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Production method for producing butyric anhydride through dividing wall reaction rectification

A technology for the production of butyric anhydride and production methods, applied in the direction of carboxylic anhydride preparation, chemical instruments and methods, carboxylate preparation, etc., can solve the problems of many by-products, large equipment investment, and low purity of butyric anhydride products, and achieve energy saving The effect of saving energy consumption and saving equipment investment

Pending Publication Date: 2022-07-29
FUQING BRANCH OF FUJIAN NORMAL UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The continuous production device is composed of a reactor, a reactive distillation tower and a refining tower. There are many by-products (about 20%) in the production process, the intermediate acetic acid butyric anhydride, large equipment investment and low purity of the butyric anhydride product (up to 96.7%), etc. shortcoming

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  • Production method for producing butyric anhydride through dividing wall reaction rectification
  • Production method for producing butyric anhydride through dividing wall reaction rectification

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0035] The partition wall reactive distillation column T1 is a packed column with a column diameter of 50mm, the column body and packing material are both 2205, the packing type is φ3×3 θ ring packing, the column height is 6.0m, and the theoretical plate number of rectifying section A is 18 , the number of theoretical plates in the reaction section B is 22, the number of theoretical plates in the stripping section C is 16, the number of theoretical plates in the rectifying section E of the auxiliary column is 38, the number of theoretical plates in the common stripping section D is 25, and the number of theoretical plates in the auxiliary column D is 25. The cross-sectional area ratio to the main tower is 0.4.

[0036] The n-butyric acid is fed from the upper feed pipe PL3 of the next-wall reactive distillation column T1 at a flow rate of 8.0g / min, wherein the flow rate of fresh n-butyric acid is 5.3g / min, and the flow rate of circulating n-butyric acid at the top of the auxili...

Embodiment 2

[0039] The partition wall reactive distillation column T1 is a packed column with a column diameter of 50mm, the column body and packing material are both 2205, the packing type is φ3×3 θ ring packing, the column height is 6.0m, and the theoretical plate number of rectifying section A is 18 , the number of theoretical plates in the reaction section B is 22, the number of theoretical plates in the stripping section C is 16, the number of theoretical plates in the rectifying section E of the auxiliary column is 38, the number of theoretical plates in the common stripping section D is 25, and the number of theoretical plates in the auxiliary column D is 25. The cross-sectional area ratio to the main tower is 0.4.

[0040] The n-butyric acid is fed from the upper feed pipe PL3 of the next-wall reactive distillation column T1 at a flow rate of 10.0g / min, wherein the flow rate of fresh n-butyric acid is 4.0g / min, and the flow rate of circulating n-butyric acid at the top of the auxil...

Embodiment 3

[0043] The partition wall reactive distillation column T1 is a packed column with a column diameter of 50mm, the column body and packing material are both 2205, the packing type is φ3×3 θ ring packing, the column height is 6.0m, and the theoretical plate number of rectifying section A is 18 , the number of theoretical plates in the reaction section B is 22, the number of theoretical plates in the stripping section C is 16, the number of theoretical plates in the rectifying section E of the auxiliary column is 38, the number of theoretical plates in the common stripping section D is 25, and the number of theoretical plates in the auxiliary column D is 25. The cross-sectional area ratio to the main tower is 0.4.

[0044] The n-butyric acid is fed from the upper feed pipe PL3 of the next-wall reactive distillation column T1 at a flow rate of 10.0g / min, wherein the flow rate of fresh n-butyric acid is 4.0g / min, and the flow rate of circulating n-butyric acid at the top of the auxil...

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Abstract

The invention relates to a production method for producing butyric anhydride through dividing wall reaction rectification, which comprises the following steps of: feeding a raw material n-butyric acid from an upper feeding hole of a main tower of a dividing wall reaction rectification tower, and feeding a raw material acetic anhydride from a lower feeding hole of the main tower of the dividing wall reaction rectification tower; the raw materials n-butyric acid and acetic anhydride are subjected to acylation reaction in the middle of the main tower of the partition reaction rectifying tower and vapor-liquid mass transfer; condensing mixed steam of n-butyric acid and a small amount of acetic acid-butyric anhydride obtained at the top of the auxiliary tower of the dividing wall reaction rectifying tower through a condenser, and reacting at a feeding hole in the main tower of the dividing wall reaction rectifying tower; the butyric anhydride product is discharged from the tower kettle of the dividing wall reaction rectifying tower. According to the invention, the acylation reaction and the light component removal of the product are integrated into the same tower, and the equipment has the advantages of high conversion rate, high selectivity, low energy consumption, low equipment investment and the like.

Description

technical field [0001] The invention relates to the field of chemical production, in particular to a production method for producing butyric anhydride by reactive distillation of a partition wall. Background technique [0002] Butyric anhydride is an important organic compound, colorless liquid at room temperature, CAS number 106-31-0. Butyric anhydride is widely used in the production of cellulose acetate butyrate, as well as in the preparation of butyrate, spices, and gallbladder contrast agents. At present, butyric anhydride mainly adopts a batch production process, using n-butyric acid and acetic anhydride as raw materials to undergo an acylation reaction in the reactor. When the reaction reaches a certain conversion rate, acetic acid, acetic anhydride, Butyric acid, and finally the butyric anhydride product is distilled. Due to the disadvantages of slow reaction speed, low conversion rate, long production cycle, etc., butyric anhydride product quality is low and yield...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C51/56C07C51/573C07C53/124
CPCC07C51/56C07C51/573C07C53/124Y02P20/10
Inventor 杨金杯林漪高梦婷黄颖陈锦溢余美琼王兆宇张明文程锦添陈玉成
Owner FUQING BRANCH OF FUJIAN NORMAL UNIV
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