A method for removing olefins from a reformate

Abstract

The present application relates to a kind of methods for removing olefin from reforming oil, which comprises: reforming oil, hydrogenation adjuvant and hydrogenation catalyst are contacted to carry out the hydrogenation reaction of olefin;Wherein, the hydrogenation adjuvant is selected from the combination of one or more of norbornene, C2-C6 olefin group substituted norbornene, styrene, 1-butene, cyclopentene and dicyclopentadiene.The method for removing olefin from reforming oil of the present application promotes the selective hydrogenation of olefin in reforming oil by introducing hydrogenation adjuvant into the reaction system to remove olefin, the whole reaction process has less side reaction, the removal rate of olefin is high and the loss rate of aromatic hydrocarbon is low, the efficient removal of olefin in reforming oil is realized;The method is simple and easy to operate, low in cost, the reaction process is mild, it has important significance for petrochemical field, and has wide industrial application prospect.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of petroleum chemical industry, in particular to a method for removing olefins from reforming oil. BACKGROUND

[0002] Reforming oil can be used to produce aromatic chemicals such as BTX (benzene, toluene and xylene). However, a small amount of olefins is mixed in the reforming oil, which needs to be removed to achieve purification and separation. Therefore, continuous removal of olefins from reforming oil is of great significance to the chemical industry.

[0003] Since the hydrogenation side reaction of aromatics is prone to occur at high temperature, it is particularly important to remove olefins from reforming oil at low temperature and high efficiency. The existing technology mainly starts from developing new catalysts, such as patent CN1045305C which uses non-noble metal (such as Co-Mo or Ni-Mo / Al2O3) or noble metal (Pt, Pd / Al2O3) catalyst to selectively hydrogenate and remove olefins in reforming oil. The reaction temperature of non-noble metal catalyst is high (generally around 300-330℃), and the loss of aromatics is large. The cost of noble metal catalyst is high.

[0004] Based on the current situation of serious loss of aromatics and high cost in removing olefins from reforming oil, how to develop a method for removing olefins from reforming oil with high efficiency and low loss of aromatics is a technical problem to be solved.

[0005] It should be noted that the information disclosed in the foregoing background section is only used to strengthen the understanding of the background of the present application, and therefore it can include information which does not constitute prior art known to those skilled in the art. SUMMARY

[0006] The present application provides a method for removing olefins from reforming oil, which aims to efficiently remove olefins in reforming oil while keeping low loss of aromatics.

[0007] The present application relates to a method for removing olefins from reforming oil, which comprises: contacting reforming oil, a hydrogenation aid and a hydrogenation catalyst to carry out hydrogenation reaction of olefins; wherein the hydrogenation aid is selected from one or more combinations of norbornene, C2-C6 olefin-substituted norbornene, styrene, 1-butene, cyclopentene and dicyclopentadiene.

[0008] Optionally, the C2-C6 olefin-substituted norbornene is selected from one or more combinations of vinyl norbornene, propenyl norbornene and butenyl norbornene.

[0009] Optionally, the mass ratio of the hydrogenation aid to the reforming oil is 1:(1-1000); preferably, the mass ratio of the hydrogenation aid to the reforming oil is 1:(1-100).

[0010] Optionally, the hydrogenation catalyst comprises an active component and a support; the active component is selected from one or more combinations of Ni, Mo, W, Co, Pd, Pt and Rh; the support is selected from one or more combinations of SiO2, C, Al2O3 and molecular sieves.

[0011] Optionally, the active component is selected from one or more combinations of Ni, Pd and Pt, and the support is selected from one or more combinations of SiO2, C and Al2O3.

[0012] Optionally, the hydrogenation reaction is carried out in a fixed-bed reactor.

[0013] Optionally, the conditions for the hydrogenation reaction include: a reaction temperature of 10℃ to 200℃, a hydrogen pressure of 0.1 MPa to 10 MPa, and a mass hourly space velocity of 0.1 h⁻¹. -1 ~50h -1 The hydrogen-to-oil volume ratio is 10–1000.

[0014] Optionally, contacting the reformate, hydrotreating aid, and hydrotreating catalyst includes: dissolving the hydrotreating aid in the reformate, then feeding it into the fixed-bed reactor to contact the hydrotreating catalyst, and introducing hydrogen gas.

[0015] Optionally, the hydrogenation reaction is carried out in a high-pressure reactor.

[0016] Optionally, the conditions for the hydrogenation reaction include: a reaction temperature of 10℃ to 200℃, a hydrogen pressure of 0.1MPa to 10MPa, a reaction time of 0.1h to 10h, a stirring speed of 400r / min to 1000r / min, and a mass ratio of the hydrogenation catalyst to the reformate of 1:(1 to 500).

[0017] Beneficial effects:

[0018] The method for removing olefins from reformed oil of the present invention promotes the selective hydrogenation of olefins in reformed oil to remove olefins by introducing a hydrogenation aid into the reaction system. The entire reaction process has few side reactions, a high olefin removal rate and a low aromatic loss rate, achieving efficient removal of olefins from reformed oil. The method is simple, easy to implement, low in cost, and the reaction process is mild. It is of great significance to the petrochemical field and has broad prospects for industrial application. Detailed Implementation

[0019] The present application will be further described in detail below through embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more apparent.

[0020] The term “exemplary” as used herein means “serving as an example, embodiment, or illustration.” Any embodiment illustrated herein as “exemplary” is not necessarily to be construed as superior to or better than other embodiments.

[0021] Furthermore, the technical features involved in the different embodiments of this application described below can be combined with each other as long as they do not conflict with each other.

[0022] This invention relates to a method for deolefination of reformate, the method comprising: contacting the reformate, a hydrotreating agent, and a hydrotreating catalyst to perform a hydrogenation reaction of olefins; wherein the hydrotreating agent is selected from one or more combinations of norbornene, C2-C6 olefin-substituted norbornene, styrene, 1-butene, cyclopentene, and dicyclopentadiene.

[0023] It should be noted that, firstly, in the method for deolefin removal from reformed oil of the present invention, reformed oil, hydrogenation aid, and hydrogenation catalyst are contacted to carry out olefin hydrogenation reaction. By introducing the hydrogenation aid into the reaction system for deolefin removal from reformed oil, selective hydrogenation of olefins in reformed oil is promoted. Through the olefin hydrogenation reaction, olefins in reformed oil can be removed with a high olefin removal rate and a low aromatic loss rate, thus achieving efficient removal of olefins from reformed oil and providing a guarantee for the subsequent utilization of reformed oil.

[0024] Secondly, reforming oil and hydrotreating additives can be introduced into the hydrotreating reaction system simultaneously, contacting the hydrotreating catalyst while hydrogen is introduced to carry out the hydrotreating reaction; or, reforming oil and hydrotreating additives can be mixed first, and the mixed material can be used as raw material to enter the reaction system, contacting the hydrotreating catalyst while hydrogen is introduced to carry out the hydrotreating reaction.

[0025] According to a specific embodiment of the method of the present invention, the C2-C6 olefin-substituted norbornene is selected from one or more combinations of vinyl norbornene, propenyl norbornene, and butenyl norbornene.

[0026] It should be noted that in the C2-C6 olefin-substituted norbornene, the C2-C6 olefin group can be a straight-chain hydrocarbon group, and the connection position and mode of the olefin group can be similar to that of vinyl norbornene shown in formula (1) below. The olefin group can be attached to the 5-C position of norbornene. The hydrogenation accelerator can be a C2-C4 olefin-substituted norbornene, which can be pentenyl norbornene or hexenyl norbornene. Preferably, it is a combination of one or more of norbornene, vinyl norbornene, propenyl norbornene, and dicyclopentadiene.

[0027]

[0028] According to another specific embodiment of the method of the present invention, the mass ratio of the hydrotreating agent to the reformate is 1:(1-1000).

[0029] In a preferred embodiment of the method described in this invention, the mass ratio of the hydrotreating agent to the reformate is 1:(1-100).

[0030] It should be noted that in the method for deolefination of reformed oil of the present invention, the reformed oil, the hydrotreating agent and the hydrotreating catalyst are contacted to carry out the olefin hydrotreating reaction. The olefins carried out in the hydrotreating reaction include olefins in the reformed oil and one or more combinations of norbornene, C2-C6 olefin-substituted norbornene, styrene, 1-butene, cyclopentene and dicyclopentadiene, etc., which are used as hydrotreating agents.

[0031] The reformed oil product after olefin removal by the method of this invention contains a small amount of hydrogenated product from the hydrogenation additive. Because the amount of hydrogenation additive is very small, the reformed oil product after olefin removal can be used directly without separation and purification when the purity requirement is not high. For example, when the product is used for oil combustion, separation and purification are not required. Alternatively, if a certain purity requirement is required, such as when the reformed oil product after olefin removal is used to prepare aromatic products, the method of this invention may further include a separation and purification step after the hydrogenation reaction to separate the product from the hydrogenation additive. The separation and purification method can be a conventional method in the art, such as distillation, rectification, chemical purification, etc., and this invention is not limited thereto.

[0032] It should be noted that when the mass ratio of the hydrogenation aid to the reformate is within the above-mentioned preferred range, the olefins in the reformate can be removed with a higher olefin removal rate after the olefin hydrogenation reaction. Specifically, the mass ratio of the hydrogenation aid to the reformate can also be 1:20, 1:50, 1:60, 1:80, 1:90, 1:150, 1:200, 1:220, 1:250, 1:300, 1:400, 1:500, 1:600, 1:700, 1:800, 1:900, etc.

[0033] According to a specific embodiment of the method of the present invention, the hydrogenation catalyst comprises an active component and a support; the active component is selected from one or more combinations of Ni, Mo, W, Co, Pd, Pt and Rh; the support is selected from one or more combinations of SiO2, C, Al2O3 and molecular sieves.

[0034] It should be noted that the method of the present invention, which improves the olefin removal rate in reformate by adding a hydrogenation aid in the reaction system for removing olefins in reformate while maintaining a low aromatic loss rate, has a wide range of applicability. Catalysts based on the above-mentioned active components and supports can all be used in the method of the present invention to effectively remove olefins from reformate.

[0035] In a preferred embodiment of the method described in this invention, the active component is selected from one or more combinations of Ni, Pd and Pt, and the support is selected from one or more combinations of SiO2, C and Al2O3.

[0036] It should be noted that, based on the catalyst composed of the above-mentioned preferred active components and support, when carrying out the method for deolefin removal from reformed oil according to the present invention, the catalyst and hydrogenation aid can better exert a synergistic effect, so that olefins in reformed oil can be better removed.

[0037] According to one specific embodiment of the method of the present invention, the hydrogenation reaction is carried out in a fixed-bed reactor.

[0038] It should be noted that the method for deolefin removal from reformed oil of the present invention has wide applicability and can be carried out well in a variety of reactors.

[0039] According to an embodiment of the method of the present invention carried out in a fixed-bed reactor, the conditions for the hydrogenation reaction include: a reaction temperature of 10°C to 200°C, a hydrogen pressure of 0.1 MPa to 10 MPa, and a mass hourly space velocity of 0.1 h⁻¹. -1 ~50h -1 The hydrogen-to-oil volume ratio is 10–1000.

[0040] It should be noted that when the method of the present invention is carried out in a fixed-bed reactor, the reformate and hydrotreating agent can be mixed first and then fed into the fixed-bed reactor. Under the above reaction conditions, olefins in the reformate can be removed at a higher removal rate, and the aromatic loss rate is low. The specific reaction temperature can be 20℃, 40℃, 60℃, 70℃, 75℃, 80℃, 90℃, 100℃, 103℃, 110℃, 116℃, 124℃, 136℃, 141℃, 159℃, 168℃, 180℃, 190℃, etc. Optionally, the reaction temperature is 40℃~160℃. The hydrogen pressure can be 0.2MPa, 0.7MPa, 1MPa, 2MPa, 3.5MPa, 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, etc. Optionally, the hydrogen pressure is 2MPa~7MPa. Mass hourly space velocity can be 0.1 h. -1 0.5h -1 1h -1 2h -14h -1 10h -1 25h -1 37h -1 45h -1 50h -1 The hydrogen-to-oil volume ratio can be 100, 220, 350, 490, 550, 760, 880, 1000, 1600, 2000, etc.

[0041] According to an embodiment of the method of the present invention carried out in a fixed-bed reactor, contacting reformate, hydrotreating agent and hydrotreating catalyst includes: dissolving the hydrotreating agent in the reformate, then feeding it into the fixed-bed reactor to contact the hydrotreating catalyst, and introducing hydrogen gas.

[0042] It should be noted that when the method of the present invention is carried out in a fixed-bed reactor, the hydrogenation aid is first dissolved in the reformate, and then fed into the fixed-bed reactor to contact the hydrogenation catalyst for hydrogenation reaction. In this way, the entire reaction can be carried out more stably and continuously, and can better achieve a high olefin removal rate while maintaining a low aromatic loss rate.

[0043] In another specific embodiment of the method according to the present invention, the hydrogenation reaction is carried out in a high-pressure reactor.

[0044] It should be noted that, as can be seen from the above, the method of the present invention can be carried out in a fixed-bed reactor or a high-pressure reactor, both of which can effectively remove olefins from reformate. However, the method of removing olefins from reformate in the present invention is not limited to a certain fixed reactor. Any method that introduces the hydrogenation additive during the hydrogenation deolefination reaction of reformate falls within the protection scope of the present invention.

[0045] According to an embodiment of the method of the present invention carried out in a high-pressure reactor, the conditions for the hydrogenation reaction include: a reaction temperature of 10℃ to 200℃, a hydrogen pressure of 0.1MPa to 10MPa, a reaction time of 0.1h to 10h, a stirring speed of 400r / min to 1000r / min, and a mass ratio of the hydrogenation catalyst to the reformate of 1:(1 to 500).

[0046] It should be noted that when carrying out the method of the present invention in a high-pressure reactor, the reformate can first be mixed with the hydrotreating agent, then placed in the high-pressure reactor, and a hydrotreating catalyst can be added to the high-pressure reactor. Under a hydrogen atmosphere, the reformate and the hydrotreating catalyst undergo a selective hydrotreating reaction. When the method of the present invention is carried out in a high-pressure reactor under the above reaction conditions, olefins in the reformate can be removed at a higher removal rate while maintaining a low aromatics loss rate.

[0047] It should be noted that, specifically, when carrying out the method of the present invention in a high-pressure reactor, the reaction temperature can be 20℃, 40℃, 60℃, 70℃, 75℃, 80℃, 90℃, 100℃, 103℃, 110℃, 116℃, 124℃, 136℃, 141℃, 159℃, 168℃, 180℃, 190℃, etc. Optionally, the reaction temperature is 40℃~160℃. The hydrogen pressure can be 0.2MPa, 0.7MPa, 1MPa, 2MPa, 3.5MPa, 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa, etc., preferably 2MPa~7MPa. The reaction time can be 0.1h, 0.5h, 1h, 2h, 4h, 10h, etc., optionally 0.5h~4h. The stirring speed can be 400 r / min, 500 r / min, 670 r / min, 800 r / min, 950 r / min, 1000 r / min, etc. The mass ratio of the hydrogenation catalyst to the reformate can be 1:10, 1:20, 1:25, 1:30, 1:35, 1:40, 1:45, 1:50, 1:60, 1:70, 1:80, 1:90, 1:100, 1:150, 1:200, 1:220, 1:250, 1:280, 1:300, 1:350, 1:400, etc.

[0048] In summary, in the method for deolefin removal from reformed oil of the present invention, by adding the aforementioned hydrogenation aid to the reaction system for deolefin removal from reformed oil, the selective removal of olefins from reformed oil is better promoted, the selective hydrogenation deolefin removal reaction in reformed oil is more effectively completed, and the aromatic components in the reformed oil are well retained. The method of the present invention has relatively mild reaction conditions and low cost. It is applicable to various reactors, such as fixed-bed reactors or high-pressure reactors, and has wide applicability, representing a significant breakthrough for scientific research and practical production in the petrochemical field.

[0049] The present invention will be further described in detail below through examples, but these examples do not limit the invention. Unless otherwise specified, all reagents and other materials used in the following examples are commercially available finished products.

[0050] The 20% Ni / SiO2 catalyst used in the following examples was synthesized using the method disclosed in patent ZL201811408739.0; the Raney Ni catalyst was sourced from Macklin, catalog number N858485 on the Innocare platform, with a purity ≥99% and a Ni mass content ≥47%; the 0.5% Pd / C catalyst was sourced from Alfa, catalog number 038289 on the Innocare platform; and the 3% Co-11% Mo / γ-Al2O3 catalyst was sourced from Alfa, catalog number 045579 on the Innocare platform. The bromine index of the reformed oil before the reaction in the following examples was 0.6 mgBr / 100g oil.

[0051] The calculation method is explained in the following examples:

[0052]

[0053]

[0054] It should be noted that in the formula for calculating the olefin removal rate, the olefin concentration at the end of the reaction refers to the concentration of olefins in the reformate after the reaction, while the olefin concentration before the reaction refers to the concentration of olefins in the reformate before the reaction. Similarly, in the formula for calculating the aromatics loss rate, the aromatics concentration at the end of the reaction refers to the concentration of aromatics in the reformate after the reaction, while the aromatics concentration before the reaction refers to the concentration of aromatics in the reformate before the reaction. The concentrations of olefins or aromatics in the reformate before or after the reaction can be determined by chromatography.

[0055] Example of preparation of 20% Ni / SiO2 catalyst:

[0056] 290g of Ni(NO3)2·6H2O and 773g of silica sol (30% solid content) were weighed and dissolved in deionized water to prepare solution a with a concentration of 1.0 mol / L (based on Ni ions). A 1.0 mol / L sodium hydroxide solution b was prepared. While keeping solution a stirred, solution b was slowly added to solution a until the pH of the system reached 10.5. After the addition was complete, stirring was continued for 1 hour, then stirring was stopped, and the mixture was allowed to stand for 8 hours to age. The precipitate was then filtered and washed until neutral. The filter cake was dried in a forced-air drying oven at 110℃ for 12 hours, and then calcined in a muffle furnace at 500℃ for 3 hours to obtain a nickel-silicon composite oxide. Finally, the above nickel-silicon composite oxide was reduced with hydrogen to obtain a 20% Ni / SiO2 catalyst.

[0057] Example 1

[0058] 20.0 g of reformed oil, 0.1 g of vinyl norbornene, and 0.1 g of 20% Ni / SiO2 catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 3 MPa hydrogen. Stirring was started at 60 °C and the stirring speed was 600 r / min. The reaction time was 0.5 h. Ultimately, the olefin removal rate was 99.7%, and the aromatic hydrocarbon loss rate was 0.2%.

[0059] Example 2

[0060] 20.0 g of reformed oil, 0.2 g of propylene-based norbornene, and 0.3 g of Raney Ni catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 5 MPa hydrogen. Stirring was started at 100 °C at a speed of 600 r / min, and the reaction time was 2 h. Ultimately, the olefin removal rate was 99.8%, and the aromatic hydrocarbon loss rate was 0.3%.

[0061] Example 3

[0062] 20.0 g of reformed oil, 0.1 g of dicyclopentadiene, and 0.1 g of 0.5% Pd / C catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 4 MPa hydrogen. Stirring was started at 60 °C and the stirring speed was 600 r / min. The reaction time was 1 h. Ultimately, the olefin removal rate was 99.5%, and the aromatic hydrocarbon loss rate was 0.1%.

[0063] Example 4

[0064] 3g of 20% Ni / SiO2 catalyst was used in a fixed-bed reactor for the deolefination reaction of reformed oil. Norbornene was dissolved in the reformed oil, with a norbornene mass fraction of 2%. The reaction temperature was 60℃, the hydrogen pressure was 3MPa, and the mass hourly space velocity (HHSV) was 10h. -1 The hydrogen-to-oil volume ratio was 800. Ultimately, after 1000 hours of continuous operation, the catalyst activity did not significantly decrease, the olefin removal rate was 99.8%, and the aromatics loss rate was 0.2%.

[0065] Example 5

[0066] 20.0 g of reformed oil, 0.1 g of dicyclopentadiene, and 0.1 g of 3% Co-11% Mo / γ-Al₂O₃ catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 4 MPa hydrogen. Stirring was started at 60 °C and the stirring speed was 600 r / min. The reaction time was 1 h. Ultimately, the olefin removal rate was 95.4%, and the aromatic hydrocarbon loss rate was 0.1%.

[0067] Example 6

[0068] 20.0 g of reformed oil, 0.1 g of cyclopentene, and 0.1 g of 20% Ni / SiO2 catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 3 MPa hydrogen. Stirring was started at 60 °C and the stirring speed was 600 r / min. The reaction time was 0.5 h. Ultimately, the olefin removal rate was 97.6%, and the aromatic hydrocarbon loss rate was 0.2%.

[0069] Comparative Example 1

[0070] 20.0 g of reformed oil and 0.1 g of 20% Ni / SiO2 catalyst were added to a 100 mL reactor. After tightening the reactor, the gas inside was purged with 3 MPa hydrogen. Stirring was started at 60 °C and the stirring speed was 600 r / min. The reaction time was 0.5 h. Ultimately, the olefin removal rate was 69.5%, and the aromatic hydrocarbon loss rate was 0.1%.

[0071] The results above show that the methods for removing olefins from reformed oil in Examples 1-6 of this invention have the advantages of mild reaction process, low cost, and low aromatic loss rate. Under the same reaction conditions, compared with Comparative Example 1 without the addition of hydrogenation aid (vinyl norbornene), the olefin removal rate of Example 1 is improved, indicating that the introduction of hydrogenation aid (vinyl norbornene) into the reaction system promotes the removal of olefins from reformed oil.

[0072] In summary, this invention promotes the removal of olefins by introducing a hydrogenation aid into the reaction system for deolefin removal from reformed oil, and is expected to be widely used in the future.

[0073] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. Those skilled in the art can understand the specific meaning of these terms in this application based on the specific circumstances.

[0074] The present application has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present application based on these embodiments, all of which fall within the protection scope of the present application.

Claims

1. A method for deolefin removal from reformed oil, characterized in that, The method includes: The reformate, hydrotreating additive, and hydrotreating catalyst are brought into contact to carry out the hydrogenation reaction of olefins. The hydrogenation aid is selected from one or more combinations of norbornene, C2-C6 olefin-substituted norbornene, cyclopentene, and dicyclopentadiene. The hydrogenation catalyst comprises an active component and a support. The active component is selected from one or more combinations of Ni, Mo, W, Co, Pd, Pt, and Rh; the support is selected from one or more combinations of SiO2, C, Al2O3, and molecular sieves. The mass ratio of the hydrotreating agent to the reformate is 1:(50-1000). The conditions for the hydrogenation reaction include: a reaction temperature of 10℃ to 200℃ and a hydrogen pressure of 0.1MPa to 10MPa.

2. The method according to claim 1, characterized in that, The C2-C6 olefin-substituted norbornene is selected from one or more combinations of vinyl norbornene, propenyl norbornene, and butenyl norbornene.

3. The method according to claim 1, characterized in that, The mass ratio of the hydrotreating agent to the reformate is 1:(50-100).

4. The method according to claim 1, characterized in that, The active component is selected from one or more combinations of Ni, Pd and Pt, and the support is selected from one or more combinations of SiO2, C and Al2O3.

5. The method according to any one of claims 1 to 4, characterized in that, The hydrogenation reaction is carried out in a fixed-bed reactor.

6. The method according to claim 5, characterized in that, The conditions for the hydrogenation reaction include: Mass hourly space velocity is 0.1 h. -1 ~50h -1 The hydrogen-to-oil volume ratio is 10~1000.

7. The method according to claim 5, characterized in that, Contacting reformate, hydrotreating additives, and hydrotreating catalysts includes: The hydrotreating agent is dissolved in the reformate and then fed into the fixed-bed reactor to contact the hydrotreating catalyst, and hydrogen is introduced.

8. The method according to any one of claims 1 to 4, characterized in that, The hydrogenation reaction is carried out in a high-pressure reactor.

9. The method according to claim 8, characterized in that, The conditions for the hydrogenation reaction include: The reaction time is 0.1 h to 10 h, the stirring speed is 400 r / min to 1000 r / min, and the mass ratio of the hydrogenation catalyst to the reformate is 1:(1~500).

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