Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking

A cracking reaction and reactor technology, applied in the direction of hydrocarbons, hydrocarbons, hydrocarbon cracking and hydrocarbon production, etc., can solve the problems of poor selectivity and low conversion rate of ethylene and propylene, and achieve the effect of catalytic cracking

Pending Publication Date: 2020-09-29
SHANGHAI SUPEZET ENG TECH CO LTD +4
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] Olefins above C4 are easily converted into propylene or ethylene + propylene by catalytic cracking on HZSM-5 molecular sieves; under the same conditions, alkanes in propane, n-butane and naphtha fractions hardly react, even if the reaction temperature When it comes to 700℃, the conversion rate is not high, and the selectivity of ethylene and propylene is not good.

Method used

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  • Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking
  • Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking
  • Combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking

Examples

Experimental program
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Effect test

Embodiment 1

[0070] as attached figure 1 , figure 2 As shown, the reaction unit for the alkane catalytic dehydrogenation-cracking olefins provided by the application is used in conjunction with the catalyst regeneration unit. These two sets of devices can be used separately and used in conjunction with other reaction devices or catalyst regeneration devices of the prior art respectively.

[0071] like figure 1 , 2 The reaction device for catalytic dehydrogenation-cracking of alkane to produce olefins includes a reactor for catalytic dehydrogenation-cracking and a settling section 7 of the reactor. The settling section of the reactor is located at the upper part of the reactor, wherein the reactor includes Hydrogen reaction section 2 and cracking reaction section, cracking reaction section includes dense phase section 3 and dilute phase section 5, dehydrogenation reaction section 2 is positioned at the bottom of cracking reaction section, dehydrogenation reaction section 2 part stretche...

Embodiment 2

[0088] Others are the same as in Example 1, only the catalytic cracking reactor is changed into a straight tube reactor. The average superficial gas velocity and average residence time in the pyrolysis reaction zone are 10m / s and 5.5s, respectively. From the results listed in Table 2, it can be seen that the single-pass conversion rate of n-butane cracking is slightly reduced by using the straight pipe cracking reaction zone, and the selectivity of ethylene+propylene is slightly reduced, but after including ethane, propane and C4+ circulation From the point of view of the total product distribution, the yield of ethylene+propylene to fresh n-butane is still above 76%.

[0089] Table 2. The product distribution of n-butane and ethane in one pass and the product distribution of ethane, propane and C4+ after full recovery, wt%

[0090]

Embodiment 3

[0092] Others are the same as in Example 1, except that the n-butane raw material is changed into naphtha whose composition is shown in 3. The yield of naphtha catalytic cracking ethylene+propylene alone is 52.2wt%. Catalytic cracking of naphtha produces less ethane and propane, less than 3 percent. After recycling ethane and propane, the total ethylene + propylene increased by more than 2 percent.

[0093] Table 3. Naphtha composition, wt%

[0094]

[0095] Table 4. Naphtha catalytic cracking product distribution, wt%

[0096]

[0097]

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PUM

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Abstract

The invention relates to a combined reactor for preparing olefin by alkane dehydrogenation and hydrocarbon catalytic cracking. The reactor for preparing olefin by catalytic dehydrogenation-cracking ofalkane comprises a catalytic dehydrogenation-cracking reactor and a reactor settling section, the reactor settling section is located at the upper part of the reactor, the reactor comprises a dehydrogenation reaction section and a cracking reaction section, the dehydrogenation reaction section is located below the cracking reaction section, and one end of a catalyst regeneration inclined pipe isconnected with the dehydrogenation reaction section. The method is beneficial to dehydrogenation reaction and catalytic cracking reaction.

Description

technical field [0001] The application relates to a reaction device for catalytic dehydrogenation and cracking of alkanes, more specifically, a combined reaction device for preparing ethylene and propylene by dehydrogenation of ethane and propane and catalytic cracking of hydrocarbons, which belongs to the field of petrochemical industry. Background technique [0002] Ethane dehydrogenation to ethylene has been one of the research hotspots for many years. Limited by thermodynamic equilibrium, under the typical reaction conditions of propane and butane dehydrogenation, the single-pass conversion rate of ethane is very low, which has almost no value for industrial application. [0003] Industrially, the steam cracking route has been adopted for the production of ethylene from ethane, that is, ethane is converted into ethylene by thermal reaction at about 850°C and a certain water vapor partial pressure. Ethane thermally reacts under high temperature conditions, in addition to...

Claims

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Application Information

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IPC IPC(8): B01J8/00B01J8/18C07C5/333C07C4/06C07C11/04C07C11/06
CPCB01J8/00B01J8/008B01J8/18C07C5/333C07C4/06C07C11/04C07C11/06Y02P20/584
Inventor 李春义李康王国玮庞春天张凌云
Owner SHANGHAI SUPEZET ENG TECH CO LTD
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