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Processing method for by-products of ethylene equipment

A processing method and technology of an ethylene plant, which is applied in the processing field of by-products of an ethylene plant, can solve problems such as environmental pollution, low quality, and long process flow, and achieve the effects of simple process flow, good product quality, and increased added value

Active Publication Date: 2014-05-14
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] The methods disclosed in CN102041091A, CN101724423A, CN101724458A and CN101724448A are to first divide ethylene tar into light and heavy fractions, and then use a fixed-bed hydrotreating process to produce clean fuel oil. These methods all have problems such as poor quality of light diesel oil and long processing flow
In addition, because heavy benzene contains a certain amount of heterocyclic compounds such as O, S, N, etc., as solvent oil, it has a pungent odor in addition to poor stability. When it is directly used as fuel oil, it is not only of low quality but also pollutes the environment. There are problems of poor product quality, lack of competitiveness or environmental pollution

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  • Processing method for by-products of ethylene equipment

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Embodiment 1

[0044] See Table 3 for the thermal cracking / catalytic reaction process conditions of the ethylene tar and heavy benzene mixed raw materials, the yields of the gas products, liquid products, and residues, and the properties of the heavy fraction. The catalyst used in the catalytic reaction zone is HC-1 molecular sieve catalyst, and the catalyst dosage is 1.5wt% of ethylene tar. The light ends and ethylene cracking C 9 The hydrofinishing process conditions of component mixed raw materials are shown in Table 4, in which the volume ratio of pre-hydrofinishing catalyst to hydrofining catalyst is 3:1. The process conditions of the heavy fraction hydrofining / hydrocracking are shown in Table 5, wherein the volume ratio of the hydroprotecting agent, the hydrofining catalyst, and the hydrocracking catalyst is 10:60:30. The properties of the gasoline fraction and diesel fraction obtained at the end of the reaction are shown in Table 6.

Embodiment 2

[0046] Compared with Example 1, the catalyst used in the catalytic reaction zone is a ZSM-5 molecular sieve catalyst. The light ends and ethylene cracking C 9 The hydrofinishing process conditions of component mixed raw materials are shown in Table 4, in which the volume ratio of the pre-hydrofinishing catalyst to the hydrofining catalyst is 1:2. The conditions of the heavy fraction hydrofining / hydrocracking process are shown in Table 5, wherein the volume ratio of the hydrotreating agent, hydrofining catalyst, and hydrocracking catalyst is 15:50:35, and the reaction results are shown in Table 6.

Embodiment 3

[0048] Compared with Example 1, the catalysts used in the catalytic reaction zone are HC-1 molecular sieve catalyst and ZSM-5 molecular sieve catalyst, and the volume ratio of the two catalysts is 1:1. The light ends and ethylene cracking C 9 The hydrofinishing process conditions of component mixed raw materials are shown in Table 4, in which the volume ratio of the pre-hydrofinishing catalyst to the hydrofinishing catalyst is 1:1. The process conditions of the heavy fraction hydrofining / hydrocracking are shown in Table 5, wherein the volume ratio of the hydroprotecting agent, the hydrofining catalyst, and the hydrocracking catalyst is 10:60:30. The reaction results are shown in Table 6.

[0049]

[0050] Table 1 Properties of ethylene tar

[0051] crude oil name Ethylene tar Density (20℃), kg·m -3 1090.5 S, μg g -1 355 N, μg·g -1 187 Four components, wt% Saturation 2.57 Aroma 45.50 colloid 29.93 Asphaltenes 2...

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Abstract

The invention discloses a processing method for by-products of ethylene equipment. The method includes: mixing ethylene tar and heavy benzene, passing the mixture firstly through a thermal cracking reaction area and a catalytic reaction area, condensing the reaction effluent, then leading the condensed product into an oil-water separator to undergo gas-liquid separation so as to obtain a gas product and a liquid phase oil product respectively, remaining the residue generated during reaction in the cracking reaction area, collecting the gas product to serve as a fuel gas, fractionating the liquid phase oil product to obtain light fraction and heavy fraction, mixing the light fraction with ethylene cracked C9 fraction, then leading the mixture into a hydrofining reaction area, passing the heavy fraction through the hydrofining reaction area and a hydrocracking reaction area in order, mixing the hydrocracking product with the light fraction hydrofining product and bringing the mixture into a separation system to undergo separation, thus obtaining gasoline and diesel fractions. According to the method provided by the invention, full-range ethylene tar can be fully utilized, and the obtained gasoline fraction yield is greater than 70%, the obtained gasoline and diesel have good quality, and the added value of ethylene tar is improved.

Description

technical field [0001] The present invention relates to a kind of processing method of by-product of ethylene plant, in particular to a kind of process of treating ethylene tar, heavy benzene and ethylene cracking C by thermal cracking / catalysis / hydrogenation 9 Fraction method. Background technique [0002] At present, the world's oil resources are increasingly scarce and the price is increasing. On the other hand, with the improvement of people's living standards, the demand for clean motor transportation fuels is increasingly strong. This contradiction makes it necessary for refineries to reduce emissions and increase efficiency, and it is of practical significance to convert the by-products of refineries that have not been fully utilized into clean fuel oil. [0003] Ethylene tar is a high-temperature condensation product of ethylene cracking raw materials and products in the steam cracking process. Its initial boiling point is 170-260°C, and its final boiling point is &...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G67/14
Inventor 关明华许杰张忠清姚春雷
Owner CHINA PETROLEUM & CHEM CORP
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