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Method for preparing ethylene glycol by gas-phase hydrogenating oxalate

A technology of oxalate and ethylene glycol, which is applied in chemical instruments and methods, preparation of hydroxyl compounds, preparation of organic compounds, etc., can solve the problem of low selectivity of ethylene glycol

Inactive Publication Date: 2012-08-29
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0009] The technical problem to be solved by the present invention is the low technical problem of ethylene glycol selectivity in the process of hydrogenation of oxalate ester used in the previous document technology to prepare ethylene glycol, and a new oxalate ester is provided through gas-phase hydrogenation Method for preparing ethylene glycol by reaction

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  • Method for preparing ethylene glycol by gas-phase hydrogenating oxalate
  • Method for preparing ethylene glycol by gas-phase hydrogenating oxalate

Examples

Experimental program
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Effect test

Embodiment 1

[0020] use figure 1 The fluidized bed reactor with a composition of 30wt%Cu+10wt%Bi+1wt%W / SiO 2 The average diameter of the catalyst particles is 80 microns, and methanol is the terminator. The vertical distance between the terminator injection port and the bottom of the riser is 1 / 15 of the length of the riser. The inner diameter of the riser is the outer diameter of the dense phase zone 1 / 10, the height of the riser is 1 / 4 of the height of the dense phase zone. The vertical distance between the connection port of the regenerating inclined pipe and the dense phase zone from the bottom of the dense phase zone is 1 / 4 of the vertical height of the dense phase zone. The vertical height of the transition zone is 1 / 10 of the vertical height of the dense phase zone. The vertical distance between the gas inlet of the cyclone separator and the top of the gas collection chamber is 1 / 8 of the diameter of the settler. Using dimethyl oxalate as raw material, the weight ratio of raw mater...

Embodiment 2

[0022] use figure 1 The fluidized bed reactor adopts a composition of 30wt%Cu+3wt%Al / SiO 2 The average diameter of the catalyst particles is 120 microns, and methanol is the terminator. The vertical distance between the terminator injection port and the bottom of the riser is 1 / 12 of the length of the riser. The inner diameter of the riser is the outer diameter of the dense phase zone. 1 / 7, the height of the riser is 1 / 6 of the height of the dense phase zone. The vertical distance between the connection port of the regenerating inclined pipe and the dense phase zone from the bottom of the dense phase zone is 1 / 8 of the vertical height of the dense phase zone. The vertical height of the transition zone is 1 / 6 of the vertical height of the dense phase zone. The vertical distance between the gas inlet of the cyclone separator and the top of the gas collection chamber is 1 / 4 of the diameter of the settler. Using dimethyl oxalate as raw material, the weight ratio of raw material t...

Embodiment 3

[0024] use figure 1 The fluidized bed reactor with a composition of 25wt%Cu+3wt%Zn / SiO 2 The average diameter of the catalyst particles is 120 microns, and methanol is the terminator. The vertical distance between the terminator injection port and the bottom of the riser is 1 / 4 of the length of the riser. The inner diameter of the riser is the outer diameter of the dense phase zone. 1 / 4, the height of the riser is 1 / 6 of the height of the dense phase zone. The vertical distance between the connection port of the regenerating inclined pipe and the dense phase zone from the bottom of the dense phase zone is 1 / 6 of the vertical height of the dense phase zone. The vertical height of the transition zone is 1 / 6 of the vertical height of the dense phase zone. The vertical distance between the gas inlet of the cyclone separator and the top of the gas collection chamber is 1 / 5 of the diameter of the settler. Using dimethyl oxalate as the raw material, the weight ratio of the raw mater...

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Abstract

The invention relates to a method for preparing ethylene glycol by gas-phase hydrogenating oxalate. The technical problem of the prior art of low selectivity of ethylene glycol during the process of preparing the ethylene glycol by hydrogenating oxalate is solved. The invention adopts the technical scheme that the method comprises the following steps of: taking oxalate as a raw material; taking carbinol, alcohol or water as a terminating agent; and contacting the raw material with a copper-containing catalyst in a fluidized bed reactor under the conditions of reaction temperature at 170-270 DEG C, weight hourly space velocity of oxalate at 0.2-5 per hour, mole ratio of hydrogen to ester at (40-200):1 and reaction pressure at 1.5-10MPa, thereby generating an effluent containing the ethylene glycol. According to the technical scheme, the problem is more efficiently solved. The method is suitable for the industrial production for preparing the ethylene glycol by hydrogenating oxalate.

Description

Technical field [0001] The invention relates to a method for preparing ethylene glycol from oxalate ester through gas phase hydrogenation reaction, in particular to a fluidized bed reactor coupled with a riser reactor and a fast separation device, which is practically used for the hydrogenation of oxalate ester to produce ethylene glycol During the reaction. Background technique [0002] Ethylene glycol (EG) is an important organic chemical raw material, mainly used in the production of polyester fiber, antifreeze, unsaturated polyester resin, lubricant, plasticizer, non-ionic surfactant and explosives, etc. It can be used in coatings, photographic developer, brake fluid, ink and other industries, used as a solvent and medium for ammonium perborate, and used in the production of special solvent glycol ethers. It has a wide range of uses. [0003] At present, my country has surpassed the United States to become the world's largest consumer of ethylene glycol. The average annual gro...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C31/20C07C29/149B01J8/22
Inventor 刘俊涛孙凤侠蒯骏
Owner CHINA PETROLEUM & CHEM CORP