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Method for preparing chemicals by double-tube parallel multi-zone catalytic conversion of crude oil

A technology for catalytic conversion and chemicals, applied in chemical instruments and methods, catalytic cracking, production of bulk chemicals, etc., can solve the problems of low content of gasoline aromatics, low yield of low-carbon olefins, and low content of aromatics in gasoline, etc. The effect of reducing coke yield, increasing aromatics content, and high aromatics content

Active Publication Date: 2021-10-01
CHINA UNIV OF PETROLEUM (EAST CHINA)
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, with this method, only a certain amount of propylene can be increased, the ethylene yield is low, and the content of aromatics in gasoline is low
Patents CN1557915A, CN1069054A, CN1237477A, ​​WO99 / 57230, US7261807, US4980053, US6569316, MAXOFIN process, PetroFCC process, LOCC process, NEXCC process, MILOS process, HS-FCC process, etc. also have low yields of low-carbon olefins and gasoline aromatics low content problem

Method used

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  • Method for preparing chemicals by double-tube parallel multi-zone catalytic conversion of crude oil
  • Method for preparing chemicals by double-tube parallel multi-zone catalytic conversion of crude oil
  • Method for preparing chemicals by double-tube parallel multi-zone catalytic conversion of crude oil

Examples

Experimental program
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Effect test

Embodiment 1

[0040] This example takes an upward reaction tube with a swirl structure as an example. After desalination and dehydration, the crude oil is divided into light components and heavy components according to the boiling point after desalination and dehydration, and fractions below 200°C are classified into light components. , The distillate above 200°C is a heavy component.

[0041] see figure 1 As shown in the process flow and schematic diagram of the device, the low-carbon alkanes 121 are injected from the lower part of the first riser reactor 102, and the high-temperature regeneration from the regenerator 103 is transported by the regeneration inclined pipe 105, and the pre-lifting steam or the lifting dry gas 104 is lifted up. Catalyst undergoes contact reaction, reacts for 0.1-5.0s at 600-800°C, agent-oil ratio 5-30, and pressure 0.1-0.4MPa, then leaves the light alkane reaction zone 123 and enters the first heavy oil reaction zone 124. The bottom of the reaction zone is mi...

Embodiment 2

[0043] The upward reaction tube with swirl feed structure is adopted, and the crude oil is directly fed.

[0044] see figure 1 As shown in the process flow and schematic diagram of the device, the low-carbon alkanes 121 are injected from the lower part of the first riser reactor 102, and the high-temperature regeneration from the regenerator 103 is transported by the regeneration inclined pipe 105, and the pre-lifting steam or the lifting dry gas 104 is lifted up. Catalyst undergoes contact reaction, reacts for 0.1-5.0s at 600-800°C, agent-oil ratio 5-30, and pressure 0.1-0.4MPa, then leaves the light alkane reaction zone 123 and enters the first heavy oil reaction zone 124. The bottom of the reaction zone is mixed with crude oil 101 preheated to 150-250°C, reacted for 0.1-5.0s at 500-700°C, agent-oil ratio 5-30, and pressure 0.1-0.4MPa, then enters the gas-solid separator 106 and The top spin 107 of the settler separates the oil agent, and the main reaction oil gas 108 enter...

Embodiment 3

[0046] A descending reaction tube with a swirling feed structure is used. After desalination and dehydration, the crude oil is first desalted and dehydrated, and then flashed or distilled. According to the boiling point, it is divided into light components and heavy components. °C fractions are heavy components. For the specific process, refer to Example 1.

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Abstract

The invention discloses a method for preparing chemicals by double-tube parallel multi-zone catalytic conversion of crude oil, the method comprises the following steps: directly feeding or desalting and dehydrating the crude oil, then dividing the crude oil into light and heavy components through a flash evaporation or distillation process, strengthening the contact reaction of oil gas and a catalyst by using two parallel novel structure reaction tubes, and performing zone control reaction, optimally combining feeding modes according to different properties of reaction materials, controlling suitable reaction conditions of different materials, and increasing the yield of low-carbon olefins and aromatic hydrocarbons.

Description

technical field [0001] The invention relates to the technical field of petroleum processing, in particular to a method for producing chemicals through double-pipe parallel connection and multi-zone catalytic conversion of crude oil. Background technique [0002] Low-carbon olefins such as ethylene and propylene are basic organic synthetic raw materials for petrochemical industry. With the rapid development of the world economy, their market demand is also increasing year by year, and the growth rate of propylene demand has exceeded that of ethylene. At present, more than 90% of the world's ethylene and nearly 70% of the propylene are derived from steam cracking processes that use light petroleum hydrocarbons such as ethane, naphtha, and light diesel oil as raw materials. However, the reaction severity of steam cracking is high, the reaction temperature even exceeds 1100°C, and the residence time is shortened to less than 0.2 seconds. The space for technological progress is a...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G55/00C10G1/00C10G1/08C10G1/10C10G3/00C07C4/06C07C11/04C07C11/06
CPCC10G55/00C10G3/42C10G1/08C10G1/10C10G1/002C07C4/06C10G2400/02C10G2400/20C10G2300/10C10G2300/1037C10G2300/1044C10G2300/104C10G2300/1077C10G2300/107C10G2300/70C07C11/04C07C11/06Y02P30/20Y02P20/52Y02P20/584C10G51/026C10G11/18C10G55/06C10G3/57B01J23/02B01J21/14B01J21/10B01J21/20B01J23/92B01J38/30C10G50/00B01J35/08C10G2300/1003C10G2300/1014C10G2300/1018C10G2300/1059C10G2300/202C10G2300/205C10G2300/301C10G2300/308
Inventor 张金弘杨朝合田原宇山红红高春晓
Owner CHINA UNIV OF PETROLEUM (EAST CHINA)
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