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A methanol aromatization process

A technology of aromatization and methanol, which is applied in the field of aromatization technology, can solve the problems of low oil phase yield, which is difficult to exceed 30%, and achieve improved oil phase yield, high methanol utilization rate, and good selectivity Effect

Active Publication Date: 2016-06-08
SINOPEC LUOYANG PETROCHEM ENG CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In all the patent literature reports about MTA reactors, it is one-stage type, and its heat extraction method adopts an external heat extraction and cold source, and the biggest disadvantage of the one-stage type is that the oil phase yield is relatively low, which is difficult to exceed 30%.

Method used

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  • A methanol aromatization process

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0034] 1. Preparation of tube-side catalyst

[0035] 1) Weigh 70 g of ZSM-5 molecular sieve with a silicon-aluminum ratio of 38, and calcinate it at 550° C. for 4 hours to remove physically adsorbed impurities.

[0036] 2) Weigh 10g of SAPO-34 molecular sieve, 20g of coagulant SB powder, and 3g of Tianqing powder, and mix them evenly with the ZSM-5 roasted in step (1).

[0037]3) Weigh 50g of water, add 3g of citric acid, 5ml of nitric acid and stir evenly, add to the mixture in step 2), stir well, extrude it into a columnar shape of Φ2 with a screw extruder, and place it in an oven at 120°C Dry at 550°C for 4 hours to remove nitric acid and moisture. The calcined catalyst is crushed into 20-40 mesh particles for later use.

[0038] 4) Weigh an appropriate amount of Cu and P nitrate to form a solution, weigh 20 g of the catalyst prepared in step 3) and impregnate it in equal volume, stand at room temperature for 24 hours, and dry at 120 ° C. During this period, stir once ever...

Embodiment 2

[0055] 1. Preparation of tube-side catalyst

[0056] 1) Weigh 60 g of ZSM-5 molecular sieve with a silicon-aluminum ratio of 38, and calcinate it at 550° C. for 4 hours to remove physically adsorbed impurities.

[0057] 2) Weigh 20g of SAPO-34 molecular sieve, 20g of coagulant SB powder, and 3g of Tianqing powder, and mix them evenly with the ZSM-5 roasted in step 1).

[0058] 3) Weigh 50g of water, add 3g of citric acid, 5ml of nitric acid and stir evenly, add to the mixture in step 2), stir well, extrude it into a columnar shape of Φ2 with a screw extruder, and place it in an oven at 120°C Dry at 550°C for 4 hours to remove nitric acid and moisture. The calcined catalyst is crushed into 20-40 mesh particles for later use.

[0059] 4) Weigh an appropriate amount of Cu and Zn nitrate to form a solution, weigh 20 g of the catalyst prepared in step 3) and impregnate it in equal volume, stand still at room temperature for 24 hours, and dry at 120 ° C. During this period, stir on...

Embodiment 3

[0076] 1. Preparation of tube-side catalyst

[0077] 1) Weigh 60 g of ZSM-5 molecular sieve with a silicon-aluminum ratio of 60, and bake it at 550° C. for 4 hours to remove physically adsorbed impurities.

[0078] 2) Weigh 20g of 5APO-34 molecular sieve, 20g of coagulant SB powder, and 3g of Tianqing powder, and mix them evenly with the ZSM-5 roasted in step 1).

[0079] 3) Weigh 50g of water, add 3g of citric acid, 5ml of nitric acid and stir evenly, add to the mixture in step 2), stir well, extrude it into a columnar shape of Φ2 with a screw extruder, and place it in an oven at 120°C Dry at 550°C for 4 hours to remove nitric acid and moisture. The calcined catalyst is crushed into 20-40 mesh particles for later use.

[0080] 4) Weigh an appropriate amount of Cu, Zn, and P nitrates to make a solution, weigh 20g of the catalyst prepared in step 3) and impregnate it in equal volume, stand at room temperature for 24h, dry at 120°C, and stir once every 1h during this period , ...

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Abstract

The invention discloses a methanol aromatization process. The steps are: 1) Methanol enters the tube side of the reactor to contact with the tube side catalyst, the operating temperature is 400-450°C, the operating pressure is 0.1-5Mpa, and the liquid space velocity of the raw material methanol is 0.5-7.0h -1 ; 2) The reaction product from the tube side enters the shell side of the reactor to contact with the catalyst on the shell side, the operating temperature is 330-380°C, the operating pressure is 0.1-3.5Mpa, and the operating space velocity is 0.4-4.0h -1 , converted to C through shell-side catalysis 5 + Hydrocarbon liquid products are separated by rectification to obtain aromatics and non-aromatics. After the gas products in the shell side products are separated, the low carbon olefins return to the shell side of the reactor to continue the reaction. The use of the invention can improve the utilization rate of methanol, simplify complex reactions, increase the selectivity of low-carbon olefins, and reduce the generation of dry gas and liquefied gas.

Description

technical field [0001] The present invention relates to a methanol aromatization process, in particular to an aromatization process using methanol / dimethyl ether as a raw material to produce aromatic hydrocarbons through secondary reactions in the tube side of the reactor and the shell side of the reactor, using two different catalysts . Background technique [0002] With the development of coal chemical industry, the synthesis and conversion technology of coal-based methanol is becoming more and more mature. In recent years, in order to improve competitiveness, my country's methanol production is developing towards large-scale and energy-saving development. Coal-based methanol accounts for more than 80% of methanol production. Methanol production has increased year by year, leading to serious overcapacity problems. As of November 2012, there were 172 methanol production enterprises in China with a production capacity of more than 100,000 tons per year, with a total productio...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C15/02C10G3/00
CPCY02P20/52Y02P30/20
Inventor 李康魏小波郝代军韩海波毛继平张国良刘雪芬
Owner SINOPEC LUOYANG PETROCHEM ENG CORP
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