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Catalytic conversion method for preparing propylene and aromatic hydrocarbons

A catalytic conversion method and propylene technology, applied in the purification/separation of hydrocarbons, chemical instruments and methods, hydrocarbon cracking and hydrocarbon production, etc., can solve the problems of low yield of propylene and aromatics, increase of dry gas and coke yield, etc.

Active Publication Date: 2009-09-16
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0012] The above-mentioned prior art still has deficiencies in the design of the molecular cracking reaction of alkanes in the feedstock oil, and the cracking reaction of other hydrocarbon molecules in the feedstock is excessive, resulting in a substantial increase in the yield of dry gas and coke. At the same time, the product distribution of the prior art It is cut according to the conventional FCC fractionation system, the potential content of aromatics and low-carbon olefins in gasoline or diesel oil is not fully utilized, resulting in low yields of propylene and aromatics

Method used

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  • Catalytic conversion method for preparing propylene and aromatic hydrocarbons
  • Catalytic conversion method for preparing propylene and aromatic hydrocarbons

Examples

Experimental program
Comparison scheme
Effect test

Embodiment approach 1

[0044] The preferred technical solution of this embodiment comprises the following steps:

[0045] (1) The raw material of type 3 is first contacted with the thermally regenerated catalyst at a reaction temperature of 650°C-800°C and a weight hourly space velocity of 100h -1 -800h -1 , the reaction pressure is 0.10MPa-1.0MPa (absolute pressure), the weight ratio of catalytic cracking catalyst and raw material is 30-150, and the weight ratio of water vapor and raw material is 0.05-1.0 to carry out the cracking reaction;

[0046] (2) The reaction effluent is mixed with the type 2 raw material without oil separation, and the type 2 raw material is mixed at a reaction temperature of 550°C-720°C and a weight hourly space velocity of 10h -1 -300h -1 , the reaction pressure is 0.10MPa-1.0MPa (absolute pressure), the weight ratio of the catalytic cracking catalyst to the raw material is 10-100, and the weight ratio of water vapor to the raw material is 0.05-1.0 to carry out the crac...

Embodiment approach 2

[0053] The preferred technical solution of this embodiment comprises the following steps:

[0054] (1) The raw material of type 3 is first contacted with the thermally regenerated catalyst at a reaction temperature of 650°C-800°C and a weight hourly space velocity of 100h -1 -800h -1 , the reaction pressure is 0.10MPa-1.0MPa (absolute pressure), the weight ratio of catalytic cracking catalyst and raw material is 30-150, and the weight ratio of water vapor and raw material is 0.05-1.0 to carry out the cracking reaction;

[0055] (2) The reaction effluent is mixed with the type 2 raw material without oil separation, and the type 2 raw material is at a reaction temperature of 550°C-720°C, a weight hourly space velocity of 10h-1-300h-1, and a reaction pressure of 0.10MPa-1.0MPa (absolute pressure), the weight ratio of catalytic cracking catalyst and raw material is 10-100, and the cracking reaction is carried out under the condition that the weight ratio of steam and raw material...

Embodiment 1

[0113] This example follows figure 1 process to test. The total height of the pre-lift section, the first reaction zone, the second reaction zone and the third reaction zone of the variable-diameter riser reactor of this process is 21 meters, the diameter of the pre-lift section is 0.25 meters, and its height is 1.5 meters; The first reaction zone has a diameter of 0.25 meters and a height of 3.5 meters; the second reaction zone has a diameter of 0.5 meters and a height of 7 meters; the third reaction zone has a diameter of 1 meter and a height of 9 meters; the first and second reaction zones The longitudinal section of the junction and the junction of the second and third reaction zones etc. should have a trapezoidal apex angle of 45 degrees.

[0114] Feedstock A is directly used as the raw material for catalytic cracking, and the test is carried out on a medium-sized device with a riser reactor. Light aromatics raffinate and C 3 -C 5 Hydrocarbons enter the bottom of reac...

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Abstract

A catalytic conversion method for preparing propylene and aromatic hydrocarbons comprises the following steps: hydrocarbon raw materials with different cracking performances are contacted with a catalytic cracking catalyst to carry out cracking reaction in a fluidized-bed reactor under the conditions that the temperature is 450-750 DEG C, the weight hourly space velocity is 0.1-800h<-1>, the reaction pressure is 0.10-1.0MPa, the weight ratio of the catalytic cracking catalyst to the raw materials is 1-150 and the weight ratio of water vapor to the raw materials is 0.05-1.0, the spent catalyst and reaction oil and gas are separated, the spent catalyst returns to the reactor after the regeneration, the separated reaction oil and gas are separated to obtain target products of low-carbon olefins, aromatic hydrocarbons and the raw materials for re-cracking, wherein the raw materials for re-cracking are re-cracked after hydrotreating. The method can product the propylene and other low-carbon olefins from the heavy raw materials to the maximum extent, wherein the yield of the propylene is more than 40 percent by weight; meanwhile, the method can co-produce toluene, xylene and other aromatic hydrocarbons, and the yield of the dry gas is unexpectedly reduced by more than 80 percent by weight.

Description

technical field [0001] The invention belongs to a method for catalytic conversion of hydrocarbon oil, more specifically, a method for converting heavy raw materials into low-carbon olefins and aromatics rich in propylene by combining the catalytic cracking and hydrotreating processes of hydrocarbon oil. Background technique [0002] Low-carbon olefins such as ethylene and propylene are important organic chemical raw materials, among which propylene is a synthetic monomer for products such as polypropylene and acrylonitrile. With the rapid growth of demand for derivatives such as polypropylene, the demand for propylene is also increasing year by year. The demand in the world propylene market has increased from 15.2 million tons 20 years ago to 51.2 million tons in 2000, with an average annual growth rate of 6.3%. It is estimated that the demand for propylene will reach 86 million tons by 2010, with an average annual growth rate of about 5.6%. [0003] The methods for produc...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C4/06C07C7/00C07C11/06C07C15/00C10G47/02
Inventor 许友好谢朝钢戴立顺崔守业鲁维民张久顺龙军达志坚聂红郭锦标田松柏田辉平汪燮卿舒兴田何鸣元李大东
Owner CHINA PETROLEUM & CHEM CORP
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