Method for producing light olefins and monocyclic aromatic hydrocarbons from heavy hydrocarbons

A technology for low-carbon olefins and single-ring aromatics, which is applied in the treatment of hydrocarbon oil, the petroleum industry, and hydrotreating processes. It can solve the problems of increasing the production of high-value target products, and achieve the effects of improving properties and improving the removal rate of impurities

Active Publication Date: 2010-06-23
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The technical problem to be solved by the present invention is that in the prior art, the deactivation rate of the hydrogenation catalyst is too fast under mild operating conditions, and the catalytic cracking of light cycle oil and heavy cycle oil cannot use self-refining to increase production of high value due to polycyclic aromatic hydrocarbons The problem of the target product

Method used

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  • Method for producing light olefins and monocyclic aromatic hydrocarbons from heavy hydrocarbons
  • Method for producing light olefins and monocyclic aromatic hydrocarbons from heavy hydrocarbons

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0046] Embodiment 1 adopts the method provided by the present invention:

[0047] The first hydrogenation reaction zone (first reaction) is filled with 200ml of wax oil hydrogenation refined preparation A, and the second hydrogenation reaction zone (second reaction) is filled with catalysts B, C and D from top to bottom, a total of 400ml, and the filling volume The ratio is 5:45:50. The mixed oil of wax oil and heavy cycle oil (mass ratio 9:1) is first passed through the first reactor for hydrorefining at a flow rate of 320g / h, and mixed with the residual oil at the outlet of the first reactor at a flow rate of 80g / h, and then enters the second reactor for adding Hydrogen reaction. The reaction pressure of the first reactor and the second reactor is 10.0 MPa, and the reaction temperature is 370°C. The effluent after the reaction is cooled and separated, the hydrogen-containing gas is recycled, and the liquid product enters the fractionation system. Here, gas and a small amount...

Embodiment 2

[0056] Embodiment 2 adopts the method provided by the present invention:

[0057] The first reactor is filled with 250ml of wax oil hydrofining preparation A, and the second reactor is filled with catalysts B, C, D and E from top to bottom, a total of 400ml, and the filling volume ratio is 5:45:45:5. After wax oil, heavy cycle oil and light cycle oil are mixed in a mass ratio of 320:32:48, the mixed oil is first passed through a reactor at a flow rate of 400g / h for hydrorefining, and blended at a flow rate of 80g / h at the outlet of the first reactor. After the residual oil, enter the second reactor for hydrogenation reaction. The reaction pressure is 9.0MPa, the first reaction temperature is 365°C, and the second reaction temperature is 380°C. The effluent after the reaction is cooled and separated, the hydrogen-containing gas is recycled, and the liquid product enters the fractionation system. Here, hydrogen sulfide and a small amount of light distillate are fractionally disti...

Embodiment 3

[0060] Embodiment 3 adopts another form of the method provided by the present invention:

[0061] The first reactor is filled with 250ml of wax oil hydrofining preparation A, and the second reactor is filled with catalysts B, C, D and E from top to bottom, a total of 400ml, and the filling volume ratio is 5:45:45:5. After wax oil, heavy cycle oil and light cycle oil are mixed in a mass ratio of 320:24:36, the mixed oil is first passed through a reactor at a flow rate of 380g / h for hydrorefining, and blended at a flow rate of 100g / h at the outlet of the first reactor. After the residual oil mixed oil enters the second reactor for hydrogenation reaction, the composition of the used residual oil mixed oil is residual oil: heavy cycle oil: light cycle oil=80:8:12 (mass ratio). The reaction pressure is 9.0MPa, the first reaction temperature is 365°C, and the second reaction temperature is 380°C. The effluent after the reaction is cooled and separated, the hydrogen-containing gas is r...

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Abstract

The invention provides a method for producing light olefins and monocyclic aromatic hydrocarbons from heavy hydrocarbons. The method produces qualified catalytic cracking raw materials through hydrogenation by taking wax oil and residual oil as raw materials, returns light cycle oil and heavy cycle oil which are catalytic cracking by-products to a hydrogenation unit for the catalytic cracking rawmaterials at the same time, hydrogenates the catalytic cracking by-products together with the catalytic cracking raw materials, and then takes the obtained product as the catalytic cracking raw materials to produce light olefins and monocyclic aromatic hydrocarbons. By introducing the residual oil before a second reaction zone of hydrogenation, the method widens the sources of the catalytic cracking raw materials, increases the processing amount of low-value residual oil, and solves the problem of the heat balance of catalytic cracking units. The light and heavy cycle oil of catalytic cracking is introduced into the hydrogenation unit, hydrogenated and then taken as the catalytic cracking raw materials, so that the yield of high-value products of the catalytic cracking units can be increased, and the deactivation of hydrogenation catalysts is delayed.

Description

Technical field [0001] The present invention belongs to a method for treating hydrocarbon oil with a hydrotreating process and another conversion step. More specifically, it is a method for producing low-carbon olefins and monocyclic aromatic hydrocarbons from heavy hydrocarbons by a combined hydrogenation-catalytic cracking process. method. Background technique [0002] The world's demand for low-carbon olefins and aromatics is increasing. In addition to steam cracking methods, methods for producing low-carbon olefins, especially propylene, also include catalytic cracking processes. At present, catalytic cracking mainly uses hydrogenated or unhydrogenated vacuum distillate as raw material for cracking. For the method of deep cracking from heavy hydrocarbons as raw materials to maximize the production of propylene, if the raw materials are not hydrogenated, it is not conducive to environmental protection and cannot achieve a higher propylene yield. The first hydrogenation of t...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G65/00
Inventor 牛传峰高永灿刘涛戴立顺邵志才杨清河胡大为聂红
Owner CHINA PETROLEUM & CHEM CORP
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