Fluidized bed reactor for preparing methanol by synthesis gas and method

A fluidized bed reactor and fluidized bed technology, applied in chemical instruments and methods, preparation of hydroxyl compounds, preparation of organic compounds, etc., can solve serious problems, wear of catalysts and heat exchange tubes, and low production intensity, etc. Achieve the effects of low gas compression cost, increased production capacity, and long-term stable operation

Active Publication Date: 2012-06-27
TSINGHUA UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

In this case, the wear of the catalyst and the heat exchange tube is relatively serious
At the same time, the cross-sectional solid concentrat

Method used

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  • Fluidized bed reactor for preparing methanol by synthesis gas and method
  • Fluidized bed reactor for preparing methanol by synthesis gas and method
  • Fluidized bed reactor for preparing methanol by synthesis gas and method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0038] use as figure 2 The specific structure of the two-stage fluidized bed reactor shown is: the installation distance between the gas distributor 3 (porous plate type) and the first horizontal gas distribution plate 4 above it is 8 times the diameter of the fluidized bed 1; The pipe is externally placed, and the installation position is: the overflow pipe 6 connecting the first-stage catalyst dense-phase area 5 and the second-stage catalyst dense-phase area 5a, and the distance between the upper end installation position and the first horizontal gas distribution plate 4 is the fluidized bed 0.20 times of the diameter, and the distance between the installation position of the lower end and the gas distributor 3 at the lower part of the fluidized bed is 0.05 times of the diameter of the fluidized bed.

[0039] Cu / Zn / Al 2 o 3 Catalyst (copper content is 20wt%, zinc content is 30wt%, the rest is Al 2 o 3 ; Mohs hardness is 7, the average particle size is 50 microns, and th...

Embodiment 2

[0041] use as image 3 The specific structure of the three-stage fluidized bed reactor shown is: the installation distance between the gas distributor 3 (porous plate type) and the first horizontal gas distribution plate 4 above it is 10 times the diameter of the fluidized bed 1; The pipe adopts the combination of external and internal. The installation position of the external overflow pipe is: the overflow pipe 6 connecting the catalyst dense phase area 5 of the first stage and the catalyst dense phase area 5a of the second stage. The distance of 4a is 0.50 times the diameter of the fluidized bed 1, and the distance between the lower end installation position and the gas distributor 3 at the lower part of the fluidized bed is 0.5 times the diameter of the fluidized bed; the installation position of the built-in overflow pipe is: to connect the first stage catalyst The overflow pipe 6a of the dense phase zone 5 and the third stage catalyst dense phase zone 5b, the distance fr...

Embodiment 3

[0044] use as Figure 4The shown four-stage fluidized bed reactor has a specific structure as follows: the installation distance between the gas distributor 3 (porous plate type) and the first horizontal gas distribution plate 4 above it is 9 times the diameter of the fluidized bed 1; The pipe is externally placed, and the installation position is: the overflow pipe 6 connecting the first-stage catalyst dense-phase area 5 and the second-stage catalyst dense-phase area 5a, and the distance between the upper end of the installation position and the first transverse gas distribution plate 4 is 2 0.4 times the diameter of the bed, and the distance between the lower end installation position and the gas distributor 3 at the lower part of the fluidized bed is 0.1 times the diameter of the fluidized bed; The overflow pipe 6a, the distance between its upper end installation position and the second transverse gas distribution plate 4a is 0.4 times of the diameter of the fluidized bed, ...

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Abstract

The invention discloses a fluidized bed reactor for preparing methanol by synthesis gas and a method, belonging to the technical field of methanol preparation. One or a plurality of transverse band-hole gas distribution plates are arranged on the fluidized bed at different axial heights; the fluidized bed is divided into two or more catalyst dense-phase accumulation areas at the axial heights, meanwhile independent heat exchangers are arranged in different catalyst dense-phase areas for temperature change. The fluidized bed reaction disclosed by the invention has the advantages of permitting low hydrogen 2/carbon monoxide (H2/CO) rate operation, remarkably improving the methanol outlet concentration of the reactor and remarkably reducing cyclic hydrogen quantity, along with high heat exchange performance, low power consumption, high reactor section production flux, high operation operational flexibility, high carbon monoxide (CO) conversion rate, low methanol production cost and the like.

Description

technical field [0001] The invention belongs to the technical field of chemical process and equipment, and in particular relates to a fluidized bed reactor and a method for producing methanol from synthesis gas. Background technique [0002] Methanol is an important basic chemical and fuel. It can be used to prepare important chemicals such as acetic acid, dimethyl ether, and methyl acetate, and can be compounded with gasoline to form a fuel for motor vehicles. At the same time, it is also used as a solvent in the chemical absorption process. With the increasing demand in China's chemical industry market, the domestic annual demand for methanol is about 8-10 million tons. [0003] At present, the production process of industrial production of methanol is mostly the synthesis gas (H 2 / CO) under the action of a catalyst containing copper and zinc components, synthesize methanol in a fixed-bed reactor at 200-270°C and 40-100 atmospheric pressure. Since the reaction is a str...

Claims

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Application Information

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IPC IPC(8): B01J8/28C07C31/04C07C29/152
CPCY02P20/52
Inventor 骞伟中魏飞李琰李欢
Owner TSINGHUA UNIV
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