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Ethyl acetate synthetic process and apparatus thereof

A technology for ethyl acetate and acetic acid, which is applied to the synthesis process of ethyl acetate and the field of devices thereof, can solve the problems of high energy consumption and equipment investment, low thermodynamic efficiency, unfavorable economic benefits and the like, and achieves reduction of energy consumption and equipment investment cost. , the effect of improving the reaction conversion rate and simplifying the distillation process

Inactive Publication Date: 2009-02-04
CHINA UNIV OF PETROLEUM (EAST CHINA)
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] However, the above-mentioned reactive distillation technology still has certain defects: the top of the reactive distillation tower is close to the mixture of ethyl acetate, ethanol and water ternary azeotrope, and a series of follow-up rectification towers and extraction towers are required to be further separated to obtain high Pure ethyl acetate product, and there will be back-mixing of intermediate components in the conventional multi-component rectification process, and the thermodynamic efficiency is low
This leads to high energy consumption and equipment investment, which is not conducive to improving economic benefits

Method used

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  • Ethyl acetate synthetic process and apparatus thereof
  • Ethyl acetate synthetic process and apparatus thereof
  • Ethyl acetate synthetic process and apparatus thereof

Examples

Experimental program
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Effect test

example 1

[0018] Example 1: The reactive distillation dividing wall tower is a packed tower with a tower diameter of 1600mm and a height of 18000mm. The packing heights of areas (1) to (4) are 2500m, 2500m, 5500m, and 3500m respectively. The rectifying section (2) and the side stripping Section (4) has a cross-sectional area ratio of 3.4:1. The operating pressure is 1 atm, and the operating temperature of the overhead condenser and phase separator is 40°C. The reaction section (3) and the lower part of the tower kettle (5) are equipped with a catalyst, the catalyst is Purolite CT179 acidic cation exchange resin, and the temperature of the catalyst bed is 105-115°C. The volumetric space velocity of the acetic acid feed is 0.77h -1 , the molar ratio of ethanol feed to acetic acid feed was 1.04:1. The ratio of the mass flow rate of the liquid phase flowing into the rectifying section (2) from the top of the bulkhead to the mass flow rate of the liquid phase flowing into the side strippin...

example 2

[0021] Example 2: in the device described in example 1, each parameter is the same as example 1, but the cross-sectional area ratio of the rectifying section (2) and the side strip stripping section (4) is 2.3: 1, and flows into the rectifying section by the partition top The ratio of the mass flow rate of the liquid phase of (2) to the mass flow rate of the liquid phase flowing into the side stripping section (4) is 3:2, and the catalyst is Amberlyst 15 acidic cation exchange resin, and the temperature of the catalyst bed is 105-115°C. The flow rate and composition of each stream are shown in Table 2. The resulting acetic acid conversion was 99.99%.

[0022] Table 2 Example 2 Each logistics flow rate and composition

[0023]

example 3

[0024] Example 3: The reactive distillation dividing wall tower is a tray tower with a tower diameter of 1600 mm and a height of 24000 mm. The number of plates in the area (1) to area 4 is 10, 10, 22, and 14 respectively. The rectifying section (2) and the side stripping section (4) The cross-sectional area ratio is 1.5:1. The operating pressure is 1 atm, and the operating temperature of the overhead condenser and phase separator is 40°C. The reaction section (3) and the lower part of the tower kettle (5) are equipped with a catalyst, the catalyst is Purolite CT179 acidic cation exchange resin, and the temperature of the catalyst bed is 105-115°C. The volumetric space velocity of the acetic acid feed is 0.86h -1 , the molar ratio of ethanol feed to acetic acid feed was 1.04:1. The ratio of the mass flow rate of the liquid phase flowing into the rectifying section (2) from the top of the partition wall to the mass flow rate of the liquid phase flowing into the side stripping ...

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Abstract

The invention discloses a technological method for synthesizing ethyl acetate by using reactive rectifying bulkhead tower and a device thereof. The reactive rectifying bulkhead tower is provided with a piece of bulkhead along the vertical direction in the conventional rectifying tower, and the bottom of the right side of the bulkhead is closed. The whole tower is divided into five zones. Ethanol and acetate which are taken as raw materials are put into the tower from the top space of a tower kettle, and carry out esterification to generate ethyl acetate under the action of a catalyst of acidic cation exchange resin in the reaction section and at the lower part of the tower kettle. After the condensation and phase separation of the gas phase at the top of the tower, water phase is discharged from the system, and ester phase is driven into the top of the tower as reflux. Ethyl acetate with high purity is obtained at the bottom of the siding stripping section, and the bottom of the tower has no discharging material. The method gives a full play of the advantages of the bulkhead tower and reaction rectifying, which can cause the esterification and the product purification to be realized in the same tower and can reduce equipment investment and energy consumption effectively.

Description

technical field [0001] The present invention relates to a reactive distillation process method and its device, in particular to a novel process method and device for synthesizing ethyl acetate by using a reactive rectification dividing wall tower, which can combine the synthesis, product separation and purification of ethyl acetate Complete in one tower. Background technique [0002] Ethyl acetate is an important organic chemical raw material and organic solvent, which is widely used in perfumery, medicine, paint, food and coating industries. The production technology of ethyl acetate has experienced a history of more than 100 years, and has become increasingly mature through numerous improvements. At present, the industrial preparation methods of ethyl acetate in the world include ethanol acetate esterification method, acetaldehyde condensation method (US5,030,749), ethylene addition method (US5,478,911) and ethanol dehydrogenation method (US6,248,814). The most widely us...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C69/14C07C67/08
Inventor 孙兰义杨德连李军李青松
Owner CHINA UNIV OF PETROLEUM (EAST CHINA)
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