Method used for catalytic gasoline deep hydrodesulfurization

A technology for catalyzing gasoline and deep hydrogenation, which is applied in hydrotreating process, petroleum industry, processing hydrocarbon oil, etc., can solve the problems of poor adaptability of raw materials and different process flow, so as to reduce the loss of octane number and achieve good technical effect. , the effect of reducing sulfur content

Active Publication Date: 2014-05-21
CHINA PETROLEUM & CHEM CORP +1
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Problems solved by technology

Although this method can also produce gasoline products with a sulfur content less than 10 μg/g, the raw materi

Method used

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  • Method used for catalytic gasoline deep hydrodesulfurization

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Embodiment 1

[0036] Catalytic gasoline first goes to the pre-fractionation tower to obtain light and heavy fractions. The separation temperature of the light and heavy fractions is 122°C; the light fraction is deodorized without alkali, and then enters the hydrogenation pre-fractionation tower for separation. The split temperature of mid-gasoline is 66°C. The pre-hydrogenation reaction conditions are: hydrogen partial pressure 1.8MPa, volumetric space velocity 3.8 h -1 , Reaction temperature 178℃; Hydrodesulfurization reaction conditions: hydrogen partial pressure 1.6MPa, volumetric space velocity 2.8h -1 The reaction temperature is 285℃; the volume ratio of total hydrogen oil is 360:1. The conditions for alkali-free deodorization are: reactor operating pressure 0.6MPa, reaction temperature 35°C, feed space velocity 0.9h -1 , The air / feed volume ratio is 0.7. The properties and test results of the raw oil are listed in Table 2.

[0037] It can be seen from Table 2 that the use of this techno...

Embodiment 2

[0039] Catalytic gasoline first goes to a pre-fractionation tower to obtain light and heavy fractions. The separation temperature of the light and heavy fractions is 118°C; the light fraction is deodorized without alkali, and then enters the hydrogenation pre-fractionation tower for separation. The split temperature of mid-gasoline is 65°C. The pre-hydrogenation reaction conditions are: hydrogen partial pressure 2.0MPa, volumetric space velocity 3.5 h -1 , Reaction temperature 183℃; Hydrodesulfurization reaction conditions: hydrogen partial pressure 1.8MPa, volumetric space velocity 3.0 h -1 The reaction temperature is 288℃; the volume ratio of total hydrogen to oil is 380:1. The conditions for alkali-free deodorization are: reactor operating pressure 0.5MPa, reaction temperature 45°C, feed space velocity 0.8h -1 , The air / feed volume ratio is 0.6. The properties and test results of the raw oil are listed in Table 2.

[0040] It can be seen from Table 2 that the use of this tech...

Embodiment 3

[0042] Catalytic gasoline first goes to the pre-fractionation tower to obtain light and heavy fractions. The separation temperature of the light and heavy fractions is 121°C; the light fraction is deodorized without alkali, and then enters the hydrogenation pre-fractionation tower for separation, resulting in light gasoline and The split temperature of mid-gasoline is 70°C. The pre-hydrogenation reaction conditions are: hydrogen partial pressure 1.8MPa, volumetric space velocity 4.2 h -1 , Reaction temperature 180℃; Hydrodesulfurization reaction conditions are: hydrogen partial pressure 1.6MPa, volumetric space velocity 3.2 h -1 The reaction temperature is 279℃; the volume ratio of total hydrogen to oil is 320:1. ; The conditions for alkali-free deodorization are: reactor operating pressure 0.5MPa, reaction temperature 40°C, feed space velocity 1.1h -1 , The air / feed volume ratio is 0.6. The properties and test results of the raw oil are listed in Table 2.

[0043] It can be see...

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Abstract

The invention discloses a method used for catalytic gasoline deep hydrodesulfurization. The method comprises following steps: catalytic gasoline is delivered into a prefrationation tower firstly; an appropriate separation point is adopted, light gasoline fraction and middle gasoline fraction are discharged through the top of the prefrationation tower, and heavy gasoline fraction is discharged through the bottom of the prefrationation tower; the light gasoline fraction and the middle gasoline fraction are subjected to alkali-free deodorization, and are delivered into a hydrogenation prefrationation tower so as to separate light gasoline and middle gasoline, wherein catalytic cracking hot diesel oil extracted from a main fractionate tower side line is also delivered into the hydrogenation prefrationation tower; separated middle gasoline and heavy gasoline are mixed, and are subjected to selective hydrogenation, and an obtained distillate is mixed with light gasoline obtained via alkali-free deodorization so as to obtain clean gasoline products. Compared with existing catalytic gasoline hydrodesulfurization method, the method and equipment of the invention is capable of reducing energy consumption greatly, octane value loss of the gasoline products is less, sulfur content of the gasoline products is less than 10<mu>g/g, and economic benefits of oil refining enterprises are improved.

Description

Technical field [0001] The invention relates to a catalytic gasoline deep hydrodesulfurization method, in particular to a method for hydrogenating catalytic gasoline as a raw material to produce clean gasoline blending components with a sulfur content of 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 legislated more and more stringent regulations on the sulfur and olefin content in motor gasoline. From 2009, the Euro V emission standard for sulfur content less than 10μg / g will be implemented. my country’s requirements for the sulfur content of motor gasoline are becoming more and more stringent. Starting from January 1, 2008, gasoline supplied to Beijing began to implement specifications equivalent to Euro IV emission standards, that is, the sulfur content is less than 50μg / g, Shanghai and Guangzhou Other major domestic cities will con...

Claims

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Application Information

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IPC IPC(8): C10G67/02
Inventor 陈琳徐大海丁贺庞宏牛世坤
Owner CHINA PETROLEUM & CHEM CORP
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