the vinylacetate containing benzene is 1:100~1:10 in the entrainer of object composition and the step 1).
Methanol in step 1) of the present invention, water, ethyl alcohol, propyl alcohol, butanol one or more mixtures composition azeotropic The mass ratio of agent and the vinylacetate containing benzene is 1:100~1:10.
Azeotropy rectification column operating pressure is normal pressure in step 1) of the present invention, and tower top temperature is 50-65 DEG C, bottom temperature It is 68-75 DEG C.
The operating pressure of purifying column is normal pressure in step 3) of the present invention, and tower top temperature is 60-65 DEG C, and bottom temperature is 70-85℃。
The preferred hydroquinone of polymerization inhibitor in step 2) of the present invention.
Second technical solution of the invention is: realize the device using benzene in azeotropic distillation separation vinylacetate, it is main It to include azeotropy rectification column, purifying column, azeotropic distillation tower top condenser, azeotropy rectification column return tank of top of the tower, azeotropy rectification column tower Push up reflux pump, azeotropic distillation tower reboiler, azeotropic distillation tower bottoms pump, purifying column overhead condenser, purify column overhead aftercooler, Purify column overhead phase separation tank, purifying column tower top return pump, purification tower reboiler, purification tower bottoms pump;The azeotropy rectification column is set It is equipped with vinylacetate feed inlet, entrainer feed inlet and purification column overhead phase separation tank oil phase phegma feed inlet containing benzene; The azeotropy rectification column tower reactor liquid outlet pump is connected with the purifying column feed inlet;Azeotropy rectification column top gaseous phase outlet with Azeotropy rectification column overhead condenser is connected, and overhead condenser outlet is connected with azeotropic rectifying column top return tank, return tank of top of the tower Outlet line is connected with azeotropic rectifying column top return pump, and tower top return pump outlet line one the same as the acetic acid second that will contain benzene impurity The pipeline that alkene sends out battery limit (BL) is connected, and one the same as purification column overhead phase separation tank water phase outlet line, polymerization inhibitor inlet line, entrainer After the secondary adding tube congruence is closed, it is connected with azeotropic rectifying column top return entrance;Azeotropy rectification column tower reactor liquid outlet and azeotropic essence It evaporates tower bottoms pump intake to be connected, azeotropic distillation tower bottoms pump discharge is connected with purifying column feed inlet;The purifying column top gaseous phase Outlet is connected with purifying column overhead condenser entrance, the outlet of purifying column overhead condenser and purification column overhead aftercooler entrance phase Even, purification column overhead aftercooler outlet with purification column overhead phase separation tank entrance is connected, purification column overhead phase separation tank water phase export and Azeotropy rectification column overhead reflux pipeline is connected, one, purification column overhead phase separation tank oil phase outlet pipe line and azeotropy rectification column feed inlet It is connected, one is connected with purifying column overhead reflux entrance.
The purifying column tower liquid from reactor is connected with out-of-bounds pipeline;
The purifying column lower side adopts mouth and is connected with vinyl acetate product pipeline.
Purifying column overhead condenser of the present invention condenses purifying column tower top material to 40-50 DEG C, purification column overhead Material is further cooled to 25-35 DEG C by cooler.
The advantages of the present invention are as follows:
1, after the separation of azeotropy rectification column and purifying column, so that benzene content < 1PPm in last vinyl acetate product, Meet food grade materials without benzene standard;
2, entrainer uses one or more mixtures of methanol, water, ethyl alcohol, propyl alcohol, butanol as entrainer, composition letter It is single, it is low in cost, it can be recycled during the separation process;
3, the separation method does not limit benzene content in charging vinylacetate, from micro to the impurity benzene of constant rank It can effectively remove;
4, this separation system structure is simple, and involved knockout tower is atmospheric tower, and operating cost is low, safety and environmental protection.
Detailed description of the invention
Fig. 1 is the flow diagram that the present invention separates benzene device in vinylacetate using azeotropic distillation.
Wherein: 101- azeotropy rectification column, 102- purifying column, 103- azeotropy rectification column overhead condenser, 104- azeotropic distillation Column overhead return tank, 105- azeotropy rectification column tower top return pump, 106- azeotropic distillation tower reboiler, 107- azeotropic distillation tower bottoms Pump, 108- purifying column overhead condenser, 109- purify column overhead aftercooler, and 110- purifies column overhead phase separation tank, 111- purifying column Tower top return pump, 112- purify tower reboiler, and 113- purifies tower bottoms pump.
Specific embodiment
Here is that the invention will be further described in conjunction with attached drawing and by specific embodiment, and following embodiment only describes Property, it is not restrictive, this does not limit the scope of protection of the present invention.
The present invention provide it is a kind of using azeotropic distillation separation vinylacetate in benzene method, using methanol, water, ethyl alcohol, Any one or more of mixture of propyl alcohol, butanol separates the benzene in vinylacetate through azeotropic distillation as entrainer.Tool Body includes the following steps:
Firstly, vinylacetate, entrainer containing benzene enter in tower from azeotropy rectification column lower part respectively, wherein entrainer Mass ratio with the vinylacetate containing benzene is 1:100~1:10;Azeotropy rectification column operating pressure is normal pressure, and tower top temperature is 50-65 DEG C, bottom temperature is 68-75 DEG C;
Secondly, by azeotropic separation, benzene and azeotropic dosage form are at azeotrope a part from overhead extraction, and another part is the same as adding Methanol, water, ethyl alcohol, propyl alcohol, butanol one or more mixtures as entrainer, hydroquinone is mixed as polymerization inhibitor Afterwards, it is back to tower top, the extraction of azeotropy rectification column tower reactor is free of the vinylacetate product of benzene;Comprising methanol, water, ethyl alcohol, propyl alcohol, The entrainer of any one or more of mixture composition of butanol and the mass ratio of vinylacetate are 1:100~1:10;Finally Benzene content is lower than 1ppm in obtained vinylacetate product;
Again, vinylacetate product of the output without benzene to purifying column purifies, and the operating pressure of purifying column is normal pressure, tower Pushing up temperature is 60-65 DEG C, and bottom temperature is 70-85 DEG C;
4th step, by purifying column rectification and purification, in tower lower part side take-off vinyl acetate product;
5th step, purification column overhead obtain the vinyl acetate containing light component impurity, and aqueous-phase reflux is extremely after water-oil separating Azeotropic distillation column overhead, oily phase a part are back to purification column overhead, another part be back to azeotropy rectification column lower part be used as into Material recycles azeotropic separation again;
Finally, purifying column tower bottoms draws battery limit (BL) impurities removal.
The device using benzene method in azeotropic distillation separation vinylacetate is realized, as shown in Figure 1, mainly including azeotropic essence Evaporate tower 101, purifying column 102, azeotropic distillation tower top condenser 103, azeotropy rectification column return tank of top of the tower 104, azeotropy rectification column tower Push up reflux pump 105, azeotropic distillation tower reboiler 106, azeotropic distillation tower bottoms pump 107, purifying column overhead condenser 108, purification Column overhead aftercooler 109, purification column overhead phase separation tank 110, purifying column tower top return pump 111, purification tower reboiler 112, purification Tower reactor liquid pump 113;
The azeotropy rectification column 101 is provided with vinylacetate feed inlet, entrainer feed inlet and purifying column containing benzene The oily phase phegma feed inlet of tower top phase separation tank 110;
101 tower reactor liquid outlet of the azeotropy rectification column pump is connected with 102 feed inlet of purifying column;
101 tower reactor of azeotropy rectification column is provided with azeotropic distillation tower reboiler 106;
101 operating pressure of azeotropy rectification column is normal pressure, and tower top temperature is 50-65 DEG C, and bottom temperature is 68-75 DEG C;
101 top gaseous phase of the azeotropy rectification column outlet is condensed through azeotropy rectification column overhead condenser 103, and condensate liquid flows into Azeotropy rectification column return tank of top of the tower 104, the discharging of azeotropy rectification column return tank of top of the tower 104 is through azeotropy rectification column tower top return pump A part is pumped out liquid and the 110 water phase outlet line of purification column overhead phase separation tank, polymerization inhibitor charge line, entrainer by 105 Charge line is returned after converging flow to 101 tower top of azeotropy rectification column, another part discharge;
102 top gaseous phase of purifying column exports successively purified column overhead condenser 108, purification column overhead aftercooler 109 condensations, condensate liquid flow into purification column overhead phase separation tank 110 and carry out water-oil separating, the oily phase of the purification column overhead phase separation tank 110 A part is pumped out liquid by purified column overhead reflux pump 111 to be returned and flow to 102 tower top of purifying column, and another part pumps out liquid and send to institute State 101 entrance of azeotropy rectification column;
The purifying column overhead condenser 108 condenses 102 tower top material of purifying column to 40-50 DEG C, purification column overhead Material is further cooled to 25-35 DEG C by cooler 109;
The 102 tower liquid from reactor of purifying column is connected with out-of-bounds pipeline;
102 tower reactor of purifying column is provided with purification tower reboiler 112;
The operating pressure of the purifying column 102 is normal pressure, and tower top temperature is 60-65 DEG C, and bottom temperature is 70-85 DEG C;
102 lower side of purifying column adopts mouth and is connected with vinyl acetate product pipeline.
Embodiment 1:
In this example, a method of using benzene in azeotropic distillation separation vinylacetate, this method uses structure such as Routine process units shown in FIG. 1 carries out.
The vinyl acetate of impure benzene enters azeotropy rectification column (101) from lower part, inlet amount 5500kg/hr, wherein vinegar The purity of vinyl acetate is 99.96wt%, benzene content 300ppm.
Entrainer methanol, butanol, water mixture enter azeotropy rectification column (101), inlet amount 83kg/hr from lower part; Azeotropy rectification column (101) is atmospheric operation, and tower top temperature is 53.4 DEG C, and bottom temperature is 69.8 DEG C.
By azeotropic separation, benzene and azeotropic dosage form are at azeotrope a part from overhead extraction, another part and secondary addition Entrainer methanol, water, butanol mixture mixing, the entrainer inlet amount of secondary addition is 536kg/hr, is then added Hydroquinone is 10kg/hr as polymerization inhibitor, the inlet amount of hydroquinone, and mixed flow stock returns at the top of azeotropy rectification column (101). Azeotropy rectification column (101) tower reactor obtains vinyl acetate, the azeotropic agent composition without benzene, is sent into purifying column (102) and further mentions It is pure.
Purifying column (102) is atmospheric operation, and tower top temperature is 61.0 DEG C, and bottom temperature is 75.5 DEG C.Purifying column (102) top Portion obtains entrainer, a small amount of vinyl acetate, first condenses by overhead condenser (108) to 50 DEG C, cold using aftercooler (109) It coagulates to 35 DEG C, into phase separation tank (110) split-phase, water phase returns to azeotropy rectification column (101) overhead reflux, and oil phase part point returns to purification Tower (102) overhead reflux, part return to azeotropy rectification column (101) recycling charging.
Purifying column (102) bottom obtains the vinyl acetate containing impurity such as heavy constituents, the removal of impurities of discharge battery limit (BL).
Purifying column (102) lower part side take-off obtains the vinyl acetate product of high-purity.
It is handled by above-mentioned process and device, the benzene content in vinyl acetate product finally obtained is 0.83ppm, acetic acid Ethylene purity is 99.99%, reaches de- benzene purpose.
Embodiment 2:
Realize that device such as Fig. 1 of separation purpose, the vinyl acetate of impure benzene enter azeotropy rectification column (101) from lower part, Inlet amount is 42000kg/hr, and wherein the purity of vinylacetate is 98.82wt%, benzene content 1500PPm.
Entrainer water enters azeotropy rectification column (101), inlet amount 418kg/hr from lower part.Azeotropy rectification column (101) is Atmospheric operation, tower top temperature are 50.5 DEG C, and bottom temperature is 70.3 DEG C.
By azeotropic separation, benzene and azeotropic dosage form are at azeotrope a part from overhead extraction, another part and secondary addition Entrainer propyl alcohol, butanol mixture mixing, the entrainer inlet amount of secondary addition is 46kg/hr, mixed then to add pair For benzenediol as polymerization inhibitor, the inlet amount of hydroquinone is 10kg/hr, and interflow stock returns at the top of azeotropy rectification column (101).Azeotropic Rectifying column (101) tower reactor obtains vinyl acetate, the azeotropic agent composition without benzene, is sent into purifying column (102) and further purifies.
Purifying column (102) is atmospheric operation, and tower top temperature is 63.3 DEG C, and bottom temperature is 77.7 DEG C.Purifying column (102) top Portion obtains entrainer, a small amount of vinyl acetate, condenses by overhead condenser (108) to 45 DEG C, condenses using aftercooler (109) To after 30 DEG C, into phase separation tank (110) split-phase, water phase returns to azeotropy rectification column (101) overhead reflux, and oil phase part point returns to purification Tower (102) overhead reflux, part return to azeotropy rectification column (101) recycling charging.
Purifying column (102) bottom obtains the vinyl acetate containing impurity such as heavy constituents, the removal of impurities of discharge battery limit (BL).
Purifying column (102) lower part side take-off obtains the vinyl acetate product of high-purity.
It is handled by above-mentioned process and device, the benzene content in vinyl acetate product finally obtained is 0.97ppm, acetic acid Ethylene purity is 99.99%, reaches de- benzene purpose.
Embodiment 3:
Realize that device such as Fig. 1 of separation purpose, the vinyl acetate of impure benzene enter azeotropy rectification column (101) from lower part, Inlet amount is 50000kg/hr, and wherein the purity of vinylacetate is 99.07wt%, benzene content 700PPm.
Entrainer methanol, water, ethyl alcohol enter azeotropy rectification column (101), inlet amount 360kg/hr from lower part.Azeotropic distillation Tower (101) is atmospheric operation, and tower top temperature is 64.8 DEG C, and bottom temperature is 74.7 DEG C.
By azeotropic separation, benzene and azeotropic dosage form are at azeotrope a part from overhead extraction, another part and secondary addition Entrainer propyl alcohol, butanol mixture mixing, the entrainer inlet amount of secondary addition is 420kg/hr, is then added to benzene Diphenol is 10kg/hr as polymerization inhibitor, the inlet amount of hydroquinone, and mixed flow stock returns at the top of azeotropy rectification column (101).Azeotropic Rectifying column (101) tower reactor obtains vinyl acetate, the azeotropic agent composition without benzene, is sent into purifying column (102) and further purifies.
Purifying column (102) is atmospheric operation, and tower top temperature is 64.9 DEG C, and bottom temperature is 83.9 DEG C.Purifying column (102) top Portion obtains entrainer, a small amount of vinyl acetate, condenses by overhead condenser (108) to 40 DEG C, condenses using aftercooler (109) To after 25 DEG C, into phase separation tank (110) split-phase, water phase returns to azeotropy rectification column (101) overhead reflux, and oil phase part point returns to purification Tower (102) overhead reflux, part return to azeotropy rectification column (101) recycling charging.
Purifying column (102) bottom obtains the vinyl acetate containing impurity such as heavy constituents, the removal of impurities of discharge battery limit (BL).
Purifying column (102) lower part side take-off obtains the vinyl acetate product of high-purity.
It is handled by above-mentioned process and device, the benzene content in vinyl acetate product finally obtained is 0.74ppm, acetic acid Ethylene purity is 99.99%, reaches de- benzene purpose.
A kind of method and device using benzene in azeotropic distillation separation vinylacetate that the present invention is disclosed and proposed, ability Field technique personnel can be by using for reference present disclosure, and the appropriate links such as condition route that change are realized, although method and system of the invention Standby device is described by preferred embodiment, and related technical personnel can obviously not depart from the content of present invention, spirit Methods and techniques described herein route is modified or is reconfigured in range, to realize final technology of preparing.It is special Not it should be pointed out that all similar replacements and apparent to those skilled in the art, the Ta Mendou of change It is deemed to be included in spirit of that invention, range and content.

Claims (9)

1. it is a kind of using azeotropic distillation separation vinylacetate in benzene method, it is characterized in that using methanol, water, ethyl alcohol, propyl alcohol, Any one or more of mixture of butanol separates the benzene in vinylacetate through azeotropic distillation as entrainer.
2. the method as described in claim 1, it is characterized in that including the following steps:
1) containing the vinylacetate of benzene, methanol, water, ethyl alcohol, propyl alcohol or butanol one or more mixtures as entrainer Enter in tower from azeotropy rectification column lower part;
2) pass through azeotropic separation, benzene and azeotropic dosage form at azeotrope a part from overhead extraction, another part and secondary addition Methanol, water, ethyl alcohol, propyl alcohol, butanol one or more mixtures entrainer be uniformly mixed, then add polymerization inhibitor, flow back To tower top, the extraction of azeotropy rectification column tower reactor is free of the vinylacetate product of benzene;
3) the vinylacetate product in the step 2) without benzene enters purifying column purification;
4) pass through purifying column rectification and purification, in tower lower part side take-off vinyl acetate product;
5) purification column overhead obtains the vinyl acetate containing light component impurity, water-oil separating, aqueous-phase reflux to azeotropy rectification column tower Top, oily phase a part are back to purification column overhead, and another part is back to azeotropy rectification column lower part as charging, and circulation is total again Boiling separation;
6) purifying column tower bottoms draws battery limit (BL) impurities removal.
3. method according to claim 2, it is characterized in that the methanol being added in the step 2) through tower top, water, ethyl alcohol, third Alcohol, butanol one or more mixtures composition entrainer and the step 1) in the vinylacetate containing benzene mass ratio For 1:100~1:10.
4. method according to claim 2, it is characterized in that in the step 1) methanol, water, ethyl alcohol, propyl alcohol, butanol one kind Or the entrainer of a variety of mixtures composition and the mass ratio of the vinylacetate containing benzene are 1:100~1:10.
5. method according to claim 2, it is characterized in that azeotropy rectification column operating pressure is normal pressure, tower top in the step 1) Temperature is 50-65 DEG C, and bottom temperature is 68-75 DEG C.
6. method according to claim 2, it is characterized in that the operating pressure of purifying column is normal pressure, tower top temperature in the step 3) Degree is 60-65 DEG C, and bottom temperature is 70-85 DEG C.
7. method according to claim 2, it is characterized in that polymerization inhibitor is hydroquinone in the step 2).
8. the device using the method for benzene in azeotropic distillation separation vinylacetate of claim 1 is realized, it is characterized in that including Azeotropy rectification column, purifying column, azeotropic distillation tower top condenser, azeotropy rectification column return tank of top of the tower, azeotropy rectification column overhead reflux Pump, azeotropic distillation tower reboiler, azeotropic distillation tower bottoms pump, purifying column overhead condenser, purification column overhead aftercooler, purifying column Tower top phase separation tank, purifying column tower top return pump, purification tower reboiler, purification tower bottoms pump;The azeotropy rectification column, which is provided with, to be contained Vinylacetate feed inlet, entrainer feed inlet and the purification column overhead phase separation tank oil phase phegma feed inlet of benzene;It is described total Boiling tower bottom of rectifying tower liquid outlet pump is connected with the purifying column feed inlet;The azeotropy rectification column top gaseous phase outlet and azeotropic essence It evaporates column overhead condenser to be connected, overhead condenser outlet is connected with azeotropic rectifying column top return tank, return tank of top of the tower outlet Line is connected with azeotropic rectifying column top return pump, and tower top return pump outlet line one is sent out with the vinyl acetate that will contain benzene impurity The pipeline of battery limit (BL) is connected, one with purification column overhead phase separation tank water phase outlet line, polymerization inhibitor inlet line, entrainer is secondary adds After adding pipeline to converge, it is connected with azeotropic rectifying column top return entrance;Azeotropy rectification column tower reactor liquid outlet and azeotropic rectifying tower reactor Liquid pump entrance is connected, and azeotropic distillation tower bottoms pump discharge is connected with purifying column feed inlet;Purifying column top gaseous phase outlet with Purifying column overhead condenser entrance is connected, and the outlet of purifying column overhead condenser is connected with purification column overhead aftercooler entrance, purifies The outlet of column overhead aftercooler is connected with purification column overhead phase separation tank entrance, the outlet of purification column overhead phase separation tank water phase and azeotropic distillation Column overhead reflux pipeline is connected, and one, column overhead phase separation tank oil phase outlet pipe line of purification is connected with azeotropy rectification column feed inlet, and one Item is connected with purifying column overhead reflux entrance.
9. device as claimed in claim 8, it is characterized in that purifying column overhead condenser condenses purifying column tower top material to 40- 50 DEG C, purification column overhead aftercooler material is further cooled to 25-35 DEG C.
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