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Coaxial fluidized bed reaction system and reaction method for producing ethylene, propylene and aromatics by converting methanol and/or dimethyl ether

A technology of fluidized bed reaction and dimethyl ether, applied in chemical instruments and methods, hydrocarbon production from oxygen-containing organic compounds, physical/chemical process catalysts, etc., can solve the problems of low yields of ethylene, propylene and aromatics, and achieve Effects of reducing diffusion effects, promoting contact, and improving mass transfer efficiency

Active Publication Date: 2016-09-07
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0012] One of the technical problems to be solved by the present invention is the technical problem of low yields of ethylene, propylene and aromatics in the prior art, providing a coaxial fluidized bed for converting methanol and / or dimethyl ether into ethylene, propylene and aromatics response system

Method used

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  • Coaxial fluidized bed reaction system and reaction method for producing ethylene, propylene and aromatics by converting methanol and/or dimethyl ether
  • Coaxial fluidized bed reaction system and reaction method for producing ethylene, propylene and aromatics by converting methanol and/or dimethyl ether

Examples

Experimental program
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Effect test

Embodiment 1

[0051] use as figure 1 device shown. The diameter of the reaction section of the reactor is 1.5 meters, and its height accounts for 80% of the total height of the reactor. The ratio of the diameter of the dilute phase section to the diameter of the reaction section is 2:1, and its height accounts for 15% of the total height of the reactor. The height of the external heat extractor of the reactor accounts for 85% of the height of the reactor. The height of the external heat receiver of the regenerator accounts for 70% of the height of the regenerator.

[0052] The reaction conditions of the reactor are: the temperature is 480° C., the reaction pressure in gauge pressure is 0.2 MPa, the weight space velocity is 2 (g / h) / g catalyst, and the mass ratio of the catalyst circulation amount to the raw material feed amount is 12 : 1, the catalyst density of the reaction zone in the reactor is 100 kg / m 3 , The average superficial gas velocity is 0.2 m / s. The regenerator temperature w...

Embodiment 2

[0057] use as figure 1 device shown. The diameter of the reaction section of the reactor is 5 meters, and its height accounts for 60% of the total height of the reactor. The ratio of the diameter of the dilute phase section to the diameter of the reaction section is 1.1:1, and its height accounts for 35% of the total height of the reactor. The height of the external heat extractor of the reactor accounts for 95% of the height of the reactor. The height of the external heat receiver of the regenerator accounts for 30% of the height of the regenerator.

[0058] The reaction condition of reactor is: temperature is 400 ℃, and gauge reaction pressure is 0.5 MPa, and weight space velocity is 10 (gram / hour) / gram catalyst, and the mass ratio of catalyst circulation amount and feedstock amount is 3 : 1, the catalyst density of the reaction zone in the reactor is 90 kg / m 3 , The average superficial gas velocity is 0.17 m / s. The temperature of the regenerator was 680°C. The content ...

Embodiment 3

[0063] The device of Example 1 was used.

[0064] The reaction condition of reactor is: temperature is 550 ℃, and with gauge pressure gauge reaction pressure is 0 MPa, and weight space velocity is 10 (gram / hour) / gram catalyst, and the mass ratio of catalyst circulation amount and raw material feeding amount is 30 : 1, the catalyst density of the reaction zone in the reactor is 50 kg / m 3 , with an average superficial air velocity of 1 m / s. The temperature of the regenerator was 580°C. The content of char on the regenerated catalyst is 0.09% by weight based on the mass percentage of the catalyst. Using methanol as a raw material, the water content is 0.01% by weight. The height of the external heat extractor of the reactor accounts for 30% of the height of the reactor. The height of the external heat receiver of the regenerator accounts for 60% of the height of the regenerator.

[0065] The stripping medium is water vapor. The lifting medium is N 2 . The regeneration mediu...

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Abstract

The invention relates to a coaxial fluidized bed reaction system and a reaction method for preparing ethylene, propylene and arene by converting methanol and / or dimethyl ether, and aims at solving the problem of low yield of ethylene, propylene and arene in the prior art. The problem can be solved well by adopting the technical scheme that the system comprises a reactor (1), a regenerator (2) and a stripper (3), wherein raw materials (15) enter the reactor (1) through the lower part of a reaction section (24) of the reactor to be contacted and reacted with a catalyst; the reacted catalyst with carbon deposit enters an inclined regenerating tube (7) connected with the bottom part of the reactor (1) and then is lifted to the stripper (3) through a vertical stripping tube (8); the catalyst subjected to stripping is regenerated through the regenerator (2), and the regenerated catalyst is degassed through a degassing tank (4) and then downwards moves to reach the reaction section (24) of the reactor. The system can be applied to the industrial production of ethylene, propylene and arene.

Description

technical field [0001] The invention relates to a coaxial fluidized bed reaction system and method for converting methanol and / or dimethyl ether to produce ethylene, propylene and aromatics. Background technique [0002] Ethylene, propylene and aromatics (especially triphenyl, Benzene, Toluene, Xylene, or BTX) are important basic raw materials for organic synthesis. Driven by the demand for downstream derivatives, the market demand for ethylene, propylene and aromatics continues to grow. [0003] The steam cracking process using liquid hydrocarbons (such as naphtha, diesel, secondary processed oil) as raw material is the main production process of ethylene, propylene and aromatics. This process belongs to the production technology of petroleum route. In recent years, due to the limited supply and high price of petroleum resources, the cost of raw materials has been increasing. Due to these factors, the technology of producing ethylene, propylene and aromatics from alternat...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C07C1/20C07C11/06C07C11/04C07C15/04C07C15/06C07C15/08B01J29/46B01J29/80B01J29/78
CPCY02P20/52Y02P20/584Y02P30/20Y02P30/40
Inventor 李晓红钟思青齐国祯金永明
Owner CHINA PETROLEUM & CHEM CORP
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