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Method for producing aromatic hydrocarbons and/or liquid fuels from light hydrocarbons

A liquid fuel and light hydrocarbon technology, applied in chemical instruments and methods, liquid hydrocarbon mixture production, bulk chemical production, etc., can solve the problems of easy catalyst deactivation, low carbon utilization rate, catalyst deactivation, etc., and achieve process design Simple operation, high carbon utilization rate, long catalyst life effect

Active Publication Date: 2021-10-12
CHNA ENERGY INVESTMENT CORP LTD +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] The purpose of the present invention is to provide a new dehydroaromatization method for light hydrocarbons to overcome the problems of low yield of aromatics, low carbon utilization rate, and easy deactivation of catalysts in the process of converting light hydrocarbons into aromatics in the prior art. A method for producing aromatics, through which a higher yield of aromatics and carbon utilization can be obtained, and problems such as catalyst deactivation can be effectively solved, so that the service life of the catalyst is greatly extended

Method used

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  • Method for producing aromatic hydrocarbons and/or liquid fuels from light hydrocarbons
  • Method for producing aromatic hydrocarbons and/or liquid fuels from light hydrocarbons
  • Method for producing aromatic hydrocarbons and/or liquid fuels from light hydrocarbons

Examples

Experimental program
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Effect test

Embodiment 1

[0074] use figure 1 The process shown, the volume ratio of 1.67:1 C 2 h 6 / N 2 The mixed gas is sent to the two reactors of dehydrogenation and oligomerization / aromatization in series, the dehydrogenation temperature is set at 750°C, and the GHSV of ethane is 1000h -1 , the pressure is normal pressure, and the reaction is carried out without a catalyst. Under these conditions, the conversion of ethane was about 57%, and the concentration of ethylene in the dehydrogenation product gas stream was about 22% by volume. The set temperatures of oligomerization / aromatization fixed bed reactors are 400°C, 450°C, 500°C and 550°C respectively, WHSV=2.68g-C 2 h 6 / g-cat·hr (equivalent to 1.6g-C 2 h 4 / g-cat·hr), the pressure is normal pressure (1 bar), the catalyst is Ga / ZSM-5 / Al prepared by saturated impregnation method 2 o 3 Catalyst (the content of Ga is 2.0% by weight, and the silicon-aluminum mol ratio of ZSM-5 is 30, and molecular sieve and binder Al 2 o 3 The weight rat...

Embodiment 2

[0091] Different from the method of Example 1, use the mixture gas stream that is formulated according to the product composition of step 1) in Example 1, and its composition and volume ratio are C 2 h 4 / H 2 / N 2 =1:1:1. The catalyst is the same as the catalyst for oligomerization / aromatization in Example 1, that is, Ga / ZSM-5 / Al prepared by saturated impregnation method 2 o 3 Catalyst (the content of Ga is 2.0% by weight, and the silicon-aluminum mol ratio of ZSM-5 is 30, and molecular sieve and binder Al 2 o 3 The weight ratio is 82.5 / 17.5). The conditions of aromatization are 450°C and 550°C, normal pressure, WHSV=0.75g-C 2 h 4 / g-cat·hr, the reaction time is 6 hours. The results of the 6-hour average BTX yield and product selectivity calculated on the basis of ethylene are shown in Table 2.

Embodiment 4

[0095] The experiment was carried out according to the method of Example 2, except that the catalyst used for ethylene aromatization was ZSM-5 containing 1% nickel by the total weight of molecular sieves (ZSM-5 was the same as in Example 1). The average results of the reaction at 450°C for 6 hours are shown in Table 2.

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Abstract

The invention provides a method for producing aromatic hydrocarbons and / or liquid fuels through light hydrocarbon dehydrogenation aromatization, which comprises the following steps: 1) under dehydrogenation reaction conditions, carrying out dehydrogenation reaction on light hydrocarbon material flow to obtain material flow containing olefin; and 2) under aromatization reaction conditions, contacting the material flow containing olefin with an aromatization catalyst, and carrying out oligomerization / aromatization reaction to obtain a material flow containing aromatic hydrocarbon and / or liquid fuel. According to the method, dehydrogenation and oligomerization / aromatization are separated and executed step by step under different conditions, a zeolite molecular sieve loaded with an active metal component is used as an aromatization catalyst, and under an optimal low-temperature aromatization condition, the high alkane conversion rate, the high carbon utilization rate and the high single-cycle aromatic hydrocarbon production capacity can be obtained through the method disclosed in the invention; and the catalyst is slow in deactivation, long in one-way service life, easy to regenerate and good in multi-cycle stability.

Description

technical field [0001] The present invention relates to a process for the production of aromatics and / or liquid fuels from light hydrocarbons. Background technique [0002] Since the mid-2000s, the shale gas revolution has led to exponential growth in North American natural gas (NG) and natural gas liquids (NGLs) production. This has directly led to the low prices of NGL components, especially ethane, in recent years. Abundant and low-priced ethane has also led to a shift in ethylene production from traditional naphtha to ethane-based production, and prices have tended to drop as supply continues to increase. On the other hand, the switch from naphtha catalytic reforming to ethane cracking has also left insufficient aromatics production and higher prices. Objectively, there is a big gap with the prices of ethane and ethylene. [0003] The direct conversion of light hydrocarbons to aromatic compounds has long been one of the main interests of academia and industry. Shell ...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G50/00C07C2/84C07C15/04C07C15/06C07C15/08
CPCC10G50/00C07C2/84C07C2529/40C07C15/04C07C15/06C07C15/08C07C15/02C07C2/42Y02P20/52
Inventor 张爱华王辉丽萨·阮单军军乔舒亚·迈尔斯路易斯·吉伦刘华
Owner CHNA ENERGY INVESTMENT CORP LTD
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