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Method for producing light olefin by catalytic pyrolysis of petroleum hydrocarbon

A technology for catalytic cracking and low-carbon olefins, which is applied in the field of producing low-carbon olefins by catalytic cracking of petroleum hydrocarbons, can solve the problems of high yield of low-carbon number olefins, low energy consumption and high energy consumption, and achieves lower reaction temperature and energy saving. consumption effect

Active Publication Date: 2009-06-24
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0004] The purpose of the present invention is to overcome the shortcoming of high energy consumption in the method for producing low-carbon olefins by catalytic cracking of petroleum hydrocarbons in the prior art, and to provide a low-energy-consumption and high yield of low-carbon number olefins to produce low-carbon olefins by catalytic cracking of petroleum hydrocarbons. carbene method

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0021] This example illustrates the preparation of the dehydrogenation catalyst used in the present invention and its dehydrogenation activity.

[0022] 11.5 g of analytically pure NH 4 VO 3 Dissolve in 68 ml of distilled water to make a solution. 50 grams of 20-40 mesh γ-Al 2 o 3 The carrier was immersed in the above-prepared solution for 24 hours, then evaporated to dryness on a 70°C water bath, then dried at 120°C for 24 hours, and calcined at 550°C in air for 15 hours. Thus made V 2 o 5 / γ-Al 2 o 3 Dehydrogenation catalyst, denoted as DH-1, wherein based on the weight of the catalyst, V 2 o5 The content is 10% by weight, γ-Al 2 o 3 The content is 90% by weight.

[0023] Use a small fixed bed to evaluate the dehydrogenation activity of the dehydrogenation catalyst. The evaluation conditions are: the reaction temperature is 530°C, and the weight hourly space velocity is 30 hours. -1 , the pressure is 0.3 MPa, the reaction raw material is naphtha, and the product ...

Embodiment 2

[0025] This example illustrates the preparation of the dehydrogenation catalyst used in the present invention and its dehydrogenation activity.

[0026] 5.25 grams of oxalic acid and 10 milliliters of deionized water were mixed to prepare a solution, and then 0.395 grams of hexachloroplatinic acid was added to obtain solution A. 0.498 g of SnCl 2 2H 2 O and 10 ml of deionized water were mixed to prepare a solution, and then 1.0 ml of concentrated hydrochloric acid was added to obtain solution B. Add solution B to solution A, stir well and add dropwise to 50 grams of 20-40 mesh ZnAl 2 o 4 In the carrier, heat it at 70°C for 1 hour after adding, and then dry it at 150°C for 6 hours. The dried particles are heated at 266°C for 2 hours, and then roasted at 524°C for 5 hours, and then heated with hot water Wash in a Soxhlet extractor for 6 hours, then dry at 150°C for 24 hours. Thus prepared Pt-Sn / ZnAl 2 o 4 Dehydrogenation catalyst, wherein based on the weight of the cataly...

Embodiment 3

[0029] This example illustrates the preparation of the dehydrogenation catalyst used in the present invention and its dehydrogenation activity.

[0030] 50 grams of 20-40 mesh γ-Al 2 o 3 The carrier is added to a solution made by mixing 10.87 g of chromic acid and 70 ml of deionized water for 2 hours, then pre-dried at 50-60 °C for 4 hours, then placed in a 120 °C oven overnight, and finally placed in a 550 °C muffle furnace Medium roasting for 6 hours. Cr 2 o 3 / γ-Al 2 o 3 Dehydrogenation catalyst, wherein based on the weight of the catalyst, Cr 2 o 3 The content is 14% by weight γ-Al 2 o 3 The content is 86% by weight. The dehydrogenation catalyst is pressed into tablets, pulverized and sieved, and the particles with a size of 20-40 meshes are collected as the dehydrogenation catalyst to be used, which is counted as DH-3.

[0031] Use a small fixed bed to evaluate the dehydrogenation activity of the dehydrogenation catalyst. The evaluation conditions are: the reac...

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PUM

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Abstract

The invention relates to a method for producing low-carbon olefin by petroleum hydrocarbon catalytic pyrolysis; the method comprises: catalytic pyrolysis is carried out on the petroleum hydrocarbon; wherein, the method also comprises that the step that catalytic dehydrogenation is carried out on the petroleum hydrocarbon under the catalytic dehydrogenation condition and in the presence of catalytic dehydrogenation catalyst before the catalytic pyrolysis, and then the catalytic pyrolysis is carried out on the catalytic dehydrogenation product under the catalytic pyrolysis condition in the presence of catalytic pyrolysis catalyst. In the method, when the petroleum hydrocarbon is naphtha or light diesel oil, the needed reaction temperature of the conversion rate of the petroleum hydrocarbon and selectivity of the olefin is greatly reduced compared with the existing technique that the light olefin is prepared by the naphtha and light diesel oil through catalytic conversion, and the temperature is reduced to 550-650 DEG C from 750-850 DEG C in the prior art, thus greatly saving energy consumption.

Description

technical field [0001] The invention relates to a method for producing light olefins by catalytic cracking of petroleum hydrocarbons. Background technique [0002] Tube furnace steam cracking technology has always been dominant in the production of ethylene and propylene from petroleum hydrocarbon cracking. Its technology has been perfected day by day, but the main problems at present are: high energy consumption. At present, the steam cracking process consumes more energy than the entire petrochemical enterprise. 40%; the yield of ethylene and propylene is difficult to increase. In recent years, due to the harsher reaction conditions (such as millisecond furnace cracking temperature of 900 ° C and residence time of 0.1 seconds), it is difficult to pass through due to the limitation of furnace tube material. Increase the severity of the cracking reaction to increase the yield of ethylene and propylene; harsh reaction conditions make the furnace tube more likely to coke and s...

Claims

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Application Information

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IPC IPC(8): C07C4/06C07C11/02
Inventor 张书红王子军崔德春李锐侯焕娣
Owner CHINA PETROLEUM & CHEM CORP
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