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Method and device for preparing aromatic hydrocarbons from syngas

A technology for synthesis gas and aromatic hydrocarbons, applied in the chemical industry, can solve the problems of low olefin yield, long reaction process, complicated preparation method of aromatic hydrocarbons, etc., and achieve the effects of low olefin content, process reduction, and process adaptability enhancement.

Active Publication Date: 2019-07-12
TSINGHUA UNIV
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0006] In order to overcome the problems of the above-mentioned complex preparation method of aromatics, too long reaction process, or too low yield of olefins, the object of the present invention is to provide a method and device for preparing aromatics by utilizing synthesis gas

Method used

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  • Method and device for preparing aromatic hydrocarbons from syngas
  • Method and device for preparing aromatic hydrocarbons from syngas
  • Method and device for preparing aromatic hydrocarbons from syngas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0025] use figure 1 Shown reaction device, first section reaction zone 3 and second section reaction zone 4 are the reactor of fixed bed, and catalyst (50%Fe-30%Zn-20%Na 2 O) placed in the first stage of reaction zone 3, the catalyst (ZSM-5) is placed in the second stage of reaction zone 4. A perforated plate 5 is arranged between the two sections so that the catalysts in the two sections are not exchanged or mixed.

[0026] Feed H into the first stage reaction zone 3 through the synthesis gas inlet 1 2 Mixed gas with / CO molar ratio of 2:1, at 2MPa, 450℃, volume space velocity of 10000h -1 olefin synthesis reaction. When the CO conversion rate is 90% and the olefin selectivity is 50%, the mixed gas obtained from the outlet of the first-stage reaction zone 3 enters the second-stage reaction zone 4 . At the same time, feed benzene into the second-stage reaction zone through benzene or toluene inlet 2, and control the molar ratio of benzene to total olefins in the mixed gas ...

Embodiment 2

[0028] use figure 2 Shown reaction device adopts the reactor that the first stage reaction zone 3 and the second stage reaction zone 4 are fluidized beds, and the catalyst (20%Ni-20%La-20%Ga-40%K 2 O) packing the first stage reaction zone 3, catalyst (35%ZSM-5-30%Al 2 o 3 -25% SiO2 2 ) device in the second stage reaction zone 4. A valve element 6 is set between the two sections, so that the catalysts in the two sections are not exchanged or mixed.

[0029] Feed H into the first stage reaction zone 3 through the synthesis gas inlet 1 2 Mixed gas with / CO molar ratio of 1:1, at 5MPa, 250℃, and volume space velocity of 500h -1 olefin synthesis reaction. When the CO conversion rate is 50% and the olefin selectivity is 90%, the mixed gas obtained from the outlet of the first-stage reaction zone 3 enters the second-stage reaction zone 4 . At the same time, feed benzene into the second-stage reaction zone 4 through the benzene or toluene inlet 2, and control the molar ratio o...

Embodiment 3

[0031] use figure 2 The shown reaction device adopts the reactor in which the first stage reaction zone 3 and the second stage reaction zone 4 are both moving beds, and the catalyst (15%Co-5%Ag-40%Mn-40%CaO) is placed in the first stage section, the catalyst (30% β molecular sieve-20% ZSM-22-50% Al2 o 3 ) placed in the second paragraph. A valve element 6 is set between the two sections, so that the catalysts in the two sections are not exchanged or mixed.

[0032] Feed H into the first stage reaction zone 3 through the synthesis gas inlet 1 2 Mixed gas with / CO molar ratio of 5:1, at 0.5MPa, 350℃, volume space velocity of 3000h -1 olefin synthesis reaction. When the CO conversion rate is 60% and the olefin selectivity is 75%, the mixed gas obtained from the outlet of the first-stage reaction zone enters into the second-stage reaction zone 4 . At the same time, toluene is introduced into the second stage reaction zone 4 through the benzene or toluene inlet 2, and the mola...

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Abstract

The invention discloses a method and a device for preparing aromatic hydrocarbons from syngas. The preparation method comprises the following steps: a first reaction zone is filled with a catalyst, and the syngas is converted into olefin-based hydrocarbons at a high temperature; and a second reaction zone is filled with another catalyst, benzene / toluene is introduced, and the olefins undergo alkylation reaction at a low temperature in the presence of a large amount of hydrogen and CO2 to make the olefins highly selectively converted into the aromatic hydrocarbons. The preparation method has the characteristics of high conversion rate of the raw material, high yield of the aromatic hydrocarbons, low olefin content and easy separation of outlet gas, low cost, and easiness in amplification. The invention also provides the device for realizing the preparation method.

Description

technical field [0001] The invention belongs to the field of chemical industry, and in particular relates to a method and a device for preparing aromatic hydrocarbons by using synthesis gas. Background technique [0002] Aromatics (benzene, toluene, xylene, trimethylbenzene, tetramethylbenzene, ethylbenzene, etc.) are important organic chemical basic raw materials, and are important raw materials for the production of synthetic resin, synthetic fiber and synthetic rubber. For a long time, the route to prepare aromatics mainly includes naphtha cracking, ethane cracking and methanol catalytic conversion. my country is short of oil resources and highly dependent on imports. Therefore, the direct preparation of aromatics from methanol has recently become a new technology growth point, and the technical level of this route has reached the industrial demonstration level. [0003] However, these technologies all use coal as raw material to synthesize olefins through synthesis gas...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C1/04C07C11/02C07C2/72C07C15/02
CPCC07C1/0435C07C1/044C07C2/72C07C2523/80C07C2523/83C07C2523/86C07C2523/889C07C2523/89C07C2529/40C07C2529/70C07C2529/80C07C11/02C07C15/02
Inventor 骞伟中宋文龙王挥遒
Owner TSINGHUA UNIV
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