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A process for preparing ethylene cracking material by hydrogenation of dry gas

A technology for ethylene cracking and hydrogen production, which is used in the processing of gas mixtures, the petroleum industry, and the treatment of hydrocarbon oil. , to avoid the effect of concentrated release

Active Publication Date: 2019-01-25
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Solved three of the above four difficulties, and compared with CN1800308A, it also simplified the process, but the problem of concentrated heat release and excessively high hot spot temperature (or temperature bulb) was still unsolved

Method used

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  • A process for preparing ethylene cracking material by hydrogenation of dry gas
  • A process for preparing ethylene cracking material by hydrogenation of dry gas
  • A process for preparing ethylene cracking material by hydrogenation of dry gas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0047] A fixed-bed reactor was used for the reaction, and the materials were fed from above. The catalysts listed in Table 3 were used. The raw material gas for hydrogenation was coking dry gas, and the composition was shown in Table 2. In addition to the coking dry gas, the reaction feed also includes refined naphtha, which is fed in parallel with the coking dry gas. The main properties of refined naphtha are shown in Table 5. The reaction conditions and results are shown in Table 6.

[0048] Table 5 Main properties of refined naphtha

[0049]

[0050] Table 6 Operating conditions and results of hydrogenation reactor

[0051]

[0052] 1-5*, is the temperature of different bed heights along the dry gas feeding direction.

[0053] From the reaction results in Table 6, it can be seen that after the introduction of refined naphtha, the reaction "temperature envelope" was greatly reduced, and the reaction temperature rise was reduced from the original 110°C to 66.7°C; but...

Embodiment 2

[0055] A fixed-bed reactor was used for the reaction, and the materials were fed from above. The catalysts listed in Table 3 were used. The raw material gas for hydrogenation was coking dry gas, and the composition was shown in Table 2. In addition to the coking dry gas, the reaction feed is also fed into the catalytic diesel, which is fed in parallel with the coking dry gas. The main properties of catalytic diesel are shown in Table 7. The reaction conditions and results are shown in Table 8.

[0056] Table 7 Main properties of catalytic diesel

[0057]

[0058] Table 8 Hydrogenation reactor operating conditions and results

[0059]

[0060] 1-5*, is the temperature of different bed heights along the dry gas feeding direction.

[0061] From the reaction results in Table 8, it can be seen that after the introduction of catalytic diesel oil, the "temperature envelope" of the reaction can also be greatly reduced, and the reaction temperature rise is reduced from the ori...

Embodiment 3

[0063] The reaction adopts a fixed-bed reactor with upper feed, and uses the catalysts listed in Table 3. The feed gas for hydrogenation is thermally cracked dry gas, and its composition is shown in Table 2. In addition to the thermal cracking dry gas, the reaction feed also feeds a piece of catalytic diesel oil, which is fed in parallel with the thermal cracking dry gas. The main properties of catalytic diesel are shown in Table 7. The reaction conditions and results are shown in Table 9.

[0064] Table 9 Operating conditions and results of hydrogenation reactor

[0065]

[0066] *: Since the total amount of olefins in the feed gas is 8.83v%, while the hydrogen content is only 7.781v%, so when hydrogenation reaction is carried out, hydrogen should be supplemented according to about 5% of the dry gas feed amount.

[0067] From the reaction results in Table 9, it can be seen that after the introduction of catalytic diesel oil, the reaction "temperature envelope" can also ...

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Abstract

The invention discloses a process for preparing an ethylene cracking material through hydrogenation of dry gas. The process comprises the following steps: introducing dry gas containing olefin, optional supplementing hydrogen and distillate oil into a fixed-bed reactor; allowing the above mentioned substances to contact with a hydrogenation catalyst under the hydrogenation process conditions for a reaction; and separating reaction products so as to obtain dry gas with saturated olefin, wherein at least a part of the distillate oil is in a liquid phase under the reaction conditions. The process provided by the invention can control the speed of an olefin hydrogenation reaction, allows the conversion rate of the olefin hydrogenation reaction to be gradually increased along a feeding direction and enables reaction heat to be gradually and smoothly released and reaction temperature rise of a catalyst bed to be decreased, so the service life of the catalyst is prolonged.

Description

technical field [0001] The invention relates to a low-carbon olefin hydrogenation treatment process, more specifically, a process method for hydrogenating olefin-containing dry gas to prepare ethylene cracking material. Background technique [0002] The raw material used in the initial design of my country's ethylene plant is mainly naphtha. Ethylene raw materials are the most important factor affecting the cost of ethylene, and raw materials account for 70% to 75% of the total cost. In recent years, domestic petrochemical enterprises have newly built and expanded several sets of large-scale ethylene production units. Although the sources of raw materials have been expanded in actual production, the raw materials for ethylene cracking are still quite tight. In addition, in recent years, the price of crude oil has continued to rise, and the price of naphtha, the raw material for ethylene cracking, has also risen accordingly, and the production economy of enterprises has dete...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G70/02
CPCC10G70/02C10G2300/1037C10G2300/1088
Inventor 艾抚宾徐彤祁文博乔凯方向晨袁毅徐大海杨成敏刘平
Owner CHINA PETROLEUM & CHEM CORP
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