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Gasoline olefin reducing catalytic cracking method and device

A catalytic cracking device and a catalytic cracking technology are applied in the field of catalytic cracking for reducing gasoline olefins, which can solve the problems of high contact temperature between a regenerated catalyst and raw materials, inability to flexibly control the temperature of the catalyst, and low coking capacity of the device, so as to reduce the catalyst storage capacity. , the effect of size reduction and equipment investment reduction

Active Publication Date: 2012-01-11
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0013] The technical problem to be solved by the present invention is that in the existing catalytic cracking process, the temperature of the catalyst in the regenerator cannot be flexibly controlled, the contact temperature between the regenerated catalyst and the raw material is high, the reaction time is long, the ratio of catalyst to oil is low, and the coking capacity of the device is low, etc.

Method used

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  • Gasoline olefin reducing catalytic cracking method and device
  • Gasoline olefin reducing catalytic cracking method and device
  • Gasoline olefin reducing catalytic cracking method and device

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0067] The raw material used in the test was atmospheric residual oil from Daqing, and the catalyst was commercially available CC-20 catalytic cracking industrial equilibrium catalyst with a microreactive activity of 65.

[0068] The catalytic cracking program is carried out on a small-scale fluidized bed device in the laboratory. The catalyst to be produced is burnt in a tubular manner and then enters the regenerator with a micro-reaction activity of 65. The stripping medium in the stripping section of the settler is water vapor, and the stripping temperature is 500°C. Table 5 shows the operating conditions, product distribution and properties of some products in the catalytic cracking unit of this example.

Embodiment 2

[0070] According to Example 1, the difference is the temperature of the regenerated catalyst from the regenerator, the reaction temperature of the raw material, the ratio of agent to oil, and the reaction time. The operating conditions, product distribution and some product properties of the catalytic cracking unit in this embodiment are shown in Table 6.

Embodiment 3

[0072] According to embodiment 1, the difference is the temperature of the regenerated catalyst from the regenerator, the agent-oil ratio and the reaction time of the raw materials during the reaction. The operating conditions, product distribution and some product properties of the catalytic cracking unit in this embodiment are shown in Table 7.

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Abstract

The invention discloses a gasoline olefin reducing catalytic cracking method and a gasoline olefin reducing catalytic cracking device. In the method and the device, a renewable catalyst is contacted with heavy oil and low-quality gasoline through conveying pipes for reactions respectively, the reaction oil gases enter a fractioning system respectively, the catalyst to be renewed is renewed in a tubular coke burning device and a catalyst dense-phase bed, and the renewed catalyst is used circularly. When the method and the device are used, the drawbacks of nonflexible control of catalyst temperature, high renewable catalyst and raw material contact temperature, long reaction time, low agent to oil ratio, low coke burning capacity of the device and the like are overcome.

Description

technical field [0001] The invention belongs to the catalytic cracking of hydrocarbon oil in the absence of hydrogen, in particular to a catalytic cracking method and device for reducing gasoline olefins. Background technique [0002] At present, the conventional riser type catalytic cracking unit has the following problems: [0003] First, the temperature of the regenerator cannot be flexibly controlled. The regeneration temperature of the catalyst is generally higher than 650°C, which makes the instantaneous contact temperature of the oil agent in the riser reactor higher. Excessively high oil agent contact temperature will aggravate the thermal cracking reaction and reduce the catalytic performance. The degree of cracking reaction, the result is that the product distribution deteriorates, the yield of dry gas and coke increases, and the total liquid yield decreases (the total liquid yield refers to the sum of liquefied gas yield, gasoline yield and diesel yield), due to t...

Claims

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Application Information

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IPC IPC(8): C10G51/06
Inventor 王文柯王龙延王国良汤海涛孟凡东陈曼桥闫鸿飞张亚西常剑
Owner CHINA PETROLEUM & CHEM CORP
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