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Method for preparing glycolate through oxalate gas phase hydrogenation

A technology of glycolate and oxalate, which is applied in the preparation of carboxylate, chemical instruments and methods, and the preparation of organic compounds, can solve the problem of low selectivity of glycolate and achieve good technical effects

Active Publication Date: 2014-08-13
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0007] The technical problem to be solved by the present invention is the technical problem of low selectivity of glycolate in the reaction process of hydrogenation of oxalate ester to glycolate in the previous document technology, and a new gas-phase hydrogenation of oxalate ester is provided. Glycolate method

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  • Method for preparing glycolate through oxalate gas phase hydrogenation

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Comparison scheme
Effect test

Embodiment 1

[0018] use figure 1 The fluidized bed reactor adopts a composition of 28wt% Cu+6wt%Zn+1wt%Ag / SiO 2 The average diameter of catalyst particles is 80 microns, 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, and 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 connecting port of the regenerated inclined pipe and the dense-phase area from the bottom of the dense-phase area is 1 / 4 of the vertical height of the dense-phase area. 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. Dimethyl oxalate is used as raw material, the weight ratio of raw mat...

Embodiment 2

[0020] use figure 1 The fluidized bed reactor adopts composition as 35wt% Cu+2wt%Zn+0.5wt%Ag / SiO 2 The average diameter of catalyst particles is 120 microns, 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, and 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 connecting port of the regenerated inclined pipe and the dense-phase area from the bottom of the dense-phase area is 1 / 8 of the vertical height of the dense-phase area. 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. Dimethyl oxalate is used as raw material, the weight ratio of raw mate...

Embodiment 3

[0022] use figure 1 The fluidized bed reactor adopts a composition of 35wt% Cu+1wt%Ni+2wt%Ag / SiO 2 The average diameter of the catalyst particles is 120 microns, and methanol is used as 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, and the inner diameter of the riser is 1 / 4 of 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 connecting port of the regenerated inclined pipe and the dense-phase area and the bottom of the dense-phase area is 1 / 6 of the vertical height of the dense-phase area. 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. Dimethyl oxalate is used as raw material, the we...

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Abstract

The invention relates to a method for preparing glycolate through oxalate gas phase hydrogenation and mainly solves the technical problem of low glycolate selectivity in the reaction process of preparing the glycolate through the oxalate gas phase hydrogenation existing in the prior art. With the adoption of the technical scheme that the method for preparing the glycolate through the oxalate gas phase hydrogenation comprises the following steps that: oxalate is taken as a raw material, methanol, ethanol or water are taken as a terminating agent, and under the conditions that the reaction temperature is 100-250 DEG C, the weight airspeed is 0.2-5 hour<-1>, the molar ratio of hydrogen to the oxalate is (10-100):1, and the reaction pressure is 0-6.0 MPa, the raw material is in contact with a copper-contained catalyst in a fluidized bed reactor to generate an effluent containing the glycolate, so the problem is better solved. The method can be used in the industrial production for making the glycolate through the oxalate gas phase hydrogenation.

Description

technical field [0001] The invention relates to a method for preparing glycolate by gas-phase hydrogenation of oxalate, in particular about the use of a fluidized bed reactor coupled with a riser reactor and a quick separation device, which is applicable to the reaction process of hydrogenation of oxalate to glycolate middle. Background technique [0002] With its unique molecular structure: it has a-H, hydroxyl and ester functional groups at the same time, which makes it have the chemical properties of alcohol and ester, and can undergo carbonylation reaction, hydrolysis reaction, oxidation reaction, etc., and has become an important chemical raw material . Glycolate is an excellent solvent for many celluloses, resins, and rubbers. Its downstream products such as glycolic acid, glycine, dimethyl malonate and glyoxylic acid also have extensive application value. [0003] At present, there is no mature production process of environmentally friendly glycolic acid ester in C...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C69/675C07C67/31B01J8/22
Inventor 刘俊涛李蕾张琳娜
Owner CHINA PETROLEUM & CHEM CORP