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Method for preparing ethylene glycol mono-n-butyl ether by continuous pipe reaction

A technology of mono-n-butyl ether and ethylene glycol, which is applied in the field of continuous pipeline reaction to prepare ethylene glycol mono-n-butyl ether, can solve problems such as difficulty in improving production efficiency, low equipment utilization rate, and complicated process, and achieve improved production Efficiency, reduced production costs, and simple operation

Active Publication Date: 2009-01-07
江苏德纳化学股份有限公司
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The purpose of the present invention is to provide a method for preparing ethylene glycol mono-n-butyl ether by continuous pipeline reaction, which overcomes the defects of complex process, low equipment utilization rate and difficulty in improving production efficiency in the batch reaction process. Pipeline reaction to improve the production efficiency of ethylene glycol mono-n-butyl ether, and the catalyst has high activity, good selectivity and high product yield

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0018] The adiabatic reaction method is used. The pipe reactor adopts a stainless steel pipe with an outer diameter of 8 mm, a wall thickness of 1 mm, and a length of 180 m. The outer wall of the pipe reactor is insulated with an insulating material, and the volume of the reactor is 5 L. The catalyst zinc methanedisulfonate is prepared in the raw material n-butanol according to 0.04% of the mass of butanol, and the n-butanol equipped with the catalyst methanedisulfonate is transported by a metering pump, and the flow rate is controlled at 2.26L / h, epoxy Ethane is transported by another metering pump, and the flow rate is controlled at 0.24L / h. The n-butanol and ethylene oxide delivered by two metering pumps are mixed through a static mixer, and the reaction raw materials are preheated to 140°C through a preheater. , continuously sent into the pipeline reactor, and the pressure regulating valve set at the outlet of the pipeline reactor controls the operating pressure to 5.0MPa....

Embodiment 2

[0020] An isothermal reaction method was used. The pipe reactor adopts a stainless steel pipe with an outer diameter of 8mm, a wall thickness of 1mm, and a length of 180m, and the reactor volume is 5L. The pipeline reactor is placed in an oil bath, and the heat conduction oil in the oil bath is equipped with a temperature control adjustment system. The heat conduction oil in the oil bath can effectively remove the reaction heat released from the pipeline reactor, and achieve the effect of isothermal reaction. The catalyst is a mixture of aluminum trifluoromethanesulfonate and zinc methanedisulfonate, and the catalyst aluminum trifluoromethanesulfonate and zinc methanedisulfonate are prepared in the raw material at 0.01% and 0.02% of butanol mass respectively. In butanol, n-butanol equipped with a catalyst mixture of aluminum trifluoromethanesulfonate and zinc methanedisulfonate is transported by a metering pump with a flow rate of 1.85L / h, and ethylene oxide is transported by ...

Embodiment 3

[0022]A method combining partial isothermal reaction and partial adiabatic reaction is adopted. The pipe reactor adopts a stainless steel pipe with an outer diameter of 8mm, a wall thickness of 1mm, and a length of 180m, and the reactor volume is 5L. A 30m long stainless steel pipe is placed in an oil bath. The heat conduction oil in the oil bath is equipped with a temperature control adjustment system. The heat conduction oil in the oil bath can effectively remove the reaction heat released from the pipeline reactor and achieve the effect of partial isothermal reaction. Insulate the outer wall of a 150m-long stainless steel pipe with insulation materials. The catalyst uses aluminum trifluoromethanesulfonate, and the catalyst aluminum trifluoromethanesulfonate is prepared in the raw material n-butanol according to 0.03% of the mass of butanol. The n-butanol of aluminum fluoromethyl sulfonate is delivered by a metering pump with a control flow rate of 2.26L / h, and the ethylene ...

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Abstract

The invention relates to a method for preparing glycol mono-n-butyl ether by continuous channel reaction, which comprises the following steps: mixing n-butyl alcohol, ethylene oxide and alkyl sulfonate serving as a catalyst, preheating, continuously feeding into a channel reactor, carrying out etherification reaction at a reaction temperature of 130 to 220 DEG C and under a pressure of 3.5 to 6.0 MPa, and rectifying the reaction result to recover the excessive n-butyl alcohol and obtain the glycol mono-n-butyl ether. According to the method, the conversion rate of the ethylene oxide is 100%, and the selectivity of the glycol mono-n-butyl ether is 85 to 94%. The continuous channel reaction process can improve the production efficiency of the glycol mono-n-butyl ether, and has excellent large-scale industrial application prospect.

Description

technical field [0001] The invention relates to a method for preparing ethylene glycol mono-n-butyl ether, in particular to a method for preparing ethylene glycol mono-n-butyl ether through continuous pipeline reaction. Background technique [0002] As the glycol ether used as a solvent, the amount of ethylene glycol mono-n-butyl ether and its acetate is the largest. It has good dispersibility in water and is widely used in water-based coatings. In addition, it is also an excellent solvent for nitrocellulose, alkyd resin and phenolic resin. Due to its slow evaporation rate, it is effective in improving the gloss of varnishes and preventing peeling. It can be used as a thinner in quick-drying paints and enamel paints to increase the adhesion between paints, wood and metal. [0003] The etherification reaction of n-butanol and ethylene oxide (EO) is a common method for preparing ethylene glycol mono-n-butyl ether, usually using liquid acid (such as BF 3 Diethyl ether comple...

Claims

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Application Information

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IPC IPC(8): C07C43/13C07C41/03B01J31/04
Inventor 秦旭东秦怡生陈荣福王伟蒋大智
Owner 江苏德纳化学股份有限公司
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