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Double-CFB (circulating fluidized bed) reaction-regeneration system and method to prepare arenes with synthetic gas

A circulating fluidized bed and regeneration system technology, applied in chemical instruments and methods, preparation of liquid hydrocarbon mixtures, biological raw materials, etc., can solve problems such as low conversion rate of synthesis gas and regeneration of catalysts, etc., to reduce design difficulty, Reduced back-mixing and cost reduction effects

Active Publication Date: 2018-10-16
TSINGHUA UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

However, at present, such catalysts are restricted by chemical balance, the conversion rate of synthesis gas is not high, and the formation of CO 2 The selectivity is relatively high
At the same time, the catalyst for this process needs to be regenerated at high temperature, and there is no such technical report yet

Method used

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  • Double-CFB (circulating fluidized bed) reaction-regeneration system and method to prepare arenes with synthetic gas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0032] Hydrocarbon synthesis catalyst (iron nitride / aluminum oxide, iron nitride mass fraction is 50%, the rest is aluminum oxide, the average particle diameter of catalyst is 350 microns) and aromatization catalyst (Ga 2 o 3 / Y molecular sieve / alumina type, in which alumina, Y molecular sieve, Ga2 o 3 The mass fractions are 60%, 30%, and 10%, respectively, and the average particle size of the catalyst is 120 microns) are packed in the first catalyst loading area 1a of the aromatization reactor 1 . Preheat the lower area of ​​the aromatization reactor 1 to 250°C, feed synthesis gas (CO and hydrogen), control the pressure at 3MPa, and blow the aromatization catalyst from the first catalyst loading area 1a to the second catalyst loading area In 1b, the temperature of the second catalyst loading zone 1b is controlled to be 550°C.

[0033] The synthesis gas generates hydrocarbons in the first catalyst loading zone 1a, and the hydrocarbons further react in the second catalyst loa...

Embodiment 2

[0038] Hydrocarbon synthesis catalyst (Fe / Cr / alumina catalyst, alumina, Fe, Cr mass fraction are respectively 5%, 20%, 75%, the average particle diameter of catalyst is 200 microns) and aromatization catalyst (ZnO / Ga 2 o 3 / ZSM-5 / alumina, of which alumina, ZSM-5 molecular sieve, Ga 2 o 3 , ZnO mass fractions are 50%, 35%, 5%, 10% respectively, and the average particle diameter of the catalyst is 40 micrometers) are packed in the first catalyst loading area 1a area in the reactor. The lower area of ​​the reactor was preheated to 380°C, and the synthesis gas (CO and hydrogen) was introduced to control the pressure at 2MPa. The aromatization catalyst is blown from the first catalyst loading area 1a into the second catalyst loading area 1b, and the temperature of the second catalyst loading area 1b is controlled to be 450°C.

[0039] The synthesis gas generates hydrocarbons in the first catalyst loading zone 1a, and the hydrocarbons further react in the second catalyst loadin...

Embodiment 3

[0044] The hydrocarbon synthesis catalyst (Co / Mn / alumina / silicon oxide catalyst (Co, Mn, alumina, silica mass fraction is 0.6%, 0.4%, 70%, 29%, the average particle diameter of catalyst is 270- Micron) and aromatization catalyst (MoO 3 / Fe / β molecular sieve / alumina, of which alumina, β molecular sieve, MoO 3 , Fe mass fractions are 58%, 36%, 3%, 3%, respectively, and the average particle diameter of the catalyst is 80 micrometers) are packed in the first catalyst packing area 1a area in the reactor. The lower area of ​​the reactor was preheated to 280°C, and the synthesis gas (CO and hydrogen) was introduced to control the pressure at 0.1MPa. The aromatization catalyst is blown from the first catalyst loading area 1a into the second catalyst loading area 1b, and the temperature of the second catalyst loading area 1b is controlled to be 480°C.

[0045] The synthesis gas generates hydrocarbons in the first catalyst loading zone 1a, and the hydrocarbons further react in the sec...

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Abstract

A double-CFB (circulating fluidized bed) reaction-regeneration system and method to prepare arenes with synthetic gas are provided. The system herein comprises an aromatization reactor and a catalystregeneration reactor which are connected with each other through a pipeline; the aromatization reactor comprises a first catalyst filling area and a second catalyst filling area; the catalyst regeneration reactor includes a fourth catalyst filling area and a third catalyst filling area; the aromatization reactor is filled with a hydrocarbon synthetic catalyst and an aromatization catalyst; under the action of a flow of gas, the hydrocarbon synthetic catalyst stays mainly in the area below, and the aromatization catalyst stays mainly in the area above. A regeneration method is also disclosed, including: after the aromatization catalyst is inactive, allowing the aromatization catalyst to enter a low-temperature hypoxic area of the catalyst regeneration reactor and then enter a high-temperature hyperoxic area of the catalyst regeneration reactor. The system and method herein have the advantages that controlling at different temperatures is achieved and catalyst design is less difficult.

Description

technical field [0001] The invention relates to the technical field of chemical processes and equipment, in particular to a two-stage circulating fluidized bed reaction-regeneration system and method for preparing aromatics from synthesis gas. Background technique [0002] The synthesis gas aromatization technology is an emerging aromatics production process, one of which is to form hydrocarbon intermediates in the synthesis gas first, and then prepare aromatics through hydrocarbons. The obvious advantage of combining the two reactions in one reactor is that there is no need to separate the complex hydrocarbon components and prepare high-purity products, so that the separation units of the two processes that were originally carried out independently can be effectively merge. The technical challenge is that the original catalyst for hydrocarbon synthesis works at 300-380°C, and the catalyst for preparing aromatic hydrocarbons from hydrocarbons works at 350-500°C. At present...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): B01J8/26B01J8/18C10G3/00
CPCB01J8/1809B01J8/1845B01J8/26C10G3/57C10G3/62C10G2300/70Y02P30/20
Inventor 骞伟中宋文龙侯一林陈兆辉
Owner TSINGHUA UNIV
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