A method for efficiently converting methanol to aromatics

A technology for methanol and aromatics, applied in the field of high-efficiency conversion of methanol to aromatics, can solve the problems of low yield of aromatics, hydrothermal deactivation of catalysts, etc., achieve high yield of aromatics, good technical effect, and maintain the effect of catalyst activity

Active Publication Date: 2021-11-30
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] It can be seen that the existing patented technologies all have the problems of severe hydrothermal deactivation of the catalyst and low yield of aromatics

Method used

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  • A method for efficiently converting methanol to aromatics

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] The methanol mass percentage content is 100% methanol raw material enters the fluidized bed reactor and the modified ZSM-5 catalyst at 440 ° C, the reaction gauge pressure is 0 MPa, and the methanol weight space velocity is 0.2 hours -1 Under the conditions of contact reaction, the reaction product containing aromatics and the raw catalyst are separated by the cyclone separator of the reactor, and the reaction product enters the subsequent separation system; The catalyst and flue gas I enter the riser regeneration cyclone separator connected to the riser regenerator, and the separated semi-regenerated catalyst enters the double-dense bed A area to contact with the degassing medium I, and the separated flue gas I enters the subsequent flue gas system ; After degassing, 20% of the semi-regenerated catalyst returns to the riser regenerator, and after degassing, 80% of the semi-regenerated catalyst enters the fast bed regenerator and regeneration medium II for contact regene...

Embodiment 2

[0037] According to the conditions and steps described in Example 1, methanol mass percentage content is 10% methanol raw material enters the fluidized bed reactor and catalyst at 550 ° C, the reaction gauge pressure is 1 MPa, and the methanol weight space velocity is 15 hours -1 50% of the semi-regenerated catalyst after degassing returns to the riser regenerator, and 50% of the semi-regenerated catalyst enters the fast-bed regenerator after degassing and contacts regeneration medium II.

[0038] The height of the partition is 90% of the total height of the double dense bed; the volume ratio of the area A of the double dense bed and the area B of the double dense bed is 1:1.

[0039] The temperature of the catalyst in the fast bed regenerator is 700°C, the density of the catalyst bed is 110 kg / m3, and the residence time of the catalyst is 5 minutes.

[0040] The catalyst temperature in the riser regenerator is 600°C, the catalyst density is 50 kg / m3, and the catalyst residenc...

Embodiment 3

[0046] According to the conditions and steps described in Example 1, methanol mass percentage composition is 98% methanol raw material enters fluidized bed reactor and catalyst at 490 ° C, reaction gauge pressure is 0.3 MPa, methanol weight space velocity is 4 hours -1 30% of the semi-regenerated catalyst is returned to the riser regenerator after degassing, and 70% of the semi-regenerated catalyst after degassing enters the fast bed regenerator and is contacted with regeneration medium II for regeneration.

[0047] The height of the partition is 70% of the total height of the double dense bed; the volume ratio of the area A of the double dense bed and the area B of the double dense bed is 0.8:1.

[0048] The temperature of the catalyst in the fast bed regenerator is 650°C, the density of the catalyst bed is 180 kg / m3, and the residence time of the catalyst is 25 minutes.

[0049] The catalyst temperature in the riser regenerator is 570°C, the catalyst density is 82 kg / m3, and...

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Abstract

The invention relates to a method for efficiently converting methanol to produce aromatics, which mainly solves the problems of low yield of aromatics and serious hydrothermal deactivation of catalysts in the prior art. In the present invention, the methanol raw material enters the fluidized bed reactor and the modified ZSM-5 catalyst is contacted and reacted under effective reaction conditions; the unborn catalyst enters the riser regenerator for regeneration, and the obtained semi-regenerated catalyst and flue gas I enter and rise the riser The riser regeneration cyclone separator connected to the regenerator, the separated semi-regenerated catalyst enters the double-dense bed A area for degassing; after degassing, the semi-regenerated catalyst part returns to the riser regenerator, and part of it enters the fast bed regenerator for regeneration, and the obtained regenerated The technical scheme that the catalyst enters the double-dense bed B area for degassing, and the regenerated catalyst enters the fluidized bed reactor after degassing solves this problem well, and can be used in the industrial production of aromatics.

Description

technical field [0001] The invention relates to a method for efficiently converting methanol to aromatics. Background technique [0002] Aromatic hydrocarbons (especially triphenyl, benzene, toluene, xylene, namely BTX) are important basic raw materials for organic synthesis. Driven by the demand for downstream derivatives, the market demand for aromatics continues to grow. [0003] Catalytic reforming and steam cracking processes are the main production processes of aromatics, which belong to the petroleum route production technology. my country is relatively rich in coal resources. With the successful development of high-efficiency, long-cycle methanol catalysts and large-scale methanol plant technology in recent years, the production cost of coal-based methanol has been greatly reduced, which provides a cheap source of raw materials for the production of methanol downstream products (olefins, aromatics, etc.). Therefore, it is considered to use methanol as raw material...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C15/02
CPCC07C1/20C07C2529/40C07C15/02Y02P20/584
Inventor 李晓红齐国祯金永明俞志楠
Owner CHINA PETROLEUM & CHEM CORP
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