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Method for producing ethylene cracking material through dry gas hydrogenation

An ethylene cracking and dry gas technology, which is applied in the processing of gas mixtures, the petroleum industry, and the treatment of hydrocarbon oils, etc., can solve the problems of concentrated reaction heat release, high hot spot temperature and temperature envelope, and large differences in dry gas composition.

Active Publication Date: 2017-05-31
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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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
[0008] In addition, the composition of dry gas produced by various enterprises is quite different. Generally, the olefin content in the dry gas produced is 4%~6%, and the oxygen content is 200~300 mg∙m -3 , but some enterprises produce dry gas with olefin content of 8%~14% and oxygen content of 5000~9000 mg∙m -3 , this kind of dry gas hydrogenation reaction heat is very large, if it is still produced according to CN103450941A, the reaction temperature will exceed the upper limit of catalyst use

Method used

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  • Method for producing ethylene cracking material through dry gas hydrogenation

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0064] The reaction adopts a fixed bed reactor with upper feed; the catalyst adopts four-stage packing, and the packing ratio is the same as that of Comparative Example 1. From top to bottom, the catalysts are A, B, A, D in sequence. Its physical properties are listed in Table 3. The hydrogenation feed gas is coking dry gas, whose composition is shown in Table 2. The reaction feed includes only coking dry gas. The reaction conditions and results are shown in Table 5.

[0065] From the reaction results in Table 5, it can be seen that if the catalyst grading scheme of the present invention is adopted and only a single coking dry gas feed is used for hydrogenation reaction, the temperature rise of the reaction bed is 259℃; Up to 41°C.

[0066] In addition, from the reaction results in Table 5, it can be seen that after adopting the catalyst grading scheme of the present invention, the maximum temperature of the reaction bed is 396°C, the hot spot temperature can be controlled with...

Embodiment 2

[0068] The reaction adopts a fixed bed reactor with upper feed; the catalyst adopts four-stage packing, and the packing ratio is the same as that of Comparative Example 1. From top to bottom, the catalysts are A, B, A, D in sequence. Its physical properties are listed in Table 3. The hydrogenation feed gas is coking dry gas, whose composition is shown in Table 2. In addition to the coking dry gas, the reaction feed also contains catalytic diesel, and the feed is fed in parallel with the coking dry gas. The main properties of catalytic diesel are shown in Table 4. The reaction conditions and results are shown in Table 5.

[0069] From the reaction results in Table 5, it can be seen that compared with Example 1, after the two improved methods of catalyst grading filling and introduction of catalytic diesel, the reaction "warm bulb" is further reduced, and the reaction temperature rise is reduced from the original 259°C. To 173°C; but the average reaction temperature was 312.4°C...

Embodiment 3

[0071] The reaction adopts a fixed bed reactor with upper feed; the catalyst adopts four-stage packing, and the packing ratio is the same as that of Comparative Example 1. From top to bottom, the catalysts are A, B, A, D, and their physical properties are listed in Table 3. The hydrogenation feed gas is coking dry gas, whose composition is shown in Table 2. In addition to the coking dry gas, the reaction feed is also fed with No. 5 jet fuel (RP-5), which is fed in parallel with the coking dry gas. The main properties of No. 5 jet fuel (RP-5) are shown in Table 4. The reaction conditions and results are shown in Table 5.

[0072] From the reaction results in Table 5, it can be seen that after the two improved methods of catalyst grading filling and No. 5 jet fuel (RP-5), the reaction "warm bulb" can also be greatly reduced, and the reaction temperature rise can be reduced from the original At 259°C, it was reduced to 173°C; but the average reaction temperature was 312.6°C, almo...

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Abstract

The present invention discloses a method for producing an ethylene cracking material through dry gas hydrogenation. According to the method, olefin-containing dry gas and optional supplemented hydrogen enter a fixed bed hydrogenation reactor in a co-current flow manner, and contact a hydrogenation catalyst under a hydrogenation process condition, a reaction is performed, and the obtained reaction products are separated to obtain the dry gas having the saturated olefin; and the hydrogenation reactor comprises four reaction sections, and according to the sequence of the contact between the material and the catalyst, the law of the hydrogenation activity metal contents in the catalysts in each reaction section is the low content, the high content, the low content and the high content. According to the present invention, with the method, the relatively average reaction rate of the inlet section of the catalyst bed layer is reduced, the problem that the relatively average reaction rate of the inlet section of the catalyst bed layer is high is solved, the difference among the average reaction rates of each section of the bed layer is substantially reduced, and the relatively average reaction rates of each section are uniform; and with the method, the deep oxygen removal can be ensured.

Description

Technical field [0001] The invention relates to a low-carbon olefin hydrotreating process, more specifically, a method for hydrogenating olefin-containing dry gas to prepare an ethylene cracking feed. Background technique [0002] At present, most of the raw materials used in ethylene plants in my country are naphtha (64% naphtha, 10% hydrogenation tail oil, 10% light diesel oil). Ethylene raw materials are the most important factor affecting the cost of ethylene. The proportion of total cost is 70% to 75%, or even higher. In recent years, domestic petrochemical companies have built or expanded a number of large-scale ethylene production plants. Although the sources of raw materials have been expanded in actual production, the raw materials for ethylene cracking are still very tight; in addition, the price of crude oil continues to rise, and the price of ethylene cracking raw material naphtha It also rises accordingly, and the economy of ethylene production equipment deteriorates...

Claims

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Application Information

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IPC IPC(8): C10G70/02
CPCC10G70/02
Inventor 艾抚宾袁毅乔凯祁文博徐彤方向晨刘平
Owner CHINA PETROLEUM & CHEM CORP
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