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Parallel hydrocracking method

A hydrocracking and hydrotreating technology, which is applied in the fields of hydrotreating process, petroleum industry, and hydrocarbon oil treatment, can solve the problems of uneconomical rationality, high hydrogen consumption, and difficulty in effective treatment, so as to prevent Excessive decrease in unit cell constant, increase in yield, effects of appropriate acidity

Active Publication Date: 2009-06-10
CHINA PETROLEUM & CHEM CORP +2
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

It is difficult to effectively treat this kind of inferior catalytic cracked diesel oil by the above-mentioned hydrogenation method, and it is not economically reasonable due to the large hydrogen consumption in the processing process

Method used

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  • Parallel hydrocracking method

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0050] Weigh raw material NH 4 NaY type molecular sieve (ammonium exchange degree is 80%, weight loss on ignition is 27.1%, SiO 2 / Al 2 o 3 Molar ratio is 5.3, sodium oxide content is 4.0wt%) 2057.6 grams, add 9 liters of distilled water to make slurry, and under stirring condition, heat slurry and be warmed up to 95 ℃; Add dropwise by 495.0 grams of ammonium hexafluorosilicate The solution prepared with 3500 milliliters of distilled water was dripped in 2 hours, then continued to stir at 95° C. for 2 hours, stopped stirring and stood for about 10 minutes, and separated the precipitated sodium ammonium fluoride (silicon) aluminate crystals by decantation. And after washing with water and drying, the Y-type molecular sieve precursor A1 is obtained.

[0051] Weigh raw material NH 4 NaY type molecular sieve (ammonium exchange degree is 75%, weight loss on ignition is 26%, SiO 2 / Al 2 o 3 Molar ratio is 4.5, sodium oxide content is 4.0wt%) 270 grams, add 1.2 liters of disti...

Embodiment 2

[0053] The present embodiment prepares hydrocracking catalyst C1, and concrete steps are as follows:

[0054] (1) The Y-type molecular sieve precursor Al is subjected to hydrothermal treatment, wherein the hydrothermal treatment conditions are as follows: the temperature is 600° C., the water pressure is 0.1 MPa, and the treatment time is 1 hour to obtain the Y-type molecular sieve Y1.

[0055] (2) Get the Y-type molecular sieve Y1 of 153.5 grams of step (1) gained, by 120 grams of small hole alumina (pore volume 0.47ml / g, specific surface area is 280m 2 / g), 0.2N dilute nitric acid solution 440ml peptized binder mixed, after extrusion, molding, then through 110 ℃ of drying 5 hours, 600 ℃ of roasting 6 hours obtain catalyst carrier,

[0056] (3) impregnating the catalyst carrier obtained in step (2) with an aqueous solution containing molybdenum and nickel, drying at 110°C for 5 hours, and calcining at 500°C for 5 hours to prepare the hydrocracking catalyst C1 of the present i...

Embodiment 3

[0058] This embodiment prepares hydrocracking catalyst C2, and concrete steps are as follows:

[0059] (1) 170g Y type molecular sieve precursor A1 is mixed with the binder (same as implementation 2) prepared by peptizing 80g small-pore alumina and dilute nitric acid solution, extruded, shaped,

[0060] (2) Use ammonia-water vapor to treat the molded product obtained in step (1) at high temperature, the treatment conditions are as follows: temperature 550°C, pressure 0.1MPa, ammonia partial pressure 0.01MPa, treatment time 1 hour, obtained Carrier, which contains Y-type molecular sieve Y2;

[0061] (3) impregnating the catalyst carrier obtained in step (2) with an aqueous solution containing tungsten and nickel, drying at 110°C for 5 hours, and calcining at 500°C for 5 hours to prepare the hydrocracking catalyst C2 of the present invention.

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Abstract

This invention discloses a hydrocracking method, and this invention is used for producing high aromatic hydrocarbon heavy naphtha and high quality end oil.It includes that heavy distillate oil and poor quality catalytic cracking diesel hydrocracks separately, and the mixture of the cracking products is conducted gas liquid separation. Light naphtha, heavy naphtha, aviation kerosene, diesel oil and end oil will be obtained by distillating the liquid phase. The density of the poor quality catalytic cracking diesel oil is above 0.9g / ml, and the aromatic hydrocarbon is over 60wt% and the value of hexadecane is under 30. It is a adequate utilization of catalytic cracking craft to produce high aromatic hydrocarbon heavy naphtha and high quality end oil with heavy distillate oil and poor quality catalytic cracking diesel, which can be separately used as catalytic reforming material and making ethylene material by steam cracking method. High aromatic hydrocarbon heavy naphtha in this invention will produce a large amount of reforming hydrogen after catalytic reforming treatment, which can be used in the process of hydrocracking to make this preparation more ecnomical and reasonable.

Description

technical field [0001] The invention relates to a hydrocracking method, in particular to a hydrocracking method capable of effectively treating inferior catalytic cracking diesel oil. Background technique [0002] As crude oil becomes heavier and inferior, and the market demand for heavy oil decreases and the demand for light oil increases, the degree of deep conversion of heavy residual oil continues to increase. Among them, catalytic cracking is one of the important means of lightening heavy residue oil. However, the properties of the products obtained by catalytic cracking are generally poor, and further processing is required to obtain qualified products. The diesel fraction obtained from catalytic cracking generally has the characteristics of high aromatics content, low cetane number, high sulfur and nitrogen content, and it is difficult to directly use it as a product, and it is difficult to effectively improve its product quality by ordinary processing methods. [0...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G65/10
Inventor 戴宝华石友良胡江青曾榕辉屠伟龙刘涛潘德满吴子明
Owner CHINA PETROLEUM & CHEM CORP
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