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Method for separating ethyl acetate-isopropanol by ionic liquid extractive rectification

A technology of ethyl acetate and ionic liquids, applied in extraction distillation, preparation of carboxylic acid esters, chemical instruments and methods, etc., can solve the problems of high energy consumption and large consumption, and achieve good separation effect

Inactive Publication Date: 2014-04-30
SHENYANG INSTITUTE OF CHEMICAL TECHNOLOGY
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The key technology of extractive distillation is the selection of extractant. Traditional organic solvents consume a lot of energy and consume a lot of energy.

Method used

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  • Method for separating ethyl acetate-isopropanol by ionic liquid extractive rectification

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0017] Embodiment 1: as figure 1 The extractive distillation process shown. The extractive distillation column has 20 trays, and the ionic liquid extractant enters from the third tray after being heated, with a flow rate of 90kg / h, and the mixture of ethyl acetate and isopropanol is added from the tenth tray of the tower to form ethyl acetate 45wt% , isopropanol 55 wt%, the flow rate is 90kg / h, the extractive distillation column is operated at normal pressure, the reflux ratio is 2, the output of the tower top product is 40.5kg / h, the temperature of the extractive distillation column top is 77.1°C, and the temperature of the bottom of the tower is It is 90.8 ℃, and as a result, an ethyl acetate product with a mass fraction of 99.0% can be obtained at the top of the tower.

[0018] The mixture of isopropanol and ionic liquid from the bottom product of the extractive distillation tower enters the solvent recovery flash tank, and the flash temperature is 90°C. The isopropanol pr...

Embodiment 2

[0019] Embodiment 2: as figure 1 The extractive distillation process shown. The extractive distillation column has 25 trays, and the ionic liquid extractant enters from the fifth tray after being heated, with a flow rate of 110kg / h, and the mixture of ethyl acetate and isopropanol is added from the 15th tray of the tower to form ethyl acetate 55wt% , isopropanol 45 wt%, the flow rate is 90kg / h, the extractive distillation column is operated at normal pressure, the reflux ratio is 3, the output of the tower top product is 49.5kg / h, the temperature of the extractive distillation column top is 77.1°C, and the temperature of the bottom of the tower is It is 100°C, and as a result, an ethyl acetate product with a mass fraction of 99.5% can be obtained at the top of the tower.

[0020] The mixture of isopropanol and ionic liquid in the bottom product of the extraction and rectification column enters the solvent recovery flash tank, and the flash temperature is 120°C. The isopropano...

Embodiment 3

[0021] Embodiment 3: as figure 1 The extractive distillation process shown. The extractive distillation column has 30 trays, and the ionic liquid extractant enters from the seventh tray through heating, with a flow rate of 130kg / h, and the mixture of ethyl acetate and isopropanol is added from the tenth tray of the tower to form ethyl acetate 75wt% , isopropanol 25 wt%, the flow rate is 90kg / h, the extractive distillation column is operated at normal pressure, the reflux ratio is 2, the output of the tower top product is 67.5kg / h, the temperature of the extractive distillation column top is 77.1°C, and the temperature of the bottom of the tower is It is 121 ℃, and as a result, the ethyl acetate product with a mass fraction of 99.9% can be obtained at the top of the tower.

[0022] The mixture of isopropanol and ionic liquid at the bottom of the extraction and rectification column enters the solvent recovery flash tank, and the flash temperature is 110°C. The isopropanol produ...

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Abstract

The invention discloses a method for separating ethyl acetate-isopropanol by ionic liquid extractive rectification, and relates to a chemical extraction method. In the method provided by the invention, the ionic liquid, namely the 1-ethyl-3-methylimidazole tetrafluoroborate ionic liquid, is used as extraction agent; an extractive rectification tower is operated under normal pressure, a solvent flash vaporization recycling tank is operated under reduced pressure, mass ratio of the added ionic liquid is 0.4-0.6, and reflux ratio is 1.0-4.0; the ethyl acetate-isopropanol mixture raw material is conveyed to a heat exchanger from a raw material storage tank to be treated with heat exchange, and then, is conveyed into the extractive rectification tower, and high-purity ethyl acetate without ionic liquid can be obtained at the tower top; the material discharged from the bottom of the rectification tower is a mixture of isopropanol and ionic liquid, and moreover, isopropanol and ionic liquid can be further separated from each other at 90-110 DEG C in a flash tank; the separated ionic liquid can be reused. The method provided by the invention remarkably improves the effect of extractive rectification separation on the ethyl acetate-isopropanol mixture.

Description

technical field [0001] The invention relates to a chemical extraction method, in particular to a method for separating ethyl acetate-isopropanol through ionic liquid extraction and rectification. Background technique [0002] Both ethyl acetate and isopropanol are important chemical basic raw materials. Currently, CSPC will produce a large amount of isopropanol-ethyl acetate solvent during the production of benzylamine, especially when the mass content of ethyl acetate is 74%. When the two will form an azeotrope, the most common special separation method for this azeotrope is extractive distillation. Extractive distillation is a special rectification method that adds a third component (called extractant or solvent) from the top of the tower to the raw material liquid to change the relative volatility between the original components to meet the separation requirements. It requires the extractant Its boiling point is much higher than that of each component in the raw mate...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C67/54C07C69/14C07C29/84C07C31/10B01D3/40
CPCC07C29/84C07C67/54C07C69/14C07C31/10
Inventor 张志刚黄艳红于萍张弢李文秀张翔
Owner SHENYANG INSTITUTE OF CHEMICAL TECHNOLOGY
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