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Method for producing aromatics by catalytic conversion of methanol and/or dimethyl ether

A technology for catalytic conversion and dimethyl ether, which is applied in the treatment of hydrocarbon oil, hydrocarbon oil treatment products, preparation of liquid hydrocarbon mixtures, etc., can solve the problems of hydrothermal deactivation of catalysts, low yield of aromatics, etc., and achieve high yield of aromatics , good technical effect, the effect of maintaining catalyst activity

Active Publication Date: 2021-05-28
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The above-mentioned patented technologies all have the problems of low yield of aromatics and severe hydrothermal deactivation of the catalyst

Method used

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  • Method for producing aromatics by catalytic conversion of methanol and/or dimethyl ether
  • Method for producing aromatics by catalytic conversion of methanol and/or dimethyl ether
  • Method for producing aromatics by catalytic conversion of methanol and/or dimethyl ether

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0027] The raw material of methanol and / or dimethyl ether enters the fluidized bed reactor and contacts with the modified ZSM-5 catalyst to obtain the product containing aromatics and the raw catalyst, and the raw catalyst enters the first regenerator at 500°C and the regeneration medium Ⅰ contact with charring to get semi-regenerated catalyst and re-flue gas, semi-regenerated catalyst enters the degassing tank zone Ⅰ and degassing medium Ⅰ contact to obtain degassed semi-regenerated catalyst, after degassing semi-regenerated catalyst enters the second regeneration The device is contacted with the regeneration medium II under the condition of 610°C and continues to burn to obtain the regenerated catalyst and secondary flue gas. The regenerated catalyst is returned to the fluidized bed reactor after gas, and the primary flue gas and secondary flue gas are combined into the subsequent system.

[0028] The degassing tank is divided into a degassing tank zone I and a degassing tan...

Embodiment 2

[0036]According to the conditions and steps described in Example 1, the regeneration temperature of the first regenerator is 600°C, and the regeneration temperature of the second regenerator is 700°C. Zone I of the degassing tank is located on the upper part of zone II of the degassing tank, and the separator is a large-pore distribution plate with an opening rate of 20%. The volume ratio of degassing tank zone I and degassing tank zone II is 1:1. The water vapor entrainment of the semi-regenerated catalyst after degassing was 0.01%. The carbon content of the regenerated catalyst is 0.01% by weight of the catalyst. With dimethyl ether as raw material. The water pressures of regeneration medium I, regeneration medium II, degassing medium I, degassing medium II, lifting medium of the first regenerator, and lifting medium of degassing tank are all 0.5 kPa at 20°C. The degassing medium I and II, the lifting medium of the first regenerator and the lifting medium of the degassing...

Embodiment 3

[0040] According to the conditions and steps described in Example 1, the regeneration temperature of the first regenerator is 550°C, and the regeneration temperature of the second regenerator is 670°C. The degassing tank zone I and the degassing tank zone II are arranged side by side, and the partition height accounts for 70% of the total height of the degassing tank. The volume ratio of degassing tank zone I and degassing tank zone II is 0.8:1. The water vapor entrainment of the semi-regenerated catalyst after degassing was 0.05%. The carbon content of the regenerated catalyst is 0.2% by weight of the catalyst. The mass percent content of methanol in the methanol raw material is 99%. The water pressures of regeneration medium Ⅰ, regeneration medium Ⅱ, degassing medium Ⅰ, degassing medium Ⅱ, lifting medium of the first regenerator, and lifting medium of degassing tank at 20°C are 0.03 kPa, 0.01 kPa, and 0.01 kPa, respectively , 0.01 kPa, 0.02 kPa, 0.02 kPa. The temperature...

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Abstract

The invention relates to a method for preparing aromatics by catalytic conversion of methanol and / or dimethyl ether, 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 raw material of methanol and / or dimethyl ether enters the fluidized bed reactor and the modified ZSM-5 catalyst is contacted to obtain the product containing aromatics and the unborn catalyst, and the unborn catalyst enters the first regenerator and is contacted with the regeneration medium I for burning. The coke is used to obtain the semi-regenerated catalyst and re-flue gas. The semi-regenerated catalyst enters the degassing tank I zone of the degassing tank and contacts the degassing medium I to obtain a degassed semi-regenerated catalyst. After degassing, the semi-regenerated catalyst enters the second regenerator and regenerated The medium II contacts and continues to burn to obtain the regenerated catalyst and secondary flue gas. The regenerated catalyst enters the degassing tank II zone of the degassing tank and contacts the degassing medium II to obtain a degassed regenerated catalyst. After degassing, the regenerated catalyst returns to the fluidized bed for reaction The device 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 and / or dimethyl ether. 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-period methanol catalysts and large-scale methanol plant technology in recent years, the production cost of coal-based methanol and / or dimethyl ether has been greatly reduced, which provides a great opportunity for the downstream products of methanol and / or dimethyl ether (olefins, aromatics) etc.) produ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G3/00
CPCC10G3/49C10G3/57C10G3/62C10G2400/30Y02P30/20
Inventor 李晓红钟思青俞志楠王莉
Owner CHINA PETROLEUM & CHEM CORP