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Extractant recovery method and system of technology for preparing adiponitrile trough hydrocyanating allyl acetonitrile

An extraction agent and hydrocyanation technology, applied in organic chemistry, carboxylic acid nitrile purification/separation, etc., to achieve the effect of optimizing heat exchange network, reducing production cost, and realizing effective utilization of energy

Inactive Publication Date: 2016-04-13
CHINA TIANCHEN ENG +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

At present, my country's adiponitrile mainly relies on imports. With the rapid development of my country's nylon 66 industry in recent years, the demand for adiponitrile has gradually increased. However, as an important raw material for producing nylon 66 salt intermediate hexamethylenediamine, domestic enterprises have no Production capacity is completely dependent on imports

Method used

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  • Extractant recovery method and system of technology for preparing adiponitrile trough hydrocyanating allyl acetonitrile

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0023] The raffinate A32746kg / h of the adiponitrile extraction process is preheated to 40°C through the third-effect evaporation tower top heat exchanger 8 and enters the first-effect evaporation tower 1. In terms of mass percentage, the raffinate A contains 70% Extractant, 20% catalyst and 10% auxiliary agent. The pressure of the first effect evaporation tower 1 is 200kPaG, and the extraction agent vapor output from the bottom of the first effect evaporation tower 1 enters the second effect evaporation tower 2, the temperature is 130°C, and the pressure is reduced by 70kPa for further decompression evaporation, and then evaporates from the second effect The unevaporated liquid output from the bottom of the tower 2 enters the three-effect evaporation tower 3, the temperature is 115°C, and the pressure is further reduced by 80kPa. Finally, the catalyst and auxiliary agent B are output from the bottom of the three-effect evaporation tower 3, and the extraction agent steam output...

Embodiment 2

[0026] The raffinate A37746kg / h of the adiponitrile extraction process is preheated to 80°C through the third-effect evaporation tower top heat exchanger 8 and enters the first-effect evaporation tower 1. In terms of mass percentage, the raffinate A contains 80% Extractant, 15% catalyst and 5% additives. The pressure of the first-effect evaporation tower 1 is 20kPaG, and the extraction agent vapor output from the bottom of the first-effect evaporation tower 1 enters the second-effect evaporation tower 2, the temperature is 130°C, and the pressure is reduced by 40kPa for further decompression evaporation, and then evaporates from the second effect The unevaporated liquid output from the bottom of the tower 2 enters the three-effect evaporation tower 3, the temperature is 115°C, and the pressure is further reduced by 40kPa. Finally, the catalyst and auxiliary agent B are output from the bottom of the three-effect evaporation tower 3, and the extraction agent steam output from th...

Embodiment 3

[0029] The raffinate A38746kg / h of the adiponitrile extraction process is preheated to 60°C through the top heat exchanger 8 of the third effect evaporation tower and enters the first effect evaporation tower 1. In terms of mass percentage, the raffinate A contains 75% Extractant, 18% catalyst and 7% additives. The pressure of the first-effect evaporation tower 1 is 160kPaG, and the extraction agent vapor output from the bottom of the first-effect evaporation tower 1 enters the second-effect evaporation tower 2, the temperature is 130°C, and the pressure is reduced by 120kPa for further reduced-pressure evaporation, and then evaporated from the second effect The unevaporated liquid output from the bottom of the tower 2 enters the three-effect evaporation tower 3, the temperature is 115°C, and the pressure is further reduced by 40kPa. Finally, the catalyst and auxiliary agent B are output from the bottom of the three-effect evaporation tower 3, and the extraction agent steam ou...

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Abstract

A triple effect evaporation method is used to realize recycling of an extractant; a triple effect evaporation heat exchange network is optimized to realize effective utilization of energy; and triple effect evaporation is carried out to realize complete separation of the extractant, a heavy component catalyst and an assistant, and the heavy component catalyst and the assistant obtained from the bottom of a triple effect evaporation tower do not contain the extractant, and can completely return to a preorder reactor in order to realize recycling. The method reduces integral energy consumption in the extractant recovery process, so the production cost of a technology for preparing adiponitrile trough hydrocyanating allyl acetonitrile is reduced; and the triple effect evaporation method aiming at the specifically composed extractant allows the extractant, the catalyst and the assistant to be completely separated and recycled.

Description

technical field [0001] The invention belongs to the technical field of chemical production, and in particular relates to an extractant recovery process and system for the process of preparing adiponitrile by hydrocyanation of pentenenitrile. Background technique [0002] Adiponitrile (ADN) is a colorless and transparent oily liquid, which is mainly used to reduce hexamethylenediamine, which is neutralized with adipic acid to produce nylon 66 salt, which is the most important product of adiponitrile so far. industrial use. Adiponitrile can also be used in rocket fuel, electroplating industry, washing additives and insecticides. At present, my country's adiponitrile mainly relies on imports. With the rapid development of my country's nylon 66 industry in recent years, the demand for adiponitrile has gradually increased. However, as an important raw material for producing nylon 66 salt intermediate hexamethylenediamine, domestic enterprises have no Production capacity is compl...

Claims

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Application Information

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IPC IPC(8): C07C255/04C07C253/34
CPCC07C253/34C07C255/04
Inventor 刘晶闫伟王聪赵敏伟梁军湘李荣杨克俭赵斌赵丽丽兰杰郭启迪张红柳屈阁许景洋谢蕊霍瑜姝
Owner CHINA TIANCHEN ENG
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