Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification

A technology for the separation and recovery of butyl acetate, applied in the m-HSAD process field, can solve the problems of high energy consumption, separation and refining, etc., and achieve the effects of short process route, reduced energy consumption, and low investment

Active Publication Date: 2010-08-25
NANJING UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, the two of them generally form azeotropes under normal pressure, and it is difficult to separate and refine them by ordinary rectification methods.
In the current industrial process, butanol and butyl acetate are generally separated by azeotropic distillation, but recovery and recycling of the azeotropic agent is required, and the energy consumption is relatively high

Method used

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  • Process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0020] With butanol 0.1% (wt), butyl acetate 1% (wt), water 97.9% (wt), organic residue (or other high boiling matter) 1% (wt) flow rate is the waste water of 0.125 tons / hour, It is preheated to 45°C by heat exchanger H-01, then heated to 80°C by heat exchanger H-02, and then enters the first rectification tower T-01. The theoretical plate number of the first rectification tower T-01 is 28 block, the tower diameter is 0.3 meters, the operating pressure is normal pressure, and the tower kettle is heated by steam. The condensate of the steam at the top of the first rectification tower T-01 after heat exchange enters the phase separation tank S1, and the heavy phase refluxes. The temperature at the top of the rectification tower T-01 is 85°C, the temperature at the bottom of the tower is 100°C, and the bottom of the tower can obtain pure water and organic residues (or other high boiling substances). The light phase is extracted and enters the second rectification tower T-02. The ...

Embodiment 2

[0022] With butanol 7% (wt), butyl acetate 5% (wt), water 85% (wt), the flow of organic residue (or other high boiler) 3% (wt) is the waste water of 0.3 ton / hour through Heat exchanger H-01 is preheated to 50°C, then heated to 85°C by heat exchanger H-02, and then enters the first rectification tower T-01, the number of theoretical plates of the first rectification tower T-01 is 30 , the tower diameter is 0.6 meters, the operating pressure is normal pressure, the tower kettle is heated by steam, the condensate of the steam at the top of the first rectification tower T-01 after heat exchange enters the phase separation tank S1, the heavy phase is refluxed, and the first rectification The temperature at the top of the distillation tower T-01 is 90°C, and the temperature at the bottom of the tower is 103°C, and the bottom of the tower can obtain pure water and organic residues (or other high boilers). The light phase is extracted and enters the second rectification tower T-02. Th...

Embodiment 3

[0024] With butanol 5% (wt), butyl acetate 3% (wt), water 90% (wt), the flow of organic residue (or other high boiler) 2% (wt) is the waste water of 1.0 tons / hour through Heat exchanger H-01 is preheated to 52°C, then heated to 90°C by heat exchanger H-02, and then enters the first rectification tower T-01, the number of theoretical plates of the first rectification tower T-01 is 32 , the tower diameter is 0.8 meters, the operating pressure is normal pressure, the tower kettle is heated by steam, the condensate of the steam at the top of the first rectification tower T-01 after heat exchange enters the phase separation tank S1, the heavy phase is refluxed, and the first rectification The temperature at the top of the distillation tower T-01 is 95° C., and the temperature at the bottom of the tower is 105° C. The bottom of the tower can obtain pure water and organic residues (or other high boilers). The light phase is extracted and enters the second rectification tower T-02. Th...

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Abstract

The invention relates to a process for separating and recovering butyl acetate and butyl alcohol in wastewater by using azeotropic rectification, comprising the following steps of: carrying out normal-pressure distillation and thickening on the wastewater containing the butyl alcohol, the butyl acetate, water and organic residues in a first rectifying tower T-01 to obtain pure water and the organic residues through a tower kettle; delaminating condensed steam at a tower top, flowing a water layer back, and causing an organic layer to enter a second rectifying tower T-02 for pressurization and rectification under 120-200 Kpa so that the high-purity butyl acetate is extracted by the tower kettle and the steam with the alcohol ester ratio of 3/1-9/1 is obtained at the tower top; condensing to cause one part of a condensate to back flow and one part of the condensate to enter a third rectifying tower T-03 for pressure reduction and rectification under 3-15 KPa so that the high-purity butyl alcohol is extracted by the tower kettle and the steam with the alcohol ester ratio of 1/3-1/2 is obtained at the tower top; and after condensing and cooling, causing the steam with the alcohol ester ratio of 1/3-1/2 to enter the tower from a feed inlet of the second rectifying tower T-02 for continuous thickening and purification. The process has the advantages of environmental protection, low energy consumption, investment saving, no entrainer addition, high recovery rate (above 99%) of solvents and the like.

Description

technical field [0001] The invention relates to a process for separating and recovering butyl acetate and butanol in waste water by azeotropic rectification, referred to as the m-HSAD process. Background technique [0002] Butyl acetate is an important basic chemical raw material, which is widely used as a solvent in the paint, artificial leather and plastic industries. It can also be used as an extraction agent, to prepare banana water and in the perfume industry. The industrial production of butyl acetate generally adopts the traditional sulfuric acid catalyzed esterification method, which is divided into several process sections such as esterification, neutralization and washing, and rectification. In the production process, rectification energy consumption accounts for about 40% of the total energy consumption, and reducing energy consumption in the rectification process is an important way to save energy in the production of butyl acetate. In the esterification process...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C69/14C07C67/54C07C31/12C07C29/82C02F1/04
Inventor 周政张志炳邵旻孙德芳
Owner NANJING UNIV
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