Method for separating acetonitrile and triethylamine azeotropic mixture by extractive distillation

An extractive distillation and extractive distillation tower technology is applied in the field of chemical separation and purification to achieve the effects of reducing pollution, high product purity and simple separation

Active Publication Date: 2016-12-14
QINGDAO UNIV OF SCI & TECH
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0008] At present, there is no report about the separation method of acetonitrile and triethylamine azeotropic system in the literature, so it is of great pra

Method used

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  • Method for separating acetonitrile and triethylamine azeotropic mixture by extractive distillation

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0054] In the extractive distillation column equipped with 35 trays, the mixture of acetonitrile and triethylamine with a mass ratio of 8 and 2 enters from the 15th tray, and the flow rate is 1000kg / h, and the extraction agent ethylene glycol enters from the 10th tray The plate enters the tower, the flow rate is 2000kg / h, the operating pressure of the extractive distillation tower is 0.3atm, the control reflux ratio is 4, acetonitrile is extracted from the top of the tower, and triethylamine and ethylene glycol are extracted from the bottom of the tower from the 18th Each plate enters the solvent recovery tower equipped with 50 trays, the operating pressure is 0.3atm, the reflux ratio is controlled to be 4, triethylamine is extracted from the top of the tower, and the ethylene glycol extracted from the bottom of the tower is returned to the extractive distillation tower for recycling .

[0055] After separation: the purity of acetonitrile product reaches 99.90wt%; the purity o...

Embodiment 2

[0057] In the extractive distillation column equipped with 40 trays, the mixture of acetonitrile and triethylamine with a mass ratio of 7 and 3 enters from the 16th plate, and the flow rate is 1000kg / h, and the extraction agent ethylene glycol enters from the 11th plate Plate enters this tower, and flow rate is 1000kg / h, and extractive distillation column operating pressure is 0.4atm, and control reflux ratio is 5, and acetonitrile is extracted from tower top, and purity is 99.7wt%, and triethylamine and ethylene glycol are from tower still After extraction, enter the solvent recovery tower with 45 trays from the 19th plate, the operating pressure is 0.4atm, the reflux ratio is controlled at 4, triethylamine is extracted from the top of the tower, and the ethylene glycol extracted from the bottom of the tower is returned The extractive distillation column is recycled.

[0058] After separation: the purity of acetonitrile product reaches 99.92wt%; the purity of triethylamine pr...

Embodiment 3

[0060] In the extractive distillation column equipped with 45 trays, the mixture of acetonitrile and triethylamine with a mass ratio of 7 and 3 enters from the 13th tray, and the flow rate is 1000kg / h, and the extraction agent ethylene glycol enters from the 10th tray Plate enters this tower, and flow rate is 3000kg / h, and extractive distillation tower operation pressure is 0.6atm, and control reflux ratio is 4, and acetonitrile is extracted from tower top, and purity is 99.5wt%, and triethylamine and ethylene glycol are from tower still After extraction, enter the solvent recovery tower with 55 trays from the 21st plate, the operating pressure is 0.6atm, the reflux ratio is controlled at 5, triethylamine is extracted from the top of the tower, and the ethylene glycol extracted from the bottom of the tower is returned The extractive distillation column is recycled.

[0061] After separation: the purity of acetonitrile product reaches 99.84wt%; the purity of triethylamine produ...

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Abstract

The invention relates to a method for separating an acetonitrile and triethylamine azeotropic mixture by extractive distillation. An extractive distillation column and a solvent recovery tower adopt negative pressure operation; the acetonitrile and triethylamine mixture are introduced from the upper middle part of the extractive distillation column; ethylene glycol as an extractant is introduced from the upper part of the column; after the extractive distillation column, acetonitrile is extracted from the top of the extractive distillation column; the extractant and triethylamine are extracted from the bottom of the extractive distillation column and introduced from the upper middle part of the recovery tower; the triethylamine is extracted from the top of the solvent recovery tower; and the extractant ethylene glycol is extracted from the bottom of the recovery tower for recycling. The negative pressure operation adopted by the invention can reduce the heat load of the reboiler, and reduce the energy consumption for operation; the extractant ethylene glycol can significantly improve the relative volatility of acetonitrile and triethylamine; and the recovery rate is as high as 99.9%.

Description

【Technical field】 [0001] The invention belongs to the field of separation and purification of chemical industry, and relates to a method for separating acetonitrile and triethylamine azeotrope, furthermore, it relates to a method for extracting essence by using an extractive distillation tower and then a solvent recovery tower with ethylene glycol extractant. Distillation method for separating the azeotropic mixture of acetonitrile and triethylamine. 【Background technique】 [0002] Acetonitrile, also known as methyl nitrile, is a colorless, transparent liquid that is highly volatile and has a special odor similar to ether. Acetonitrile is an excellent solvent capable of dissolving a wide variety of organic, inorganic and gaseous substances. Acetonitrile can undergo typical nitrile reactions and is used to prepare many typical nitrogen-containing compounds. It is an important organic intermediate. [0003] Triethylamine is a kind of amine organic compound, it is a colorless...

Claims

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Application Information

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IPC IPC(8): C07C255/03C07C253/34C07C211/05C07C209/86
CPCC07C209/86C07C253/34C07C211/05C07C255/03
Inventor 王英龙赵婷然李敏文桂林朱兆友
Owner QINGDAO UNIV OF SCI & TECH
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