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Start-up vulcanizing method of hydrocracking process

A technology of hydrocracking and hydrogenation catalyst, which is applied in the fields of hydrotreating process, petroleum industry, and hydrocarbon oil treatment, etc. It can solve problems such as the optimization of vulcanization method at the start of production, and achieve sufficient and thorough wetting, reduced cracking loss, and convenient operation Effect

Inactive Publication Date: 2012-05-09
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] For the hydrocracking process including two types of catalysts, the hydrocracking pre-refining catalyst and the hydrocracking catalyst, the existing start-up sulfidation method does not have an optimized sulfidation start-up method for the difference between the two catalysts, so It is necessary to further optimize the start-up sulfidation process to improve the technical effect of the hydrocracking process

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0043] FF-46 and FC-32 are installed in their respective reactors and are airtight. After the airtightness is qualified, the hydrogen partial pressure is adjusted to 14.0MPa, the temperature is adjusted to 100°C, and the vulcanized oil is introduced (the vulcanized oil is straight-run kerosene containing 2wt% carbon disulfide), and the volume space velocity of the vulcanized oil is 2h -1 , the volume ratio of hydrogen to oil is 1000. Start to raise the temperature at 10°C / h to 220°C, keep the temperature constant for 8 hours, and wait for the vulcanizing agent to penetrate each catalyst bed layer, end the constant temperature and start to withdraw the vulcanized oil. Use the mixed gas of hydrogen sulfide and circulating hydrogen to continue to raise the temperature to 370°C at 10°C / h, keep the temperature constant for 8 hours, and when the constant temperature is over, switch the raw oil according to the operation. After switching the feedstock, it was raised to 380°C and ope...

Embodiment 2

[0045] FF-46 and FC-32 are installed in their respective reactors and are airtight. After the airtightness is qualified, the hydrogen partial pressure is adjusted to 14.0MPa, the temperature is adjusted to 150°C, and the vulcanized oil is introduced (the vulcanized oil is straight-run kerosene containing 2wt% carbon disulfide), and the volume space velocity of the vulcanized oil is 2h -1 , the volume ratio of hydrogen to oil is 1000. Start to raise the temperature at 10°C / h to 230°C, keep the temperature constant for 10 hours, and wait for the vulcanizing agent to penetrate each catalyst bed layer, end the constant temperature and start to exit the vulcanized oil. Use the mixed gas of hydrogen sulfide and circulating hydrogen to continue to raise the temperature to 370°C at 10°C / h, keep the temperature constant for 8 hours, and when the constant temperature is over, switch the raw oil according to the operation. After switching the feedstock, it was raised to 380°C and operat...

Embodiment 3

[0047] FF-46 and FC-32 are installed in their respective reactors and are airtight. After the airtightness is qualified, the hydrogen partial pressure is adjusted to 14.0MPa, the temperature is adjusted to 135°C, and the vulcanized oil is introduced (the vulcanized oil is straight-run kerosene containing 2wt% carbon disulfide), and the volume space velocity of the vulcanized oil is 2h -1 , the volume ratio of hydrogen to oil is 1000. Start to raise the temperature at 10°C / h to 220°C, keep the temperature constant for 8 hours, and wait for the vulcanizing agent to penetrate each catalyst bed layer, end the constant temperature and start to withdraw the vulcanized oil. Use the mixed gas of hydrogen sulfide and circulating hydrogen to continue to raise the temperature to 370°C at 10°C / h, keep the temperature constant for 8 hours, and when the constant temperature is over, switch the raw oil according to the operation. After switching the feedstock, it was raised to 380°C and ope...

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Abstract

The invention discloses a start-up vulcanizing method of hydrocracking process. The hydrocracking process uses the hydrocracking pre-refining catalyst and hydrocracking catalyst, wherein the hydrocracking pre-refining catalyst is the second kind active centre hydrogenation catalyst. The processes of vulcanizing with wet method first and vulcanizing with dry method then are used by the start-up vulcanizing method. The wet method vulcanization is switched as dry method vulcanization when the vulcanizing temperature reaches up to 170-260 DEG C. The start-up vulcanizing method of the invention can ensure the activities of hydrocracking pre-refining catalyst and hydrocracking catalyst simultaneously and increase the safety and stability of the start-up vulcanizing method. The start-up vulcanizing method is the start-up vulcanizing process of the hydrocracking process which is the most suitable for the second kind active centre hydrogenation catalyst.

Description

technical field [0001] The invention relates to a start-up vulcanization method of a hydrocracking process, in particular to a start-up vulcanization method of a hydrocracking process using a second-type active center hydrocracking pre-refining catalyst. technical background [0002] Due to the slow growth of crude oil production and increasingly heavy quality, the demand for clean oil products in today's world is increasing, and the product quality requirements are becoming more and more stringent. Petroleum fraction hydrogenation technology is currently the main technology for producing clean oil products, and the preparation technology of hydrogenation catalyst is the key to hydrogenation technology. The active metal component of the prepared hydrogenation catalyst is in an oxidized state, and before the oxidized state catalyst is used in industry, its active metal needs to be converted into a sulfurized state to have high catalytic activity. Therefore, the sulfidation o...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G65/02C10G65/00
Inventor 陈光杜艳泽高玉兰徐黎明李崇慧
Owner CHINA PETROLEUM & CHEM CORP