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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 field of producing low-carbon olefins and single-ring aromatics from heavy hydrocarbons in the hydrogenation-catalytic cracking combined process, which can solve the problems of increasing the production of high-value target products, and achieve property improvement and impurity removal. The effect of increasing the removal rate

Active Publication Date: 2013-04-24
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • 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

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

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

[0047] The first hydrogenation reaction zone (one reverse) is filled with 200ml of wax oil hydrofinishing preparation A, and the second hydrogenation reaction zone (two reverse) is filled with B, C and D catalysts from top to bottom, a total of 400ml, 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 hydrotreated through the first reaction at a flow rate of 320g / h, and then mixed with residual oil at the flow rate of 80g / h at the outlet of the first reaction, and then enters the second reaction for addition. hydrogen reaction. The reaction pressure of the first reaction and the second reaction are both 10.0MPa, 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. Gases and a small amount of hydrogenated naphth...

Embodiment 2

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

[0057] The first reverse is loaded with 250ml of wax oil hydrofinishing preparation A, and the second reverse is filled with B, C, D and E catalysts from top to bottom in sequence, 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 at a mass ratio of 320:32:48, the mixed oil is firstly hydrotreated through the first reverse at a flow rate of 400g / h, and mixed at the flow rate of 80g / h at the first reverse outlet Residual oil is then subjected to secondary reaction 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. Hydrogen sulfide and a small amount of light distillate are fractionally distill...

Embodiment 3

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

[0061] The first reverse is loaded with 250ml of wax oil hydrofinishing preparation A, and the second reverse is filled with B, C, D and E catalysts from top to bottom in sequence, 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 at a mass ratio of 320:24:36, the mixed oil is firstly hydrotreated through the first reverse at a flow rate of 380g / h, and mixed with a flow rate of 100g / h at the first reverse outlet Residual oil mixed oil enters secondary reaction to carry out hydrogenation reaction again, and the composition of 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 i...

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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 light olefins and single-ring aromatics from heavy hydrocarbons with a hydrogenation-catalytic cracking combined process method. Background technique [0002] The world's demand for light olefins and aromatics is increasing day by day. The method for producing low-carbon olefins, especially propylene, includes catalytic cracking processes in addition to steam cracking methods. At present, catalytic cracking mainly uses hydrogenated or unhydrogenated vacuum distillate as raw material for cracking. For the method of maximizing the production of propylene from the deep cracking of heavy hydrocarbons as the raw material, if the raw material is not hydrogenated, it will not be conducive to environmental protection and cannot achieve a higher propylene yield. Hydrogenation of catal...

Claims

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Application Information

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Patent Type & Authority Patents(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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