Catalytic cracking method and system

Active Publication Date: 2022-01-07
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The raw oil first passes through the first hydrotreating unit to obtain the first hydrogenated tail oil; the first hydrogenated tail oil enters the first catalytic cracking unit, and the catalytic active component of the catalytic cracking unit is mainly large-pore zeolite, Obtain naphtha, diesel oil and heavy oil, wherein the heavy oil enters the second hydrotreating unit for hydrogenation to obtain the second hydrogenated tail oil, and the second hydrogenated tail oil enters the second catalytic cracking unit for cracking. The catalyst active component of catalytic cracking unit is mainly mesoporous zeolite, and the propylene yield of this method is low

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  • Catalytic cracking method and system

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Experimental program
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Embodiment 1

[0117] The test was carried out in a medium-sized catalytic cracking unit. The device includes a set of composite reaction system: downcomer reactor, riser reactor plus fluidized bed combination reactor, hydrogenation reforming reactor and solvent extraction device, the bottom outlet of the downcomer reactor is connected to the fluidized bed reactor bottom. The catalyst used is MMC-2 catalyst, the raw materials shown in Table 1 are cracked, the product and catalyst obtained from the reaction are separated in the settling section, the product enters the separation device for separation, and the catalyst enters the fluidized bed reactor; the top of the riser is fluidized in series Bed reactor, the catalyst that adopts is MMC-2 catalyst, to the light gasoline (distillation range is 30-85 ℃, olefin content is 52%, weight accounts for 15% of heavy feedstock) rich in olefins from the product separation unit, Hydrogenated diesel oil (distillation range 204-350°C, weight accounted fo...

Embodiment 2

[0121] Referring to Example 1, the difference is that the weight of hydro-upgraded diesel oil increases from 10% to 18% of the heavy feedstock, and the weight of hydro-upgraded oil slurry increases from 3% to 5% of the heavy feedstock. Its reaction operating conditions and reaction results are shown in Table 3 and Table 4.

[0122] It can be seen from Table 3 and Table 4 that, compared with the comparative example in which there is no downcomer reactor, hydrogenation upgrading reactor, and solvent extraction device, embodiment 1 increases the downcomer reactor and increases the hydrogenation upgrading reaction Device and solvent extraction unit, the reduction of diesel yield indicates that more diesel is converted into low-carbon olefins, and the increase of cetane number of diesel oil indicates that the quality of diesel oil is improved; at the same time, the yield of low-carbon olefins increases significantly, and benzene, toluene and C8 are recovered Aromatics and other pro...

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Abstract

The invention relates to a catalytic cracking method and a system. The catalytic cracking method comprises a combined process of catalytic cracking, hydro-upgrading and aromatic hydrocarbon extraction. According to the process, benzene, methylbenzene and xylene can be co-produced while low-carbon olefin is produced to the maximum extent, and product distribution is optimized.

Description

technical field [0001] The invention relates to a method and system for producing light olefins and aromatics by catalytic cracking. Background technique [0002] Small molecule olefins such as ethylene, propylene and butene are the most basic raw materials for organic synthesis. At present, the main production process of small molecular olefins in the world is steam cracking process, but the high temperature cracking furnace is easy to coke, so this process basically uses light oil as raw material, such as natural gas, naphtha, light diesel oil, and hydrogenation can also be used Cracking tail oil is used as raw material. At present, the trend of heavy and inferior crude oil in my country is becoming more and more obvious, the yield of light oil such as naphtha is getting lower, and the contradiction between supply and demand of raw materials for steam cracking process and catalytic reforming process is becoming more and more serious. Since the mid-1980s, Sinopec Research...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G11/18
CPCC10G11/18C10G2400/20C10G2400/30C10G2300/1037
Inventor 沙有鑫龚剑洪魏晓丽李泽坤
Owner CHINA PETROLEUM & CHEM CORP
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