Catalytic cracking and catalytic gasoline hydrogenation combined technological method

A catalytic cracking and catalytic gasoline technology, applied in hydrotreating process, petroleum industry, treatment of hydrocarbon oil, etc., can solve the problems of different process flow, poor adaptability of raw materials, etc., to reduce energy consumption, mature and reliable technical solutions, reduce The effect of retrofit investment and operating costs

Active Publication Date: 2015-04-15
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Although this method can also produce gasoline products with a sulfur content less than 10 μg / g, the raw material has poor adaptability, and the process flow is completely different from the idea of ​​the present invention

Method used

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  • Catalytic cracking and catalytic gasoline hydrogenation combined technological method

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0044] The catalytic gasoline 1 is pre-separated in the fractionation tower of the catalytic cracking unit to obtain light fractions and heavy fractions. The division temperature of the light fractions and heavy fractions is 73°C; The thermocatalytic diesel oil enters the hydrogenation pre-fractionation tower together for fractionation. The separation temperature of the obtained light gasoline and medium gasoline is 65°C, and the dry point of medium gasoline is 78°C. The prehydrogenation reaction conditions are: hydrogen partial pressure 1.8MPa, volume space velocity 3.8 h -1 , The reaction temperature is 178°C; the hydrodesulfurization reaction conditions are: hydrogen partial pressure 1.6MPa, volume space velocity 2.8h -1 , The reaction temperature is 282°C; the total hydrogen-to-oil volume ratio is 350.

[0045] The alkali-free deodorization conditions are: the operating pressure of the reactor is 0.6MPa, the reaction temperature is 35°C, and the feed space velocity is 0.9...

Embodiment 2

[0048] The catalytic gasoline 2 is pre-separated in the fractionation tower of the catalytic cracking unit to obtain light fractions and heavy fractions; the division temperature of the light fractions and heavy fractions is 76°C; The thermocatalytic diesel oil enters the hydrogenation pre-fractionation tower together for separation. The separation temperature of the obtained light gasoline and medium gasoline is 62°C, and the dry point of medium gasoline is 76°C. The prehydrogenation reaction conditions are: hydrogen partial pressure 2.0 MPa, volume space velocity 3.5 h -1 , The reaction temperature is 183°C; the hydrodesulfurization reaction conditions are: hydrogen partial pressure 1.8MPa, volume space velocity 3.0 h -1 , The reaction temperature is 288°C; the total hydrogen-to-oil volume ratio is 380.

[0049] The alkali-free deodorization conditions are: the operating pressure of the reactor is 0.5MPa, the reaction temperature is 45°C, and the feed space velocity is 0.8h...

Embodiment 3

[0052] The catalytic gasoline 3 is pre-separated in the fractionation tower of the catalytic cracking unit to obtain light fractions and heavy fractions; the division temperature of the light fractions and heavy fractions is 80°C; The thermocatalytic diesel oil enters the hydrogenation pre-fractionation tower together for separation. The separation temperature of the obtained light gasoline and medium gasoline is 67°C, and the dry point of medium gasoline is 83°C. The prehydrogenation reaction conditions are: hydrogen partial pressure 1.8MPa, volume space velocity 4.2 h -1 , Reaction temperature 180℃; hydrodesulfurization reaction conditions: hydrogen partial pressure 1.6MPa, volume space velocity 3.2 h-1 , The reaction temperature is 277°C; the total hydrogen-to-oil volume ratio is 320.

[0053] The conditions for alkali-free deodorization are: reaction pressure 0.5MPa, reaction temperature 40°C, feed space velocity 1.1h -1 , with an air / feed volume ratio of 1.0. The operat...

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Abstract

The invention discloses a catalytic cracking and catalytic gasoline hydrogenation combined technological method. The method comprises: adjusting the operating conditions of a FCC (fluid catalytic cracking) device fractionating tower, conducting cutting pre-separation on FCC gasoline in the fractionating tower so as to obtain light fractions and heavy fractions; subjecting the light fractions to alkali-free deodorization, then letting the deodorized light fractions and thermocatalytic diesel oil enter a hydrogenation prefractionator together, thus obtaining light gasoline at the tower top and medium gasoline at a tower middle lateral line, mixing the medium gasoline with the heavy fractions, then passing the mixture through a hydrogenation protection reactor and a hydrodesulfurization reactor in order, and mixing the obtained refined product with the deodorized refined light gasoline so as to obtain a clean gasoline product. With the method provided in the invention, the equipment energy consumption is significantly reduced, the gasoline octane number loss is small, gasoline product quality can meet the quality requirement of a sulfur content of less than 10 micrograms / g, and the economic benefits of oil refining enterprises are improved.

Description

technical field [0001] The invention relates to a combined process of catalytic cracking and catalytic gasoline hydrogenation, in particular a method for hydrogenating catalytic gasoline as a raw material to produce clean gasoline with a sulfur content less than 10 μg / g. Background technique [0002] With the increasingly stringent environmental protection regulations, developed countries such as Europe and the United States have successively put forward stricter regulations on the content of sulfur and olefins in motor gasoline. From 2009 onwards, the Euro V emission standard with a sulfur content of less than 10 μg / g will be implemented. my country's requirements for the sulfur content of motor gasoline are becoming more and more stringent. Since January 1, 2008, the gasoline supplied to Beijing has begun to implement the specifications equivalent to Euro IV emission standards, that is, the sulfur content is less than 50 μg / g, and Shanghai, Guangzhou Similar standards will...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/00
Inventor 徐大海李扬牛世坤丁贺
Owner CHINA PETROLEUM & CHEM CORP
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