Hydrocarbon catalytic converting method with high butene and light arene yields

A catalytic conversion method and light aromatic hydrocarbon technology are applied in the field of catalytic conversion of hydrocarbons that produce butene and light aromatic hydrocarbons, can solve the problem of low yield of butene and/or light aromatic hydrocarbons, etc., achieve suppression of hydrogen transfer reaction, and flexible process. High-quality, high-yield effects

Active Publication Date: 2017-05-03
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The purpose of the present invention is to overcome the defect that the yield of butene and / or light aromatics is not high in the existing process of producing light olefins and light aromatics by catalytic cracking of heavy hydrocarbon raw materials, and to provide a kind of high-yielding butene Process for catalytic conversion of alkenes and light aromatics to hydrocarbons

Method used

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  • Hydrocarbon catalytic converting method with high butene and light arene yields
  • Hydrocarbon catalytic converting method with high butene and light arene yields
  • Hydrocarbon catalytic converting method with high butene and light arene yields

Examples

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Effect test

Embodiment 1

[0093] The cracking catalyst used in the present embodiment is: based on the total weight of the cracking catalyst, the cracking catalyst used contains 10% by weight of zeolite beta, 20% by weight of ZSM-5 zeolite (the ratio of silicon to aluminum is 40), 45% by weight of Kaolin and 25% by weight of alumina binder, wherein the beta zeolite contains 1% by weight of iron and 1.5% by weight of phosphorus in terms of elements. The cracking catalyst was aged for 10 hours at 800° C. under a 100% steam atmosphere, and the catalyst loading in the device (system catalyst inventory) was 60 kg.

[0094] The heavy hydrocarbon feedstock (its properties are shown in Table 1) is introduced into the riser reactor 1, and after contacting and reacting with the hot catalyst from the regenerator 7, the reaction oil gas is separated from the catalyst, and the reaction oil gas leaves the reactor and is introduced into the fractionation device, separated The obtained coke catalyst is introduced into t...

Embodiment 2

[0096] The process flow and the cracking catalyst used in this example are the same as those in Example 1, except that the light cracked gasoline (see Table 2 for properties) is used at a reaction temperature of 40°C, a reaction pressure of 0.5MPa, and a molar ratio of hydrogen to olefins of 4:1. , on the hydrogenation catalyst (purchased from Sinopec Changling Catalyst Branch, the brand is RDD-1), through selective hydrogenation reaction, the diolefins and alkynes are converted into monoolefins and introduced into the riser reactor 2, and the remaining reaction conditions And the reaction results are shown in Table 4.

Embodiment 3

[0100] The flow process of this embodiment is the same as Example 1, and the difference is that the cracking catalyst used is: based on the total weight of the cracking catalyst, the cracking catalyst used contains 15% by weight of zeolite beta, 15% by weight of ZSM-5 zeolite (silicon Aluminum ratio is 40), 45% by weight of kaolin and 25% by weight of alumina binder, wherein, zeolite beta contains 1% by weight of iron and 1.5% by weight of phosphorus in terms of elements; and reaction conditions and reaction results See Table 6.

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Abstract

The invention relates to the catalytic cracking field of heavy hydrocarbon class raw materials and particularly discloses a hydrocarbon catalytic converting method with high butene and light arene yields. The method comprises the following steps: 1, enabling a heavy hydrocarbon class raw material to carry out contact reaction with a first cracking catalyst in a first reactor, and then carrying out separation so as to obtain a first carbon depositing catalyst and a first reaction product; 2, enabling light cracked gasoline of which the final boiling point does not exceed 90DEG C to carry out contact reaction with a second cracking catalyst in a second reactor; and 3, directly guiding a reaction mixture which is obtained through reaction in the second reactor into a third reactor without separating the reaction mixture, enabling the reaction mixture to carry out contact reaction with hydrogenation modified cracked light oil of which the boiling range is between 200DEG C and 390DEG C, and then carrying out separation so as to obtain a second carbon depositing catalyst and a second reaction product, wherein the hydrogenation modified cracked light oil is prepared by carrying out hydrogenation treatment on the cracked light oil. High butene yield and high light arene yield can be obtained by the method provided by the invention.

Description

technical field [0001] The invention relates to a hydrocarbon catalytic conversion method that can produce more butene and light aromatic hydrocarbons. Background technique [0002] Butene and light aromatics (benzene, toluene and xylene, referred to as BTX) are basic chemical raw materials. At present, butene mainly comes from MTO, butane, LPG, condensate oil, naphtha, hydrocracking tail oil and crude oil Steam thermal cracking of diesel oil and catalytic cracking of hydrocarbon oil, BTX mainly comes from light hydrocarbon reforming process and steam thermal cracking process. As steam cracking adopts new light raw materials, product distribution will change. For example, when ethane is used as steam cracking raw material, compared with naphtha as raw material, the proportion of ethylene in the product is significantly increased, while butene and light aromatics yield will decrease. In this context, the use of heavy hydrocarbon oil catalytic conversion to produce butene an...

Claims

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Application Information

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IPC IPC(8): C10G55/06
CPCC10G55/06C10G2400/20C10G2400/30
Inventor 朱根权谢朝钢成晓洁杨超沙有鑫孙益群
Owner CHINA PETROLEUM & CHEM CORP
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