CN1326923A - Method for continuously producing butyl acetate - Google Patents
Method for continuously producing butyl acetate Download PDFInfo
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- CN1326923A CN1326923A CN 00107970 CN00107970A CN1326923A CN 1326923 A CN1326923 A CN 1326923A CN 00107970 CN00107970 CN 00107970 CN 00107970 A CN00107970 A CN 00107970A CN 1326923 A CN1326923 A CN 1326923A
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Abstract
The continuous butyl acetate producing process includes the heated esterification reaction of glacial acetic acid and butyl alcohol in certain ratio in a normal pressure esterifying tower, rectification inside a rectifying tower and cooling in a cooling tower. The esterification temperature is 100-110 deg.c and water content in the esterifying tower is controlled in 5-15 %; the temperatuer in the rectifying tower is controlled in 135-150 deg.c and its pressure in 0.01-0.06 MPa; and the acidity of the coarse ester in the top of the esterifying tower is controlled in 0.1%. The production process has high stability, low cost, low power consumption, and is one continuous and sealed process with no product volatilization and less environmental pollution.
Description
The invention relates to a method for producing butyl acetate, in particular to a method for continuously producing butyl acetate.
The existing butyl acetate production method is mainly based on batch production, has multiple production processes, complex production process, high production cost, long product exposure time, large volatilization amount and low recovery rate of a rectification product in the production process, also needs to consume a large amount of sodium carbonate, and is difficult to realize large-scale production.
The invention aims to overcome the defects in the prior art and provides the method for continuously producing the butyl acetate by using the sulfuric acid as the catalyst, which has the advantages of simple production process, less working procedures and low production cost.
The invention is realized by adding glacial acetic acid and butanol into a normal pressure esterification tower according to a proportion, heating by using sulfuric acid as a catalyst to perform esterification reaction, then rectifying in a rectifying tower, and cooling by a cooler, wherein the esterification reaction temperature is 100-110 ℃, the acidity of the esterification tower is controlled at 30-40%, the moisture of the esterification tower is controlled at 5-15%, the temperature of the top of the rectifying tower is controlled at 100-110 ℃, the temperature in the rectifying tower is controlled at 135-150 ℃, the internal pressure of the rectifying tower is controlled at 0.04-0.06 Mpa, the acidity of crude ester at the top of the esterification tower is controlled at 0.1%, the ester alcohol water generated by the rectifying tower and the esterification tower is treated by a recovery device and then is returned to the esterification tower, the water is discharged into a recovery pool to be recycled, and the adding proportion of the glacial acetic acid and the butanol is as follows: 1.05: 1.
The aim of the invention can also be achieved by the following technical measures that the middle part of the rectifying tower is provided with an annular groove, and the cooler is composed of stainless steel coil pipes.
Compared with the prior art, the invention has the following advantages:
1. the production process has strong operation stability;
2. production automation can be conveniently realized;
3. the production cost is low, and the power consumption is low;
4. the production process is simple, and the production procedures are few;
5. the production process is closed and continuous, so that the volatilization of products is avoided;
6. the environmental pollution is small;
description of the drawings
The attached drawing is a process flow chart of the invention
The invention is described in detail with reference to the following embodiments, according to the method of the invention, glacial acetic acid and butanol are added into an atmospheric esterification tower according to a certain proportion, sulfuric acid is used as a catalyst, heating is carried out for esterification, then the mixture enters a rectifying tower for rectification, and the mixture is cooled by a cooler, wherein the esterification temperature is 100-110 ℃, the acidity of the esterification tower is controlled to be 30-40%, the moisture of the esterification tower is controlled to be 5-15%, the temperature of the top of the rectifying tower is controlled to be 100-110 ℃, the temperature of the inside of the rectifying tower is controlled to be 135-150 ℃, the internal pressure of the rectifying tower is controlled to be 0.04-0.06 Mpa, the acidity of crude ester at the top of the esterification tower is controlled to be 0.1%, ester alcohol water generated by the rectifying tower and the esterification tower is treated by a recovery device, then the ester alcohol is returned to the esterification tower.
The reaction equation is:
the technological process is shown in the attached drawing of the specification, and the working principle of the invention is that because the conversion rate is only 67.7 percent when the esterification reaction is reversible reaction and reaches the equilibrium, the reaction equilibrium condition is destroyed to ensure that the reaction is continuously carried out towards the positive direction, therefore, the acetic acid and the butanol are continuously esterified to generate the butyl acetate and the water along with the esterification reaction, the acetic acid and the butyl ester are continuously supplemented into the reaction system to increase the concentration of reactants, and the butyl acetate and the water generated by the reaction are continuously discharged out of the reaction system to ensure that the reaction equilibrium state established in the reaction process is destroyed to ensure that the reaction is continuously carried out towards the direction of generating the butyl acetate. Meanwhile, the esterification reaction of the glacial acetic acid and the butanol is weak endothermic reaction, the reaction temperature is improved, the reaction equilibrium state is not obviously influenced, but the reaction speed is favorably accelerated, the reaction temperature is generally controlled to be 100-110 ℃, the influence of the catalyst on the reaction speed is obvious, the esterification reaction of the glacial acetic acid and the butanol takes fifteen years if the reaction reaches the equilibrium state at normal temperature, the sulfuric acid is selected as the catalystin the invention, and the method is economical, wide in source, not easy to volatilize, good in catalytic effect and capable of realizing the purpose of continuously producing the butyl acetate. In the process of continuously producing butyl acetate, the water content of esterification tower is strictly controlled, it can directly affect esterification effect, at the same time it can affect the acidity of crude ester on the top of esterification tower, so that in the invention the water content of esterification tower is controlled at 5-15% to ensure that the esterification effect and acidity of esterification tower are below 0.1%, the esterified crude butyl acetate can be fed into rectification tower to make rectification, the temperature of rectification tower top is controlled at 100 deg.C-110 deg.C, the temperature of rectification tower interior is controlled at 135 deg.C-150 deg.C, and the internal pressure of rectification tower is controlled at 0.04-0.06 MPa, after the ester alcohol water produced by rectification tower and esterification tower is treated by recovery device, the ester alcohol can be returned into esterification tower, and the water can be fed into recovery pool to make recovery and reuse, and the circular tank placed in the middle portion of rectification tower and liquid phase extraction position can effectively raise yield and quality of extracted butyl acetate, and the rectified butyl acetate can be cooled by means of cooler formed from stainless steel coiled pipe so as to obtain the invented butyl And (5) ester finished product. The production process has the advantages of strong operation stability, convenient realization of production automation, low production cost, low power consumption, simple production process, few production procedures, closed and continuous production process, avoidance of product volatilization and low environmental pollution, and is an ideal production method of butyl acetate.
Claims (3)
1. A method for continuously producing butyl acetate comprises the steps of adding glacial acetic acid and butanol into a normal pressure esterification tower according to a proportion, heating by taking sulfuric acid as a catalyst for esterification reaction, then rectifying in a rectifying tower, cooling by a cooler, returning ester alcohol to the esterification tower after ester alcohol water generated by the rectifying tower and the esterification tower is treated by a recovery device, and discharging the water into a recovery pool for recycling, and is characterized in that:
a. the esterification reaction temperature is 100-110 ℃;
b. the acidity of the esterification tower is controlled between 30 and 40 percent;
c. the water content of the esterification tower is controlled to be 5-15%;
d. the temperature of the top of the rectifying tower is controlled to be between 100 and 110 ℃;
e. controlling the temperature in the rectifying tower to be 135-150 ℃;
f. the pressure in the rectifying tower is controlled to be 0.04-0.06 MPa;
g. the acidity of the crude ester at the top of the esterification tower is controlled to be less than or equal to 0.1 percent;
h. the adding proportion of the glacial acetic acid and the butanol is as follows: 1.05: 1
2. The process for the continuous production of butyl acetate according to claim 1, characterized in that: the middle part of the rectifying tower is provided with an annular groove.
3. The process for the continuous production of butyl acetate according to claim 1, characterized in that: the cooler is composed of stainless steel coil pipes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00107970A CN1090609C (en) | 2000-06-02 | 2000-06-02 | Method for continuously producing butyl acetate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN00107970A CN1090609C (en) | 2000-06-02 | 2000-06-02 | Method for continuously producing butyl acetate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1326923A true CN1326923A (en) | 2001-12-19 |
| CN1090609C CN1090609C (en) | 2002-09-11 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN00107970A Expired - Fee Related CN1090609C (en) | 2000-06-02 | 2000-06-02 | Method for continuously producing butyl acetate |
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| Country | Link |
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| CN (1) | CN1090609C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100395226C (en) * | 2006-03-20 | 2008-06-18 | 无锡百川化工股份有限公司 | Method for mass producing butyl acetate by reactive distillation method and using sulfuric acid as catalyst |
| CN100412051C (en) * | 2006-02-28 | 2008-08-20 | 华南理工大学 | Heat pump rectifying prodn. process and plant for n-butyl acetate |
| CN102690197A (en) * | 2012-05-29 | 2012-09-26 | 江门谦信化工发展有限公司 | Method for preparing acetic acid mixed butyl ester by continuous reaction and rectification |
| CN103641735A (en) * | 2013-08-29 | 2014-03-19 | 蚌埠丰原医药科技发展有限公司 | Co-production method for paracetamol and butyl acetate |
| CN109942357A (en) * | 2019-04-16 | 2019-06-28 | 营创三征(营口)精细化工有限公司 | A kind of low-boiling point alcohol continuous esterification rectification process |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1156717A (en) * | 1996-11-26 | 1997-08-13 | 厦门大学 | Process for producing n-butyl acetate |
| CN1085653C (en) * | 1997-11-25 | 2002-05-29 | 河南省科学院化学研究所 | Continuous butyl acetate producing process |
-
2000
- 2000-06-02 CN CN00107970A patent/CN1090609C/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100412051C (en) * | 2006-02-28 | 2008-08-20 | 华南理工大学 | Heat pump rectifying prodn. process and plant for n-butyl acetate |
| CN100395226C (en) * | 2006-03-20 | 2008-06-18 | 无锡百川化工股份有限公司 | Method for mass producing butyl acetate by reactive distillation method and using sulfuric acid as catalyst |
| CN102690197A (en) * | 2012-05-29 | 2012-09-26 | 江门谦信化工发展有限公司 | Method for preparing acetic acid mixed butyl ester by continuous reaction and rectification |
| CN103641735A (en) * | 2013-08-29 | 2014-03-19 | 蚌埠丰原医药科技发展有限公司 | Co-production method for paracetamol and butyl acetate |
| CN103641735B (en) * | 2013-08-29 | 2016-01-06 | 蚌埠丰原医药科技发展有限公司 | The co-production of Paracetamol and butylacetate |
| CN109942357A (en) * | 2019-04-16 | 2019-06-28 | 营创三征(营口)精细化工有限公司 | A kind of low-boiling point alcohol continuous esterification rectification process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1090609C (en) | 2002-09-11 |
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