Method for producing aromatic hydrocarbon through light hydrocarbon dehydrogenation aromatization

A dehydroaromatization and aromatization technology, which is applied in the production of bulk chemicals, chemical instruments and methods, hydrocarbons, etc., can solve the problems of prolonging the service life of catalysts, easy deactivation of catalysts, and low yield of aromatics , to achieve slow catalyst deactivation, high liquid aromatics yield, and high alkane conversion

Active Publication Date: 2021-05-25
CHNA ENERGY INVESTMENT CORP LTD +1
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  • Description
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  • Application Information

AI Technical Summary

Benefits of technology

The technical effect that this new technology solves lies within its original design for improving efficiency when converting heavy naptha into lighter ones through various methods such as crackers or fluidized bed reactors (FBR). This allows it to produce more valuable products while minimizing any negative side reactions caused during processing.

Problems solved by technology

Technological Problem addressed in this patents relates to improving the performance of certain types of molecular sieves (zones) made up mainly of alkanes like ethanols produced during oil refining processes. These molecules can cause unwanted side effects including reduced yields caused by reducing specificity towards desired compounds while increasing costs associated with their manufacture. To address this problem, researchers explored different methods involving modifying existing materials through imitation techniques called metal transfer catalytic systems.

Method used

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  • Method for producing aromatic hydrocarbon through light hydrocarbon dehydrogenation aromatization
  • Method for producing aromatic hydrocarbon through light hydrocarbon dehydrogenation aromatization
  • Method for producing aromatic hydrocarbon through light hydrocarbon dehydrogenation aromatization

Examples

Experimental program
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Effect test

Embodiment 1

[0048] use figure 1 In the process shown, pure ethane was used as feed. The dehydrogenation temperature is set at 750°C, and the GHSV of ethane is 1000h -1 , the pressure is normal pressure, and the catalyst is Pt / Al with a Pt loading of 0.05% by weight 2 o 3 . The dehydrogenation product stream (with an ethylene content of 35% by volume) all went to a series of oligomerization / aromatization fixed bed reactors. The set temperature of the oligomerization / aromatization fixed-bed reactor is 630°C, the pressure is normal pressure, and the catalyst is ZSM-5 / Al 2 o 3 (The silicon-aluminum molar ratio of ZSM-5 is 80, molecular sieve and binder Al 2 o 3 The weight ratio is 70 / 30). Due to the accumulation of coke on the zeolite catalyst, every 10 hours at 2 The gas (the balance is nitrogen) is regenerated at 550°C. The single-pass reaction (excluding cycle) results after continuous reaction for 60 and 600 minutes are shown in Table 1 below.

Embodiment 2

[0052] A mixed gas of 10% by volume of methane and 90% by volume of ethane was used as a feed. The dehydrogenation temperature is set at 650°C, and the GHSV of the mixed gas is 800h -1 , the pressure is normal pressure, and the catalyst is Pt / Al with a Pt loading of 0.2 wt%. 2 o 3 . The dehydrogenation product stream (which has an ethylene content of 22% by volume) all goes to a series of aromatization fixed-bed reactors. The set temperature of the oligomerization / aromatization reactor is 550°C, the pressure is normal pressure, and the catalyst is ZSM-35 / SiO 2 , the silicon-aluminum molar ratio of ZSM-35 is 50, ZSM-35 / SiO 2 The weight ratio is 50:50. Due to the accumulation of coke on the zeolite catalyst, every 10 hours at 2 The gas (the balance is nitrogen) is regenerated at 600°C. The single-pass reaction (not including cycle) results after continuous reaction for 60 minutes and 600 minutes are shown in Table 1.

Embodiment 3

[0054] A mixed gas of 5% by volume of methane and 95% by volume of ethane was used as a feed. The dehydrogenation temperature is set at 850°C, and the GHSV of the mixed gas is 2000h -1 , the pressure is normal pressure, the catalyst is Pt / Al with a Pt loading of 0.15% by weight 2 o 3 . The dehydrogenation product stream (with an ethylene content of 45% by volume) all went to a series of aromatization fixed bed reactors. The set temperature of the oligomerization / aromatization reactor is 600°C, the pressure is normal pressure, and the catalyst is ZSM-11 / SiO 2 , the silicon-aluminum molar ratio of ZSM-11 is 30, ZSM-11 / SiO 2 The weight ratio is 30:70. The single-pass reaction (not including cycle) results after continuous reaction for 60 minutes and 600 hours are shown in Table 1.

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Abstract

The invention provides a method for producing aromatic hydrocarbon by light hydrocarbon dehydrogenation aromatization. The method comprises the following steps: 1) under dehydrogenation reaction conditions, carrying out dehydrogenation reaction on a light hydrocarbon material flow to obtain a material flow containing olefin; and 2) under aromatization reaction conditions, contacting the olefin-containing material flow with an aromatization catalyst, and carrying out an oligomerization/aromatization reaction to obtain an aromatic hydrocarbon-containing material flow. The thinking set that a bifunctional catalyst is used in the prior art is broken through, dehydrogenation and oligomerization/aromatization are separated, different conditions are used for executing in steps, and the following effects are achieved: 1) light hydrocarbon conversion can be independently controlled by changing the conditions of a dehydrogenation zone so as to realize minimum inactivation; and 2) the product selectivity can be independently controlled in oligomerization/aromatization, and the lowest methane selectivity and reverse reaction are achieved. The method has the advantages of high alkane conversion rate, high liquid aromatic hydrocarbon yield, slow catalyst deactivation and easy regeneration of the catalyst.

Description

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Claims

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Application Information

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Owner CHNA ENERGY INVESTMENT CORP LTD
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