Method for methanol conversion to aromatics

A technology of methanol and aromatics, applied in the field of catalytic conversion of methanol to aromatics, which can solve the problems of low aromatics yield, achieve high aromatics yield, weaken metal modification, and maintain the effect of catalyst activity

Active Publication Date: 2021-07-30
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The technical problem to be solved by the present invention is the technical problem of low yield of aromatics in the prior art, and a method for producing aromatics by catalytic conversion of methanol is provided, which has the advantage of high yield of aromatics

Method used

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  • Method for methanol conversion to aromatics

Examples

Experimental program
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Effect test

Embodiment 1

[0032] The methanol raw material enters the fluidized bed reactor and contacts with the modified ZSM-5 catalyst to obtain the product containing aromatics and the spent catalyst, and the stripped spent catalyst enters the riser regenerator and contacts regeneration medium I under the condition of 500°C Burnt, the outlet of the riser regenerator is connected to a set of closed cyclone separators, and the semi-regenerated catalyst separated by the closed cyclone separators enters the fluidized bed regenerator and contacts regeneration medium II to continue to burn under the condition of 630°C The regenerated catalyst is obtained, the regenerated catalyst enters the degassing tank, and the degassed product returns to the fluidized bed regenerator; the temperature of the regenerated catalyst after degassing is 450°C; 50% of the regenerated catalyst is returned to the riser regenerator after degassing; regenerated after degassing 50% of the catalyst is returned to the fluidized bed ...

Embodiment 2

[0037]According to the conditions and steps described in Example 1, the ungenerated catalyst enters the riser regenerator and contacts regeneration medium I and burns under the condition of 600 ° C, and the semi-regenerated catalyst enters the fluidized bed regenerator and contacts regeneration medium II at 700 ° C The temperature of the regenerated catalyst after degassing is 550°C; 90% of the regenerated catalyst after degassing is returned to the riser regenerator; 10% of the regenerated catalyst is returned to the fluidized bed reactor after degassing; the riser is regenerated The residence time of the catalyst in the vessel is 1 second; the mass ratio of hydrogen and carbon elements of the coke on the semi-regenerated catalyst is 0.06; the volume percentage of oxygen in the regeneration medium I is 30%. The carbon content of the regenerated catalyst is 0.01% by weight of the catalyst. The degassing tank is provided with an external heat extractor. The water pressures of ...

Embodiment 3

[0042] According to the conditions and steps described in Example 1, the ungenerated catalyst enters the riser regenerator and contacts regeneration medium I and burns under the condition of 550 ° C, and the semi-regenerated catalyst enters the fluidized bed regenerator and contacts regeneration medium II at 650 ° C The temperature of the regenerated catalyst after degassing is 500°C; 70% of the regenerated catalyst after degassing is returned to the riser regenerator; 30% of the regenerated catalyst is returned to the fluidized bed reactor after degassing; the riser is regenerated The residence time of the catalyst in the vessel is 3 seconds; the mass ratio of hydrogen and carbon elements of the coke on the semi-regenerated catalyst is 0.02; the volume percentage of oxygen in the regeneration medium I is 25%. The carbon content of the regenerated catalyst is 0.05% by weight of the catalyst. The degassing tank is provided with an external heat extractor. The water pressures o...

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Abstract

The invention relates to a method for preparing aromatics by catalytic conversion of methanol, 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 to obtain the product containing aromatics and the unborn catalyst, and the unborn catalyst after stripping enters the riser regenerator and contacts the regeneration medium I at 500~ Burned under the condition of 600 ℃, the outlet of the riser regenerator is connected with at least one set of closed cyclone separators, and the semi-regenerated catalyst separated by the closed cyclone separators enters the fluidized bed regenerator and contacts regeneration medium II at 630~ The technical scheme of continuing to burn at 700°C to obtain a regenerated catalyst, the regenerated catalyst entering the degassing tank, and the degassed product returning to the fluidized bed regenerator 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 preparing aromatics by catalytic conversion of methanol. 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 r...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C15/04C07C15/06C07C15/08
CPCC07C1/20C07C2529/40C07C2529/44C07C15/04C07C15/06C07C15/08Y02P20/584
Inventor 李晓红齐国祯金永明王艳学
Owner CHINA PETROLEUM & CHEM CORP
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