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Method for producing ethylene glycol and 1,2-propylene glycol through continuous hydrocrackin of sugars

A technology of hydrocracking and ethylene glycol, which is applied to the production of ethylene glycol from sugar solution. cost effect

Active Publication Date: 2014-07-02
DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

From the perspective of large-scale industrial applications, batch operation is not only time-consuming, inconvenient to operate, but also a waste of energy and materials

Method used

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  • Method for producing ethylene glycol and 1,2-propylene glycol through continuous hydrocrackin of sugars
  • Method for producing ethylene glycol and 1,2-propylene glycol through continuous hydrocrackin of sugars
  • Method for producing ethylene glycol and 1,2-propylene glycol through continuous hydrocrackin of sugars

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Experimental program
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Effect test

Embodiment 1

[0031] The glucose of 50wt% and the ammonium metatungstate 0.1wt% (in terms of metal tungsten weight) aqueous solution of 50wt% enter hydrogenation reactor by high-pressure pump, are filled with the Ru / AC of slurry state and tungstic acid catalyst (ruthenium The weight ratio of tungsten to tungsten is 1:10, water is used as solvent to immerse the catalyst at the beginning of the reaction), the weight ratio of sugar raw material to catalyst (the sum of the weight of ruthenium and tungsten elements) is between 450:1 and 460:1, and the volume is empty Speed ​​is 2 to 3. The temperature of the reactor is 220-230° C., and the hydrogen pressure is 5 MPa. Hydrogen enters from the bottom of the reactor and stirs the catalyst slurry. The reaction solution enters the reactor and is discharged from the upper outlet of the reactor after being reacted, accompanied by 1wt% solid catalyst (Ru / AC), part of hydrogen and gas products. The reactor effluent then enters a separator to separate g...

Embodiment 2

[0040] The glucose of 40wt% and the ammonium metatungstate 0.05wt% (in terms of metal tungsten weight) aqueous solution of 40wt% enter hydrogenation reactor by high-pressure pump, the Ru / AC of slurry state and tungstic acid catalyst (ruthenium The weight ratio of tungsten to tungsten is 1:5, water is used as solvent to immerse the catalyst at the beginning of the reaction), the weight ratio of sugar raw material to catalyst (the sum of the weight of ruthenium and tungsten elements) is between 800:1 and 750:1, and the volume is empty The speed is 10 to 20. The temperature of the reactor is 250-260° C., and the hydrogen pressure is 6 MPa. Hydrogen enters from the bottom of the reactor and stirs the catalyst slurry. The reaction liquid enters the reactor and is discharged from the upper outlet of the reactor after being reacted, accompanied by some hydrogen and gas products. Then the reactor effluent enters the separator to separate the gas and liquid parts.

[0041] The gas p...

Embodiment 3

[0049] The glucose of 60wt% and the ammonium metatungstate 0.2wt% (in terms of metal tungsten weight) aqueous solution of 60wt% enter hydrogenation reactor by high-pressure pump, the Ru / AC and tungstic acid catalyst (ruthenium of ruthenium) of slurry state are packed in the reactor The weight ratio to tungsten is 1:1, the catalyst is immersed in water as solvent at the beginning of the reaction), the weight ratio of sugar raw material to catalyst (the sum of the weight of ruthenium and tungsten elements) is 150:1, and the volume space velocity is 70 to 80. The temperature of the reactor is 240-250° C., and the hydrogen pressure is 10 MPa. Hydrogen enters from the bottom of the reactor and stirs the catalyst slurry. The reaction liquid enters the reactor and is discharged from the upper outlet of the reactor after being reacted, accompanied by a part (0.5-2wt%) of solid catalyst (Ru / AC), part of hydrogen and gas products. The reactor effluent then enters a separator to separat...

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Abstract

The invention relates to a continuous reaction process for producing ethylene glycol and 1,2-propanediol by catalytic hydrocracking sugar conversion, and provides a method for producing ethylene glycol and 1,2-propanediol by continuous hydrogenation cracking sugar conversion. During this process, sugars (including one or more of sucrose, glucose, fructose, xylose, soluble xylooligosaccharides, and starch) are hydrocracked by catalysts in the reactor and then enter the separation system. The hydrogen in the gas phase is separated and recovered for recycling; part of the liquid phase product is returned to the reactor, and the rest of the liquid phase product is refined to separate ethylene glycol, propylene glycol, and other polyols; it exists in the remaining heavy components after refining and separation. Concentrate in the liquid phase The soluble catalyst components are partially recycled back to the reactor.

Description

technical field [0001] The invention relates to a process for preparing ethylene glycol and 1,2-propanediol from a sugar solution, in particular to a continuous reaction process for producing ethylene glycol and 1,2-propanediol by catalytic hydrogenation cracking of sugars. Background technique [0002] Ethylene glycol (EG for short), also known as glycol and ethylene glycol, is an important petrochemical basic organic raw material, mainly used in the production of polyester fiber, antifreeze, unsaturated polyester resin, lubricant, plasticizer Agents, non-ionic surfactants and explosives, etc. In addition, it can also be used in coatings, photographic developers, brake fluids and inks, as a solvent and medium for ammonium perborate, and for the production of special solvents such as glycol ethers. very broad. [0003] At present, the large-scale industrial production of ethylene glycol at home and abroad adopts the process route of direct hydration of ethylene oxide, that ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C31/20C07C29/00C07C31/22C07C31/12C07C31/26
CPCC07C29/60C07C29/132B01J23/462B01J23/6525C07C31/205C07C31/202
Inventor 张涛陈曙光郑明远王爱琴于婷婷丁玉龙
Owner DALIAN INST OF CHEM PHYSICS CHINESE ACAD OF SCI
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