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A method and device for extracting and rectifying separation of cyclohexanol and n-hexanol

A technology for extractive rectification and extractive rectification tower, which is applied in the field of extractive rectification and separation of cyclohexanol and n-hexanol, can solve the problems of high cyclohexanol content, difficulty in separating cyclohexanol and n-hexanol, and difficulty in separation, and achieves a simple process. , improve the effective utilization rate and reduce the effect of pollution

Active Publication Date: 2021-09-03
CHINA TIANCHEN ENG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Many of these impurities are isomers of cyclohexanol and cyclohexanone, or substances with similar molecular structure and polarity, making separation difficult
[0004] The cyclohexanol content in the waste oil produced by the cyclohexanone plant is relatively high. At present, rectification methods are often used to re-separate and recover this part of cyclohexanol. However, because it contains n-hexanol as an impurity, cyclohexanol and n-hexanol belong to a mixture with a near boiling point ( The boiling point of cyclohexanol is 160.8°C, and the boiling point of n-hexanol is 157°C), and the polarities of the two are similar, so it is difficult to separate high-purity cyclohexanol and n-hexanol products by ordinary distillation

Method used

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  • A method and device for extracting and rectifying separation of cyclohexanol and n-hexanol

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0035] Extractive distillation separation process of cyclohexanol and n-hexanol, such as figure 1 shown. The extractive distillation column 1 has 35 theoretical plates. Use glycerol as the extractant, add from the fourth theoretical plate (the number of plates is from top to bottom), the addition amount is 5000kg / hr, cyclohexanol and n-hexanol are added from the 12th plate in the middle of the tower, the total flow rate is 5000kg / hr, wherein the mass fraction of cyclohexanol is 88wt%. The operating pressure of the extractive distillation tower is 5kPaA, the top reflux ratio is 2.0, the top temperature is 83.1°C, the bottom temperature is 101.3°C, and the n-hexanol product with a mass fraction of 99.6wt% is obtained at the top of the tower.

[0036] The mixture of cyclohexanol and glycerol in the tower kettle is sent to the solvent recovery tower 2, the operating pressure at the top of the tower is 5kPaA, the reflux ratio at the top of the tower is 1.0, the temperature at th...

Embodiment 2

[0038] Extractive distillation separation process of cyclohexanol and n-hexanol, such as figure 1 shown. Extractive distillation column, 1 has 35 theoretical plates. Use glycerol as the extractant, add from the 4th theoretical plate (the number of plates is from top to bottom), the addition amount is 7000kg / hr, cyclohexanol and n-hexanol are added from the 12th plate in the middle of the tower, the total flow rate is 5000kg / hr, wherein the mass fraction of cyclohexanol is 85wt%. The operating pressure of the extractive distillation tower is 5kPaA, the top reflux ratio is 1.0, the top temperature is 83.1°C, the bottom temperature is 105.6°C, and the n-hexanol product with a mass fraction of 99.8wt% is obtained at the top of the tower.

[0039] The mixture of cyclohexanol and glycerol in the tower kettle is sent to the solvent recovery tower 2, the operating pressure at the top of the tower is 5kPaA, the reflux ratio at the top of the tower is 1.0, the temperature at the top ...

Embodiment 3

[0041] Extractive distillation separation process of cyclohexanol and n-hexanol, such as figure 1 shown. The extractive distillation column 1 has 35 theoretical plates. Use glycerol as the extractant, add from the fourth theoretical plate (the number of plates is from top to bottom), the addition amount is 5000kg / hr, cyclohexanol and n-hexanol are added from the 12th plate in the middle of the tower, the total flow rate is 5000kg / hr, wherein the mass fraction of cyclohexanol is 82wt%. The operating pressure of the extractive distillation tower is 5kPaA, the top reflux ratio is 1.0, the temperature at the top of the tower is 83.1°C, and the temperature at the bottom of the tower is 101.1°C. The n-hexanol product with a mass fraction of 99.1wt% is obtained at the top of the tower.

[0042] The mixture of cyclohexanol and glycerol in the tower kettle is sent to the solvent recovery tower 2, the operating pressure at the top of the tower is 5kPaA, the reflux ratio at the top of...

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Abstract

The invention provides a method and device for separating cyclohexanol and n-hexanol by extracting and rectifying. The process of extracting and rectifying adopts a double-tower process, which is composed of an extracting and rectifying tower and a solvent recovery tower. Distillation can separate and obtain n-hexanol products with a mass concentration of ≥99.0wt% and cyclohexanol products with a mass concentration of ≥99.5wt%. Not only can the effective utilization rate of cyclohexanol be improved, but also waste oil discharge can be reduced, and can be used in industrial production.

Description

technical field [0001] The invention belongs to the technical field of chemical industry, and in particular relates to a method and a device for extracting and rectifying separating cyclohexanol and n-hexanol. Background technique [0002] Cyclohexanol is a widely used industrial raw material. It is often used as a solvent for resins, paints, ethyl cellulose, rubber, etc., and is also used as a cleaning agent, rubber reinforcement, etc. Cyclohexanol is the main raw material for the preparation of adipic acid and cyclohexanone, and its production methods mainly include phenol hydrogenation, cyclohexane oxidation and cyclohexene hydration. Cyclohexanol is dehydrogenated under the action of a catalyst to generate product cyclohexanone, which is the main raw material for producing caprolactam. [0003] In the preparation process of cyclohexanol and cyclohexanone, various side reactions will occur, resulting in various impurities in the crude alcohol and ketone. When cyclohexano...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C29/84C07C31/125C07C35/08
CPCC07C29/84C07C31/125C07C35/08
Inventor 李广忠柴永峰李发源李林李岩刘新伟高朝阳
Owner CHINA TIANCHEN ENG
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