CN102718652B - System for refining ethyl acetate and application thereof - Google Patents
System for refining ethyl acetate and application thereof Download PDFInfo
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- CN102718652B CN102718652B CN201210186515.6A CN201210186515A CN102718652B CN 102718652 B CN102718652 B CN 102718652B CN 201210186515 A CN201210186515 A CN 201210186515A CN 102718652 B CN102718652 B CN 102718652B
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Abstract
The invention provides a system for refining ethyl acetate, which comprises an esterification tower (2) for esterification reaction and a dehydrating tower (1) connected with the esterification tower through a pipeline. The system also comprises an alcohol ester recovery compound tower, a first separation device, a second separation device, a wastewater recovery device, the pipeline and a first reboiler, wherein the alcohol ester recovery compound tower is vertically, integrally and jointly formed by an alcohol ester separation tower (3A) and an ethanol concentration tower (3B). The system has the beneficial effects that a wastewater recovery tower in a traditional process is designed into an alcohol ester separation composite tower, the dehydrating tower and the alcohol ester separation composite tower are subjected to heat coupling, a heat source of the system is fully utilized, and the energy consumption is reduced; and a segregation process is adopted, low-boiling point impurities in ethyl ester are maximally segregated, and while the quality of finished products is improved, the reflux ratio of the dehydrating tower is correspondingly reduced, and the energy consumption is reduced.
Description
Technical field
The invention belongs to organic compound preparation field, be specifically related to a kind of system and application thereof of purified carboxylic acid ester.
Background technology
Acetic acid ethyl ester is that turnout is larger, a kind of important Organic Chemicals that purposes is wider, it is most widely used fatty acid ester, can be used for manufacturing second phthalein amine, second phthalein acetic acid vinegar, Sulcatone etc., in spices, medicine, paint, printing-ink and foodstuffs industry, be widely used.The main production method of China is under the catalysis of the vitriol oil at present, and acetic acid and ethanol synthesis are refined and obtained through depickling, dehydration.The reaction of producing ethyl acetate is as shown in the formula (1):
Because ethanol and acetic acidreaction are reversible, therefore to obtain acetic acid ethyl ester product, need constantly one of reaction product is taken away, reaction just can be proceeded.At present production process be esterification overhead vapours through condenser condenses and cooling after enter phase splitter layering, ester from layering is drawn mutually a part and is back in esterification column, reaction product water and unreacted ethanol are taken away with azeotropic form, to guarantee carrying out continuously of esterification; Another part ester enters the interior separating-purifying of dehydration tower mutually to reach the specification of quality of ethyl acetate finished product.
Because reaction production water, ethyl ester, ethanol can form respectively ternary, binary azeotrope; And energy partial miscibility, to the refining difficulty of bringing of ethyl acetate.Be in particular in: because the water content difference of ester phase after the water content of azeotrope and phase-splitting is little, the band outlet capacity of the ester that makes to reflux is poor; Simultaneously, because esterification is reversible reaction, in the excessive technique of acetic acid, ethanol complete reaction can not be fallen, and the polarity of ethanol is between water and ethyl ester, and dissolve each other with water and ethyl ester respectively, due to the existence of ethanol, increased the mutual solubility of water and ethyl ester, further reduced band outlet capacity; Various reasons has caused the reflux ratio of esterification column and dehydration tower large, has increased energy consumption level.
Summary of the invention
For the deficiencies in the prior art part, the object of the invention is to propose a kind of system of purified acetic acid ethyl ester.
Another object of the present invention is the method proposing with system purified acetic acid ethyl ester of the present invention.
The technical scheme that realizes above-mentioned purpose of the present invention is:
A kind of system of purified acetic acid ethyl ester, comprise and carry out the esterification column of esterification and by pipeline, be connected the dehydration tower of esterification column, this system also comprises that alcohol ester knockout tower and the common alcohol ester forming of the upper and lower one of ethanol upgrading tower reclaim combination tower, the first and second tripping devices, waste water reclaiming device and the first reboiler;
Described esterification column top is provided with phase splitter, and phase splitter has the outlet of water and ester phase.Described dehydration tower is provided with liquid inlet, product outlet, vapour outlet and steam-in, the ester of esterification column exports mutually with dehydration tower and is connected, described alcohol ester knockout tower is provided with vapour outlet and liquid inlet, liquid exit, dehydration tower vapour outlet is connected with alcohol ester knockout tower liquid inlet by the first tripping device, and the water outlet of described esterification column phase splitter is also connected with alcohol ester knockout tower liquid inlet;
The vapour outlet of described alcohol ester knockout tower connects the second tripping device;
Described ethanol upgrading tower is provided with vapour outlet, ethanol entrance and wastewater outlet, the liquid exit of described alcohol ester knockout tower is connected with ethanol upgrading tower by pipeline, the vapour outlet of described ethanol upgrading tower is connected with the first reboiler by pipeline, described the first reboiler is connected with esterification column with the ethanol entrance of ethanol upgrading tower respectively by pipeline, and the wastewater outlet of described ethanol upgrading tower is connected with waste water reclaiming device.
Wherein, described tripping device comprises partial condenser, water cooler and the phase splitter connecting successively by pipeline; Described phase splitter comprises that water outlet exports mutually with ester, and the water outlet of phase splitter connects the liquid inlet of alcohol ester knockout tower, and the ester of phase splitter exports mutually with dehydration tower and is connected; The number of described partial condenser is one or more, is preferably two.
Wherein, described waste water reclaiming device comprises flash tank and the second reboiler connecting successively by pipeline, and described the second reboiler is connected with dehydration tower steam-in by pipeline.
Wherein, also comprise preheater, between described esterification column and dehydration tower, by pipeline, connect preheater, the ester of described alcohol ester knockout tower phase splitter exports mutually also and is connected with preheater by pipeline with dehydration tower.
The method of the system purified acetic acid ethyl ester of the purified acetic acid ethyl ester that a kind of the present invention of use proposes, comprise step: the mixture of the ethyl acetate, alcohol and water of esterification column output is through phase-splitting, water enters alcohol ester knockout tower, ester enters dehydration tower mutually, the steam of the output of dehydration column overhead is after the first tripping device separation, isolated ester is back to dehydration tower mutually, and water enters alcohol ester knockout tower;
It is separated that the steam that alcohol ester knockout tower produces enters the second tripping device, isolated water enters alcohol ester knockout tower, alcohol ester knockout tower overhead extraction enters dehydration tower containing the ethyl acetate of 1-3% ethanol through separation, the solution containing ethanol that discharge alcohol ester knockout tower bottom enters ethanol upgrading tower, ethanol upgrading tower overhead distillate partial reflux, part extraction de-esterifying tower continues to participate in esterification; Meanwhile, the second tripping device produces thick methyl esters and discharges outside system.
Wherein, the isolated ester of described the first tripping device is back to dehydration tower mutually, and reflux ratio is 2-5: 1, and ethyl acetate finished product is from the product outlet extraction of dehydration tower bottom.
Wherein, the tower reactor temperature of described alcohol ester knockout tower is 90-95 degree, and the reflux ratio of described ethanol upgrading tower overhead distillate is 2-4: 1.
Wherein, the waste water that described ethanol upgrading tower tower reactor is discharged produces secondary steam as the thermal source of alcohol ester knockout tower through waste water reclaiming device.
Wherein, in described tripping device, also add water (extraction agent).Steam, after partial condenser, water cooler, becomes phlegma, and the quality and separated material (phlegma) mass ratio that add water are 0.5-2: 1, and water and phlegma are separated into the water of lower floor and the ester phase on upper strata in phase splitter.
Wherein, the spent hot water that described waste water reclaiming device produces and ethanol upgrading tower overhead vapours are as the heat source of dehydration tower.
The present invention has the following advantages:
1, the present invention is designed to the separated combination tower of alcohol ester by a waste water reclamation tower in traditional technology, completes respectively the dehydration concentration process of ethyl ester and the separated and ethanol of ethanol.
2, the present invention has carried out the coupling of heat by dehydration tower combination tower separated with alcohol ester, makes full use of system heat sources, has reduced energy consumption.
3, the present invention adopts fractional condensation technique, and the lower-boiling impurity in ethyl ester is separated to greatest extent, and when having improved the quality of finished product, also the corresponding reflux ratio that reduces dehydration tower, has reduced energy consumption.
4, the present invention, by adding extraction agent, increases the alcohol ester separating effect of dehydration tower, has cancelled the collection of hair oil, has reduced the internal circulating load (hair oil be the mixture that contain ethanol, water and a small amount of methyl acetate that dehydration tower top obtain) of ethyl ester in system.
5, the present invention and traditional technology comparison, the energy consumption level that ethyl ester can be produced reduces by 25%; Remarkable in economical benefits.
Accompanying drawing explanation
Fig. 1 is the system flowchart of purified acetic acid ethyl ester of the present invention.
In figure, 1 is dehydration tower, and 2 is esterification column, 3A is alcohol ester knockout tower, and 3B is ethanol upgrading tower, and the upper and lower one of 3A and 3B forms alcohol ester and reclaims combination tower, 4 is the first partial condenser, and 5 is the second partial condenser, and 6 is the first water cooler, 7 is dehydration tower phase splitter, and 8 is the 3rd partial condenser, and 9 is the second water cooler, 10 is alcohol ester knockout tower phase splitter, and 11 is the 4th partial condenser, and 12 is the first reboiler, 13 is flash tank, and 14 is reboiler, and 15 is preheater.
Embodiment
Following examples are used for illustrating the present invention, but are not used for limiting the scope of the invention.
Embodiment 1: the system of purified acetic acid ethyl ester
Referring to Fig. 1.A kind of system of purified acetic acid ethyl ester, comprise and carry out the esterification column 2 of esterification and the dehydration tower 1 that is connected esterification column by pipeline, between esterification column 2 and dehydration tower 1, be also connected with preheater 15, dehydration tower 1 is provided with liquid inlet, product outlet, vapour outlet and steam-in, dehydration tower 1 vapour outlet is connected with the first partial condenser 4 by pipeline, this first partial condenser 4 includes vapour outlet and liquid exit, the liquid exit of the first partial condenser 4 is connected with dehydration tower phase splitter 7 with the first water cooler 6 successively by pipeline, the vapour outlet of the first partial condenser 4 is connected by pipeline with the second partial condenser 5, the second partial condenser 5 is connected with the alcohol ester knockout tower 3A that alcohol ester reclaims combination tower top.The first partial condenser 4, the first water cooler 6, the second partial condenser 5 and dehydration tower phase splitter 7 have formed the first tripping device.Esterification column 2 tops are provided with phase splitter, and phase splitter has the outlet of water and ester phase.The ester of esterification column 2 exports mutually with dehydration tower 1 and is connected.Described alcohol ester knockout tower 3A is provided with vapour outlet and liquid inlet, liquid exit, dehydration tower 1 vapour outlet is connected with alcohol ester knockout tower 3A liquid inlet by the first tripping device, and the water outlet of described esterification column 2 phase splitters is also connected with alcohol ester knockout tower 3A liquid inlet.
Alcohol ester knockout tower 3A is provided with vapour outlet and liquid exit, and its vapour outlet connects the 3rd partial condenser 8 by pipeline.The 3rd partial condenser 8 includes vapour outlet and liquid exit, and the liquid exit of the 3rd partial condenser 8 is connected with alcohol ester knockout tower phase splitter 10 with the second water cooler 9 successively by pipeline, and the vapour outlet of the 3rd partial condenser 8 is connected with the 4th partial condenser 11.The 3rd partial condenser 8, the second water cooler 9, alcohol ester knockout tower phase splitter 10 and the 4th partial condenser 11 have formed the second tripping device.
Alcohol ester knockout tower phase splitter 10 is provided with ester and exports mutually and water outlet, and the ester of alcohol ester knockout tower phase splitter 10 exports mutually with preheater 15 and is connected by pipeline, and the water outlet of described alcohol ester knockout tower phase splitter 10 is connected by pipeline with alcohol ester knockout tower 3A; Aqueous-phase reflux is to alcohol ester knockout tower 3A.
The liquid exit of alcohol ester knockout tower 3A is connected with the ethanol upgrading tower 3B that alcohol ester reclaims combination tower bottom by pipeline, and ethanol upgrading tower 3B is malleation tower, and pressure is 0.05-0.35MPa.Ethanol upgrading tower 3B is provided with vapour outlet, ethanol entrance and wastewater outlet, its vapour outlet is connected with the first reboiler 12 by pipeline, described the first reboiler 12 is connected with esterification column 2 with the ethanol entrance of ethanol upgrading tower 3B respectively by pipeline, the wastewater outlet of described ethanol upgrading tower 3B is connected with the second reboiler 14 with flash tank 13 successively by pipeline, and the second reboiler 14 is connected with dehydration tower 1 steam-in by pipeline.
Embodiment 2: ethyl acetate refining
As shown in Figure 1.Mixture by the ethyl acetate, alcohol and water of esterification column 2 extraction, mass ratio containing ethyl acetate is 93%, refine at the middle part that enters dehydration tower 1 by pipeline through feed preheater 15 preheatings, in dehydration tower 2 tower reactors, obtains ethyl acetate finished product, and ethyl acetate content is 99.98%.Water and ethanol and low-boiling-point substance methyl acetate (57.8 degrees Celsius of boiling points) are to tower top enrichment.Overhead vapours, after pipeline enters the first partial condenser 4 condensations, enters dehydration tower phase splitter 7 after the first water cooler 6, adds water as extraction agent, and the ratio that adds water is 0.5: 1.Reach the object that reduces phase splitter ester phase alcohol content.Upper strata ester refluxes through pipeline, the first partial condenser 4 vapor phase exit temperature are controlled at 60 degrees Celsius, not condensing through the second partial condenser 5 condensations by pipeline and dehydration tower phase splitter water, esterification column phase splitter water 10 together enters the middle part that alcohol ester reclaims the epimere alcohol ester knockout tower 3A of combination tower, utilize the feature of ethyl acetate, alcohol and water ternary azeotrope, temperature by controlling this tower reactor is between 90 degrees Celsius, in tower by ethyl ester and a small amount of water and separation of ethanol, tower top is rich in the steam of ethyl ester and water after pipeline enters the 3rd partial condenser 8 condensations, after the second water cooler 9, enter alcohol ester knockout tower phase splitter 10, upper strata ester mutually part refluxes through pipeline, to maintain the normal running of this tower, another part returns to dehydration tower through pipeline, water is back to the middle part of this tower, further to reclaim the ethyl ester in water, partial condenser 8 vapor phase exit temperature are controlled at 60 degrees Celsius, and condensing extraction after partial condenser 11 condensations does not drain into outside system containing the thick methyl esters of micro-ethyl ester.
The separated tower reactor of alcohol ester is discharged faints (ethanol mass content 2%) and is entered through pipeline the hypomere ethanol upgrading tower 3B middle and lower part that alcohol ester reclaims combination tower, the ethanol that the overhead vapours of ethanol upgrading tower 3B obtains after dehydration tower the first reboiler 12 condensations, a part is through the top of pipeline backflow (reflux ratio 3: 1) this tower, a part of extraction de-esterifying tower reactor.Ethanol upgrading tower is malleation tower, pressure 0.05MPa, and tower top temperature is controlled at 95 degrees Celsius; Tower reactor adopts open steam heating, and the waste water that the concentrated tower reactor of ethanol is discharged produces secondary steam as the thermal source of alcohol ester knockout tower through flash tank 13 flash distillations.The remaining hot water of flash tank 13 enters dehydration tower the second reboiler 14 through pipeline, and as its thermal source; Waste water after heat exchange enters preheater 15 for preheated feed through pipeline, arranges outward afterwards through pipeline.
Embodiment 3: ethyl acetate refining
The method of purified acetic acid ethyl ester.Step is with embodiment 2.By the mixture of the ethyl acetate, alcohol and water of esterification column 2 extraction, containing the mass ratio of ethyl acetate, be 93%.Refine at the middle part that enters dehydration tower 1 by pipeline through feed preheater 3 preheatings, in dehydration tower 2 tower reactors, obtains ethyl acetate finished product, and ethyl acetate content is 99.8%.Dehydration column overhead steam, after pipeline enters the first partial condenser 4 condensations, enters dehydration tower phase splitter 7 after the first water cooler 6, adds water as extraction agent, and the ratio that adds water is 1: 1.Reach the object that reduces phase splitter ester phase alcohol content.Upper strata ester refluxes through pipeline, the first partial condenser 4 vapor phase exit temperature are controlled at 60 degrees Celsius, not condensing through the second partial condenser 5 condensations by pipeline and dehydration tower phase splitter water, esterification column phase splitter water 10 together enters the middle part that alcohol ester reclaims the epimere alcohol ester knockout tower 3A of combination tower, utilize the feature of ethyl acetate, alcohol and water ternary azeotrope, temperature by controlling this tower reactor is at 93 degrees Celsius, in tower by ethyl ester and a small amount of water and separation of ethanol, tower top is rich in the steam of ethyl ester and water after pipeline enters the 3rd partial condenser 8 condensations, after the second water cooler 9, enter alcohol ester knockout tower phase splitter 10, upper strata ester refluxes through pipeline, to maintain the normal running of this tower, another part returns to dehydration tower through pipeline, water is back to the middle part of this tower, further to reclaim the ethyl ester in water, partial condenser three vapor phase exit temperature are controlled at 60 degrees Celsius, and condensing extraction after partial condenser 4 11 condensations does not drain into outside system containing the thick methyl esters of micro-ethyl ester.
The separated tower reactor of alcohol ester is discharged ethanol mass content 3% and is entered through pipeline the hypomere ethanol upgrading tower 3B middle and lower part that alcohol ester reclaims combination tower, the ethanol that the overhead vapours of ethanol upgrading tower 3B obtains after dehydration tower the first reboiler 12 condensations, a part is through the reflux top (reflux ratio 2: 1) of this tower of pipeline, part extraction de-esterifying tower reactor, backflow ratio is 2: 1.Ethanol upgrading tower is malleation tower, and pressure is 0.2MPa, and tower top temperature is controlled at 98 degrees Celsius, and tower reactor adopts open steam heating.The waste water that the concentrated tower reactor of ethanol is discharged produces secondary steam as the thermal source of alcohol ester knockout tower through flash tank 13 flash distillations.The remaining hot water of flash tank 13 enters dehydration column reboiler 14 through pipeline, and as its thermal source; Waste water after heat exchange enters preheater 15 for preheated feed through pipeline, arranges outward afterwards through pipeline.
Embodiment 4: ethyl acetate refining
The method of purified acetic acid ethyl ester.Step is with embodiment 2.By the mixture of the ethyl acetate, alcohol and water of esterification column 2 extraction, containing the mass ratio of ethyl acetate, be 95%.Refine at the middle part that enters dehydration tower 1 by pipeline through feed preheater 3 preheatings, in dehydration tower 2 tower reactors, obtains ethyl acetate finished product, and ethyl acetate content is 99.99%.Dehydration column overhead steam, after pipeline enters the first partial condenser 4 condensations, enters dehydration tower phase splitter 7 after the first water cooler 6, adds water as extraction agent, and the ratio that adds water is 2: 1.Reach the object that reduces phase splitter ester phase alcohol content.Upper strata ester refluxes through pipeline, the first partial condenser 4 vapor phase exit temperature are controlled at 60 degrees Celsius, not condensing through the second partial condenser 5 condensations by pipeline and dehydration tower phase splitter water, esterification column phase splitter water 10 together enters the middle part that alcohol ester reclaims the epimere alcohol ester knockout tower 3A of combination tower, utilize the feature of ethyl acetate, alcohol and water ternary azeotrope, temperature by controlling this tower reactor is at 95 degrees Celsius, in tower by ethyl ester and a small amount of water and separation of ethanol, tower top is rich in the steam of ethyl ester and water after pipeline enters the 3rd partial condenser 8 condensations, after the second water cooler 9, enter alcohol ester knockout tower phase splitter 10, upper strata ester refluxes through pipeline, to maintain the normal running of this tower, another part returns to dehydration tower through pipeline, water is back to the middle part of this tower, further to reclaim the ethyl ester in water, partial condenser three vapor phase exit temperature are controlled at 60 degrees Celsius, and condensing extraction after partial condenser 4 11 condensations does not drain into outside system containing the thick methyl esters of micro-ethyl ester.
The solution that the separated tower reactor of alcohol ester is discharged ethanol mass content 2% enters ethanol upgrading tower 3B through pipeline, the ethanol that the overhead vapours of ethanol upgrading tower obtains after dehydration tower the first reboiler 12 condensations, a part is through the reflux top of this tower of pipeline, part extraction de-esterifying tower reactor, backflow ratio is 4: 1.Ethanol upgrading tower is malleation tower, and pressure is 0.35MPa, and tower top temperature is controlled at 100 degrees Celsius, and tower reactor adopts open steam heating.The waste water that the concentrated tower reactor of ethanol is discharged produces secondary steam as the thermal source of alcohol ester knockout tower through flash tank 13 flash distillations.The remaining hot water of flash tank 13 enters dehydration column reboiler 14 through pipeline, and as its thermal source; Waste water after heat exchange enters preheater 15 for preheated feed through pipeline, arranges outward afterwards through pipeline.
Claims (6)
1. the equipment of a purified acetic acid ethyl ester, comprise the esterification column (2) that carries out esterification and the dehydration tower (1) that is connected esterification column by pipeline, it is characterized in that, this system also comprises that alcohol ester knockout tower (3A) and the common alcohol ester forming of the upper and lower one of ethanol upgrading tower (3B) reclaim combination tower, the first and second tripping devices, waste water reclaiming device and the first reboiler;
Described esterification column (2) top is provided with phase splitter, described dehydration tower (1) is provided with liquid inlet, product outlet, vapour outlet and steam-in, the ester of esterification column (2) phase splitter exports mutually with dehydration tower (1) liquid inlet and is connected, described alcohol ester knockout tower (3A) is provided with vapour outlet and liquid inlet, liquid exit, dehydration tower (1) vapour outlet is connected with alcohol ester knockout tower (3A) liquid inlet by the first tripping device, and the water outlet of described esterification column (2) phase splitter is also connected with alcohol ester knockout tower (3A) liquid inlet;
The vapour outlet of described alcohol ester knockout tower (3A) connects the second tripping device;
Described ethanol upgrading tower (3B) is provided with vapour outlet, ethanol entrance and wastewater outlet, the liquid exit of described alcohol ester knockout tower (3A) is connected with ethanol upgrading tower (3B) by pipeline, the vapour outlet of described ethanol upgrading tower (3B) is connected with the first reboiler (12) by pipeline, described the first reboiler (12) is connected with esterification column (2) with the ethanol entrance of ethanol upgrading tower (3B) respectively by pipeline, and the wastewater outlet of described ethanol upgrading tower (3B) is connected with waste water reclaiming device;
Wherein, described waste water reclaiming device comprises flash tank (13) and the second reboiler (14) connecting successively by pipeline, and described the second reboiler (14) is connected with dehydration tower (1) steam-in by pipeline;
Use the method for described system purified acetic acid ethyl ester, comprise step: the mixture of the ethyl acetate, alcohol and water of esterification column (2) output enters dehydration tower (1), the steam of the output of dehydration tower (1) tower top is after the first tripping device separation, isolated ester is back to dehydration tower (1) mutually, and water enters alcohol ester knockout tower (3A);
It is separated that the steam that alcohol ester knockout tower (3A) produces enters the second tripping device, isolated water enters alcohol ester knockout tower (3A), alcohol ester knockout tower (3A) overhead extraction enters dehydration tower (1) containing the ethyl acetate of 1-3% ethanol through separation, the solution containing ethanol that discharge alcohol ester knockout tower (3A) bottom enters ethanol upgrading tower (3B), ethanol upgrading tower (3B) overhead distillate partial reflux, part extraction de-esterifying tower (2) continues to participate in esterification; Meanwhile, the second tripping device produces thick methyl esters and discharges outside system;
Wherein, the waste water that described ethanol upgrading tower (3B) tower reactor is discharged produces secondary steam as the thermal source of alcohol ester knockout tower (3A) through waste water reclaiming device;
Wherein, the tower reactor temperature of described alcohol ester knockout tower (3A) is 90-95 degree, and the reflux ratio of described ethanol upgrading tower (3B) overhead distillate is 2-4:1; The spent hot water that described waste water reclaiming device produces and ethanol upgrading tower (3B) overhead vapours are as the heat source of dehydration tower (1).
2. equipment as claimed in claim 1, is characterized in that, described the first and second tripping devices comprise respectively partial condenser, water cooler and the phase splitter connecting successively by pipeline; Described phase splitter comprises that water outlet exports mutually with ester, and the water outlet of phase splitter connects the liquid inlet of alcohol ester knockout tower (3A), and the ester of phase splitter exports mutually with dehydration tower (1) and is connected; The number of described partial condenser is one or more.
3. equipment as claimed in claim 2, is characterized in that, the number of described partial condenser is two.
4. the equipment as described in as arbitrary in claim 1～3, it is characterized in that, also comprise preheater (15), between described esterification column (2) and dehydration tower (1), by pipeline, connect preheater (15), the ester of described alcohol ester knockout tower phase splitter (10) exports mutually also and is connected with preheater (15) by pipeline with dehydration tower (1).
5. equipment as claimed in claim 1, is characterized in that, during purified acetic acid ethyl ester described in the isolated ester of the first tripping device be back to mutually dehydration tower (1), reflux ratio is 2-5:1.
6. equipment as claimed in claim 1, is characterized in that, also adds water in tripping device described in during purified acetic acid ethyl ester, and the quality and the separated material mass ratio that add water are 0.5-2:1.
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101412671A (en) * | 2008-11-06 | 2009-04-22 | 烟台国邦化工机械科技有限公司 | Method for separating isobutyl acetate, ethanol and water by azeotropic distillation |
| CN102030639A (en) * | 2010-11-17 | 2011-04-27 | 江门天诚溶剂制品有限公司 | New energy-saving production process of ethyl acetate |
| CN102070445A (en) * | 2011-01-13 | 2011-05-25 | 蓝仁水 | Purification method of ethyl acetate |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101412671A (en) * | 2008-11-06 | 2009-04-22 | 烟台国邦化工机械科技有限公司 | Method for separating isobutyl acetate, ethanol and water by azeotropic distillation |
| CN102030639A (en) * | 2010-11-17 | 2011-04-27 | 江门天诚溶剂制品有限公司 | New energy-saving production process of ethyl acetate |
| CN102070445A (en) * | 2011-01-13 | 2011-05-25 | 蓝仁水 | Purification method of ethyl acetate |
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Address after: 064000 No. 1, front road, Fengrun District, Hebei, Tangshan City Patentee after: Soluble Polytron Technologies Inc Address before: 064000 No. 5, front road, Fengrun District, Hebei, Tangshan City Patentee before: Tangshan Ji-Dong Solvent Co., Ltd. |
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| TR01 | Transfer of patent right |
Effective date of registration: 20171102 Address after: 063000 west side of Yang Yang Road, Qian'an Economic Development Zone, Tangshan City, Hebei Patentee after: Tangshan science and technology limited company dissolution Address before: 064000 No. 1, front road, Fengrun District, Hebei, Tangshan City Patentee before: Soluble Polytron Technologies Inc |
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| TR01 | Transfer of patent right |