Method for producing ethylene cracking material by hydrogenation of dry gas

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

Active Publication Date: 2019-03-19
CHINA PETROLEUM & CHEM CORP +1
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  • Abstract
  • Description
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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

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  • Method for producing ethylene cracking material by hydrogenation of dry gas

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0064] A fixed-bed reactor was used for the reaction, and the feed was fed from above; the catalyst was loaded in four stages, and the loading ratio was the same as in Comparative Example 1. From top to bottom, the catalysts are A, B, A, D. Its physical properties are listed in Table 3. The feed gas for hydrogenation is coking dry gas, and its composition is shown in Table 2. The reaction feed consisted of coke dry gas only. The reaction conditions and results are shown in Table 5.

[0065] From the reaction results in Table 5, it can be seen that when the catalyst gradation 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°C; up to 41°C.

[0066] In addition, it can also be known from the reaction results in Table 5 that after adopting the catalyst gradation scheme of the present invention, the maximum temperature of the reaction bed is 396°C, the temperatur...

Embodiment 2

[0068] A fixed-bed reactor was used for the reaction, and the feed was fed from above; the catalyst was loaded in four stages, and the loading ratio was the same as in Comparative Example 1. From top to bottom, the catalysts are A, B, A, D. Its physical properties are listed in Table 3. The feed gas for hydrogenation is coking dry gas, and its composition is shown in Table 2. In addition to the coking dry gas, the reaction feed also includes catalytic diesel, which 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] It can be seen from the reaction results in Table 5 that, compared with Example 1, after adopting the two improved methods of catalyst gradation packing and introducing catalytic diesel oil, the reaction "temperature envelope" was further reduced, and the reaction temperature rise was reduced from the original 259°C. to 173°C; but the average...

Embodiment 3

[0071] A fixed-bed reactor was used for the reaction, and the feed was fed from above; the catalyst was loaded in four stages, and the loading ratio was the same as in Comparative Example 1. From top to bottom, the catalysts are A, B, A, D, and their physical properties are listed in Table 3. The feed gas for hydrogenation is coking dry gas, and its 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] It can be seen from the reaction results in Table 5 that after adopting the two improved methods of catalyst graded packing and No. 5 jet fuel (RP-5), the reaction "temperature envelope" can also be greatly reduced, and the reaction temperature rise is changed from the original 259°C, decreased to 173°C; but the average reac...

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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 hydrogenation treatment process, more specifically, a method for hydrogenating olefin-containing dry gas to prepare ethylene cracking material. Background technique [0002] At present, most of the raw materials used in my country's ethylene plants are naphtha (naphtha accounts for 64%, hydrogenated tail oil accounts for 10%, and light diesel oil accounts for 10%). Ethylene raw materials are the most important factor affecting the cost of ethylene. Raw materials It accounts for 70% to 75% of the total cost, or even higher. In recent years, domestic petrochemical enterprises have built and expanded several sets of large-scale ethylene production units. Although the source of raw materials has been expanded in actual production, the raw materials for ethylene cracking are still quite tight; It also rises accordingly, and the economics of ethylene production units become worse. The reality forces companies to ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
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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