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A passivation start-up method for gasoline hydro-upgrading catalyst containing molecular sieve

A gasoline hydrogenation and hydrogenation upgrading technology, which is applied in the fields of hydrogenation treatment process, petroleum industry, hydrocarbon oil treatment, etc., can solve the problems of unusable passivation and difficulty in ensuring the stability of catalyst activity, etc., so as to improve stability, The effect of avoiding the loss of catalyst activity

Active Publication Date: 2018-08-10
PETROCHINA CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0008] The passivation process in CN201110321354.2 and CN201210432673.5 is a reversible process, it is difficult to ensure the activity stability of the catalyst, and both use heavy oil products with an initial boiling point greater than 200 ° C as the passivation oil, so they cannot be used for final Passivation of lower gasoline fractions

Method used

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  • A passivation start-up method for gasoline hydro-upgrading catalyst containing molecular sieve
  • A passivation start-up method for gasoline hydro-upgrading catalyst containing molecular sieve
  • A passivation start-up method for gasoline hydro-upgrading catalyst containing molecular sieve

Examples

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Effect test

Embodiment 1

[0023]Apply gasoline hydro-upgrading catalyst A to a 400,000-ton / year FCC gasoline hydrogenation unit. After catalyst sulfuration treatment, reduce the inlet temperature of the hydro-upgrading reactor to 260°C. 21t / h, hydrorefined oil flow rate 26t / h, FCC gasoline and hydrorefined oil are introduced into the reaction system at the same time, and the system sends out 47t / h of products; increase the inlet temperature of the reactor at 20°C / h, Until the inlet temperature of the reactor reaches 310°C;

[0024] Reduce the inlet temperature of the hydro-upgrading reactor to 300°C, and introduce the catalytic cracking gasoline and hydro-refined oil into the reaction system at the same time according to the feed flow rate of catalytic cracking gasoline of 33t / h and the flow rate of hydro-refined oil product of 14t / h. At the same time, the system sends out 47t / h of products; increase the inlet temperature of the reactor at 8°C / h until the inlet temperature of the reactor reaches 340°C;...

Embodiment 2

[0029] Pack 500ml of gasoline hydro-upgrading catalyst A into a 500ml adiabatic bed hydrogenation reactor. After the catalyst is vulcanized, the inlet temperature of the reactor is lowered to 250°C, and naphtha containing 35wt% FCC gasoline is introduced into the reaction system; increase the inlet temperature of the reactor at a heating rate of 3°C / h until the inlet temperature of the reactor reaches 315°C;

[0030] The inlet temperature of the reactor was lowered to 300°C, and naphtha containing 62wt% FCC gasoline was introduced into the reaction system; the inlet temperature of the reactor was increased by 3°C / h until the inlet temperature of the reactor reached 340°C;

[0031] Reduce the inlet temperature of the reactor to 320°C, and introduce 100wt% catalytically cracked gasoline raw material into the reaction system; increase the inlet temperature of the reactor at 3°C / h until the inlet temperature of the reactor reaches 370°C, and the passivation process ends. During th...

Embodiment 3

[0040] Pack 500ml of gasoline hydro-upgrading catalyst C into a 500ml adiabatic bed hydrogenation reactor. After the catalyst is vulcanized, the inlet temperature of the reactor is lowered to 230°C, and the catalytic reformed oil containing 41wt% coked gasoline is simultaneously introduced into the reaction System; increase the inlet temperature of the reactor at 10°C / h until the inlet temperature of the reactor reaches 310°C;

[0041] Reduce the inlet temperature of the reactor to 285°C, introduce catalytic reformed oil containing 65wt% coker gasoline into the reaction system; increase the inlet temperature of the reactor at 5°C / h until the inlet temperature of the reactor reaches 340°C;

[0042] Reduce the inlet temperature of the reactor to 315°C, introduce 100wt% coked gasoline raw material into the reaction system; increase the inlet temperature of the reactor at 5°C / h until the inlet temperature of the reactor reaches 360°C; the passivation process ends. During the passi...

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Abstract

The invention relates to a method for passivation startup of a gasoline hydro-upgrading catalyst containing a molecular sieve. After an oxidation-state catalyst in a gasoline hydro-upgrading reactor is vulcanized, reactor inlet temperature is reduced, a mixture of low-olefin light oil and gasoline raw material is used as a passivator, the proportion of gasoline in passivation oil is made to be matched with passivation temperature through oscillating type stepped heating, and then passivation startup is achieved. The gasoline raw material diluted by low-olefin light oil is used as the passivator, so that perpetual passivation and reversible passivation are both achieved, and stable startup and catalyst activity and stability improvement are realized. Meanwhile, the proportion of the catalytic gasoline raw material is increased gradually during passivation, raw oil feeding is completed when passivation is finished, and therefore introduction of raw oil after passivation is omitted.

Description

technical field [0001] The invention relates to a passivation start-up method for a gasoline hydrogenation upgrading catalyst containing molecular sieves, which mainly uses a raw material oil product with low olefin content as a passivating agent to heat up the sulfurized hydrogenation upgrading catalyst in a device through a swinging stepwise temperature rise It is used for passivation to avoid overheating. It is suitable for the passivation start-up process of various types of gasoline hydrogenation modification catalysts containing molecular sieves, especially for the hydrogenation modification of blending components for producing high-octane clean gasoline. Background technique [0002] Catalytic gasoline, coker gasoline, etc. all contain a large amount of sulfide, and need to undergo hydrodesulfurization treatment before they can be used as gasoline blending components. Among them, the content of olefins in catalytic gasoline and coker gasoline is 30-50v%. Hydrodesulfur...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/00
Inventor 吴杰张忠东王廷海王玲玲向永生李自夏高源姚文君蔡进军田力王晨晨苟尕莲孟凡芳李景峰田爱珍
Owner PETROCHINA CO LTD
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