A combined hydrotreating-catalytic cracking process that produces more isobutane and light aromatics

A catalytic cracking and combined process technology, which is applied in the direction of hydrotreating process, hydrocarbon oil treatment products, hydrocarbon oil treatment, etc., can solve the problem of reducing the processing capacity and economic benefits of catalytic cracking units, increasing the load of regenerators, and unsatisfactory cracking effects, etc. problems, to achieve the effects of excellent product quality, increased gasoline yield, and reduced coke yield

Active Publication Date: 2022-04-08
CHINA PETROLEUM & CHEM CORP +1
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Problems solved by technology

On the other hand, in order to increase the catalytic cracking conversion rate and light oil yield, the catalytic cracking unit usually circulates heavy cycle oil (HCO) in the catalytic cracking unit itself, but due to the high content of HCO aromatics, the cracking effect is not ideal. A large part of HCO is converted into coke, which increases the regenerator load and reduces the processing capacity and economic benefits of the catalytic cracking unit.

Method used

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  • A combined hydrotreating-catalytic cracking process that produces more isobutane and light aromatics
  • A combined hydrotreating-catalytic cracking process that produces more isobutane and light aromatics
  • A combined hydrotreating-catalytic cracking process that produces more isobutane and light aromatics

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Experimental program
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Effect test

preparation example Construction

[0089] (1) Preparation of silica carrier:

[0090] After 3000 grams of Silica Gel 955 commercial silica gel (the product of Davison Chemical Company in the U.S., containing SiO 99.8% by weight) and 75 grams of scallop powder were mixed uniformly, then mixed with 84 milliliters of nitric acid (concentration 65-68%, analytically pure, Shantou Xilong Chemical Industry Co., Ltd. plant) and 4200 ml of water, and the mixture was kneaded evenly on a twin-screw extruder, and then extruded into a butterfly-shaped strip of ф1.3 mm. After the wet strip was dried at 120°C for 4 hours, it was roasted at 600°C for 3 hours. A silica carrier S is obtained. Adopt BETN 2 Adsorption method analysis, the specific surface area of ​​the carrier is 180m 2 / g, the pore volume is 0.78mL / g.

[0091] (2) Preparation of aromatics deep hydrogenation saturation catalyst:

[0092] Take 200 grams of silicon oxide carrier S, impregnate with 200 milliliters of dilute ammonia solution (10% concentration) co...

Embodiment 1

[0096] use figure 1 In the process flow shown, wax oil raw material I and catalytic cracking light cycle oil (LCO) are mixed and then enter the hydrotreating reactor, and are sequentially mixed with hydrogenation protecting agent A, hydrogenation protecting agent B and hydrotreating agent in the first hydrogenation reaction zone. Hydrodemetallization catalyst D (loading volume ratio: 10:10:80) contact reaction, contact reaction with hydrodesulfurization catalyst E in the second hydrogenation reaction zone, and contact reaction with aromatics deep hydrogenation saturation catalyst F in the third hydrogenation reaction zone Contact reaction, contact reaction with hydrodesulfurization and denitrogenation catalyst H in the fourth hydrogenation reaction zone. The liquid product enters the fractionation system for further separation to obtain hydrogenated naphtha, hydrogenated diesel oil, and hydrogenated tail oil.

[0097] The obtained hydrogenated diesel enters the first cracking...

Embodiment 2

[0101] use figure 1In the process flow shown, the wax oil raw material I and the catalytic cracking heavy cycle oil (HCO) are mixed and then enter the hydroprocessing reactor, and are sequentially mixed with the hydrogenation protection agent A, the hydrogenation protection agent B and the hydrogenation reaction zone in the first hydrogenation reaction zone. Hydrodemetallization catalyst C is contacted (loading volume ratio is 15:10:75) for reaction, and reacts with hydrodesulfurization catalyst E in the second hydrogenation reaction zone, and reacts with aromatics deep hydrogenation saturation catalyst F in the third hydrogenation reaction zone Contact reaction, contact and react with hydrodesulfurization and denitrogenation catalyst H in the fourth hydrogenation reaction zone. The liquid product enters the fractionation system for further separation to obtain hydrogenated naphtha, hydrogenated diesel oil, and hydrogenated tail oil.

[0102] The obtained hydrogenated diesel ...

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Abstract

The present invention relates to a hydrotreating-catalytic cracking combined process method for producing more isobutane and light aromatics, the method comprises: mixing wax oil raw material and catalytic cracking distillate oil and sending them into four hydrotreating reactors In the reaction zone, hydrodemetallization, hydrodesulfurization reaction, aromatics deep hydrogenation saturation reaction and hydrodesulfurization denitrogenation reaction are carried out in sequence, and then separated to obtain gas products, hydrogenated naphtha, hydrogenated diesel oil and hydrogenated tail oil Introduce the gained hydrogenated diesel oil into the first cracking reaction zone of the catalytic cracking reactor to contact with the catalytic cracking catalyst and carry out the first catalytic cracking reaction to obtain the reaction oil agent; introduce the gained hydrogenated tail oil in the second cracking reaction zone with the The reaction oil agent from the first cracking reaction zone contacts and undergoes the second catalytic cracking reaction to obtain reaction products and spent catalyst. The method of the invention enables the catalytic cracking unit to produce more isobutane and light aromatics.

Description

technical field [0001] The invention relates to a hydroprocessing-catalytic cracking combined process method for producing more isobutane and light aromatics. Background technique [0002] In my country, catalytic cracking has been widely used due to its good operational flexibility, high gasoline yield and low one-time investment. A single catalytic cracking process has certain requirements for catalytic raw materials. Raw materials with high sulfur content not only make SOx emissions in catalytic cracking flue gas not meet environmental protection requirements, but also the sulfur content of gasoline products cannot meet product specifications. High nitrogen content in catalytic cracking feedstock will increase the consumption of cracking catalysts and increase operating costs. The hydrogenation pretreatment technology of catalytic cracking raw materials can greatly reduce its sulfur and nitrogen content and increase its hydrogen content, thereby reducing the sulfur and n...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G69/00
CPCC10G69/00C10G2400/04C10G2300/202C10G2300/205C10G2300/70C10G2400/30C10G2400/28C10G2300/1037
Inventor 张毓莹许友好龚剑洪梁家林陈文斌董松涛许双辰刘涛戴立顺
Owner CHINA PETROLEUM & CHEM CORP
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