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Method of producing ethyl acetate and equipment for carrying out this method

A technology of ethyl acetate, acetic acid, applied in the field of production of ethyl acetate and the equipment for implementing it, capable of solving the problems of unfavorable, high hydrodynamic resistance, corrosive environment, etc.

Inactive Publication Date: 2003-07-30
SULZER CHEMTECH AG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Of course, the rate of uncatalyzed esterification is too low to be applied industrially
Active distillation using a homogeneous catalyst feed brings the aforementioned corrosion problems and environmental disadvantages
Distillation columns filled with free particles of acidic catalysts are not suitable for industrial production due to high hydrodynamic resistance and poor separation efficiency

Method used

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  • Method of producing ethyl acetate and equipment for carrying out this method
  • Method of producing ethyl acetate and equipment for carrying out this method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0017] figure 1 A schematic representation of the apparatus of the present invention is shown. Catalytic distillation column operated continuously at atmospheric pressure 1 Divided into 3 zones. tower 1 The reaction zone is formed in the middle of 2 . in the reaction zone 2 Below is the bottom separation area 3 , in the reaction zone 2 Above is the upper separation zone 4 . Boiler 8 with tower bottom 7 connected. condenser 12 with the top of the tower 10 connected. Splitter 14 with condenser 12 connected.

[0018] reaction zone 2 The medium is packed with a catalytically active packing containing 33 g of acetic acid ion exchanger. Pouring fill is filled in the bottom separation area 3 and upper separation area 4 Medium (arc saddle packing with a diameter of 4mm). Separation zone 3 with 4 The length is 0.5m.

[0019] The production method is that the ethanol feed is passed through the pipeline 6 into the bottom separation zone 3 , acetic acid feed...

Embodiment 2

[0020] Except that acetic anhydride is used as the raw material instead of acetic acid, ethyl acetate is synthesized under the same conditions as in Example 1, and the acetic anhydride reacts with ethanol in an equimolar ratio to generate acetic acid and ethyl acetate in a prereactor. The reaction mixture is then added to the column 1 in place of acetic acid. The selected total molar ratio of ethanol to acetic anhydride was 1.52. Using a reflux ratio of 1:6, the unit delivered 0.46 mol / h of crude ethyl acetate with a purity of 91.4% by weight. Apart from ethyl acetate, the product contained only 5.2% by weight of water and 3.4% by weight of ethanol. Splitter 14 The output of the separated aqueous phase was 3.9 ml / hour. Example 3

Embodiment 3

[0021] with including a boiler with a volume of 50 liters 8 , equipped with a condenser 12 and separator 14 the tower 1 The apparatus implements the esterification of ethanol by acetic acid. catalytic distillation column 1 including reaction zone 2 , the reaction zone 2 Catalytically active packing KATAPAK  S, the packing has 1.07kg H + form of acidic ion exchangers. bottom separation zone 3 and upper separation zone 4 The directional packing (bottom separation zone) with an effective rate of 12 is filled in the medium, that is, 20 theoretical plates. Acetic acid is passed through the pipeline at an amount of 0.73kg / hour 5 into the reaction zone 2 , passing ethanol through the pipeline at an amount of 0.41kg / hour 6 Conveying into the bottom separation area 3 upper boundary of . The water produced by this reaction is removed from the separator 14 through the pipeline 15 Drain, pass the organic phase through the tube 16 reflux into tower 1 , a portion of the ...

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Abstract

The invention relates to a method of producing ethyl acetate by reaction of ethyl alcohol with acetic acid and / or acetic anhydride in presence of a solid acidic catalyst and during simultaneous distillatory separation of reaction components, in which acetic acid or acetic anhydride or their mixture and ethyl alcohol are introduced separately in molar ratio 2:1 to 1:2.5 and in a defined quantity, based on volume unit of catalyst, into the system separated into three zones, whereby, in the reaction zone, the reaction runs simultaneously with the distillatory separation of components, acetic acid feed is introduced into the reaction zone or above the zone and ethyl alcohol feed is introduced into the reaction zone or below this zone, in the upper separation zone, the volatile mixture is separated, thereafter, it is cooled to 5 to 70 DEG C and then separated to water and organic phases and this organic phase with high ethyl acetate content is drawn off and partially returned as reflux flow into this system, whereby, the ratio of the input components feed and the organic phase reflux flow is 1:1 to 1:20. A subject matter of this invention is also an equipment for carrying out this method.

Description

field of invention [0001] The present invention relates to a method for synthesizing ethyl acetate by esterification of acetic acid and ethanol or by reaction of acetic anhydride and ethanol, the method adopts catalytic distillation in the tower, during which the reaction and reaction on the catalytically active packing take place simultaneously Product separation by distillation. The invention also relates to a device for carrying out the method. Background of the invention [0002] Ethyl acetate is produced by the reaction of ethanol and acetic acid, which produces water in addition to ethyl acetate. Alternatively, ethyl acetate can be prepared by the reaction of acetic anhydride with ethanol, which produces acetic acid in addition to ethyl acetate. The generated acetic acid is further esterified by another part of ethanol. Esterification is an equilibrium reaction which is facilitated by the presence of an acid catalyst. Therefore, inorganic acids are mainly used, pre...

Claims

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Application Information

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IPC IPC(8): B01D3/00B01D3/14B01J8/02B01J10/00C07B61/00C07C67/08C07C67/54C07C69/14
CPCB01J2208/00513C07C67/08B01J2208/00274B01J8/025B01D3/009B01J2208/00283Y02P20/10C07C69/14
Inventor J·科莱纳J·莱德雷尔P·莫拉维克J·哈尼卡Q·斯梅卡D·斯卡拉
Owner SULZER CHEMTECH AG
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