A hydrocracking process for the conversion of hydrocarbons

Abstract

The present application relates to the technical field of refinery light oil hydroconversion, and discloses a hydrocracking method for hydrocarbon conversion, which comprises the following steps: introducing refinery light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst under low-pressure hydrogen conditions to perform a hydrocracking reaction, so as to obtain a hydrocracking product; and sequentially performing gas-liquid separation and fractionation on the hydrocracking product, so as to obtain light naphtha and a gas product rich in propane. The method can convert saturated hydrocarbons into small-molecule hydrocarbons under low-pressure hydrocracking conditions, especially maximize the propane yield and the n-butane selectivity, and can provide high-quality raw materials for chemical plants.

Description

Technical Field

[0001] This invention relates to the field of light oil hydroconversion technology in refineries, and specifically to a hydrocracking method for hydrocarbon conversion. Background Technology

[0002] In recent years, the energy consumption structure has shifted towards clean and environmentally friendly energy sources such as natural gas and electricity. The demand for fuel oil, represented by gasoline, has gradually reached its peak. Refinery light oil, represented by light naphtha and aromatic residue oil, urgently needs a high-value utilization method.

[0003] Meanwhile, the market demand for chemical products has been increasing year by year, which has driven the increase in the production scale of chemical feedstocks such as ethylene and propylene. The best feedstock for chemical plants such as ethylene plants is low-carbon n-alkanes. Therefore, using low-sulfur and low-nitrogen naphtha fractions as feedstock to produce propane, while also producing some low-carbon n-alkanes as by-products, can provide high-quality feedstocks for chemical plants and solve the problem of excess low-value-added naphtha fraction resources in refineries.

[0004] Existing hydrocracking units mainly produce wax oil or diesel oil, requiring refining before cracking, and the unit pressure is often between 10.0 and 15.0 MPa. In addition, the mass fraction of isomeric hydrocarbons in light naphtha produced by conventional hydrocracking units is about 40% to 60%, while that of n-hydromeric hydrocarbons is only 10% to 20%, which is not suitable as a high-quality chemical feedstock.

[0005] CN106062148A discloses a process for converting hydrocarbons into olefins. Hydrocarbon feedstocks, represented by naphtha, are separated into multiple streams classified by carbon number through a hydrocracking unit. Suitable streams are then fed into subsequent steam cracking, propane dehydrogenation, and butane dehydrogenation units to produce olefins. The hydrocracking unit conditions include a temperature of 470-550℃, a gauge pressure of 0.6-3.0 MPa, and a heating time of 0.2-10 h. -1 Mass airspeed.

[0006] CN112409121A discloses a method for converting light naphtha into low-carbon olefins and aromatics. Light naphtha with a C5 and C6 alkane content of 99% undergoes isomerization separation. The isomerized components are fed into a hydrocracking unit and separated to obtain refinery dry gas, propane, n-butane, and isobutane. These components are then further converted into ethylene and propylene through steam cracking or propane dehydrogenation units. The hydrocracking unit conditions include a temperature of 330–360°C and a gauge pressure of 6–8 MPa. After separation in the hydrocracking unit, the proportions of refinery dry gas, propane, n-butane, and isobutane are 6%, 31%, 29%, and 34%, respectively.

[0007] WO2019162392A1 discloses a method for catalytically converting alkanes and cycloalkanes from naphtha feedstock into propane via hydrocracking. The method involves mixing olefin-free naphtha feedstock with hydrogen and then catalytically converting the propane at a temperature of 200–600°C, a pressure of 1–10 MPa, and a feed mass hourly space velocity of 0.1–10.0 h⁻¹. -1 Hydrocracking reaction is carried out on a bifunctional catalyst under conditions of hydrogen-to-oil molar ratio of 1 to 1000. The catalyst used contains one or more of ZSM, MEL or SAPO type molecular sieves with acidic 10-membered ring channels.

[0008] CN13307717A discloses a method for producing propane through hydroconversion of light hydrocarbons. The method involves heating light hydrocarbon feedstock, hydrogen-rich gas, and recycled light hydrocarbons, followed by catalytic cracking under acidic catalyst conditions. The reaction products, after cooling and fractionation, yield dry gas, propane, and aromatic gasoline components, respectively. The feedstock used in this method has an alkane content greater than 50 wt% and a carbon number range of C4 to C13. The reaction temperature is 250–550 °C, the pressure is 0.01–5.0 MPa, and the mass hourly space velocity (HHSV) is 0.1–5.0 h⁻¹. -1 The hydrogen-to-oil ratio is 30–800:1, and the catalyst is HZSM-5 molecular sieve.

[0009] However, the aforementioned existing technologies all suffer from drawbacks such as harsh reaction conditions and limited adaptability of raw materials. Summary of the Invention

[0010] The purpose of this invention is to provide a method for converting low-carbon hydrocarbons to produce both propane and n-butane, addressing the problem of excess light alkanes in refineries.

[0011] To achieve the above objectives, the present invention provides a hydrocracking method for hydrocarbon conversion, the method comprising:

[0012] (1) Under low-pressure hydrogenation conditions, refinery light oil is introduced into a hydrocracking reaction zone packed with hydrocracking catalyst to carry out hydrocracking reaction, and hydrocracking products are obtained; the refinery light oil has a saturated hydrocarbon content of 90wt% to 100wt%; the hydrocracking catalyst contains an active metal component and a support, the support contains an acidic component, the acidic component is a ZSM molecular sieve and / or a modified product of ZSM molecular sieve; the content of the active metal component, calculated as oxides, is 10wt% to 50wt% based on 100% of the weight of the hydrocracking catalyst; the content of the acidic component, calculated as oxides, is 45wt% to 80wt% based on 100% of the weight of the support of the hydrocracking catalyst.

[0013] (2) The hydrocracking products are subjected to gas-liquid separation and fractionation in sequence to obtain light naphtha products and gas products containing propane and n-butane, wherein the propane content in the gas products is not less than 50 wt% and the n-butane selectivity is not less than 48%.

[0014] The n-butane selectivity = (mass yield of n-butane in the gaseous product / sum of mass yield of C4 component in the gaseous product) * 100%;

[0015] The conditions for the hydrocracking reaction are controlled such that the conversion rate of the hydrocracking reaction zone is 40% to 98%.

[0016] The conversion rate = (1 - mass percentage of C5 and above hydrocarbons in the liquid product of the hydrocracking product * yield of the liquid product of the hydrocracking product / mass percentage of C5 and above hydrocarbons in the refinery light oil) * 100%.

[0017] The hydrocracking method of the present invention can convert alkanes and cycloalkanes with carbon numbers ranging from C5 to C12 into propane and small amounts of other low-carbon hydrocarbons under relatively low pressure conditions.

[0018] The method of this invention enables the conversion of saturated hydrocarbons into small molecule hydrocarbons from low-nitrogen naphtha feedstock under low-pressure hydrocracking conditions, particularly maximizing the yield of propane and the selectivity of n-butane, thus providing high-quality feedstock for chemical plants. Attached Figure Description

[0019] Figure 1 This is a schematic flowchart of a hydrocracking method for hydrocarbon conversion described in this invention.

[0020] Explanation of reference numerals in the attached figures

[0021] Numbers 1, 3, 5, 7, 9, 11, 12, 14, 15, and 16 are all pipelines.

[0022] 2: Raw material oil pump

[0023] 4: Heating furnace

[0024] 6: Hydrocracking Reaction Zone

[0025] 8: High-pressure separator

[0026] 10: Gas purification unit

[0027] 13: Fractionation Unit Detailed Implementation

[0028] The endpoints and any values ​​of the ranges disclosed herein are not limited to the precise ranges or values, and these ranges or values ​​should be understood to include values ​​close to these ranges or values. For numerical ranges, the endpoint values ​​of the various ranges, the endpoint values ​​of the various ranges and individual point values, and individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed herein.

[0029] As mentioned above, this invention provides a hydrocracking method for hydrocarbon conversion, the method comprising:

[0030] (1) Under low-pressure hydrogenation conditions, refinery light oil is introduced into a hydrocracking reaction zone packed with hydrocracking catalyst to carry out hydrocracking reaction, and hydrocracking products are obtained; the refinery light oil has a saturated hydrocarbon content of 90wt% to 100wt%; the hydrocracking catalyst contains an active metal component and a support, the support contains an acidic component, the acidic component is a ZSM molecular sieve and / or a modified product of ZSM molecular sieve; the content of the active metal component, calculated as oxides, is 10wt% to 50wt% based on 100% of the weight of the hydrocracking catalyst; the content of the acidic component, calculated as oxides, is 45wt% to 80wt% based on 100% of the weight of the support of the hydrocracking catalyst.

[0031] (2) The hydrocracking products are subjected to gas-liquid separation and fractionation in sequence to obtain light naphtha products and gas products containing propane and n-butane, wherein the propane content in the gas products is not less than 50 wt% and the n-butane selectivity is not less than 48%.

[0032] The n-butane selectivity = (mass yield of n-butane in the gaseous product / sum of mass yield of C4 component in the gaseous product) * 100%;

[0033] The conditions for the hydrocracking reaction are controlled such that the conversion rate of the hydrocracking reaction zone is 40% to 98%.

[0034] The conversion rate = (1 - mass percentage of C5 and above hydrocarbons in the liquid product of the hydrocracking product * yield of the liquid product of the hydrocracking product / mass percentage of C5 and above hydrocarbons in the refinery light oil) * 100%.

[0035] More preferably, the conditions of the hydrocracking reaction are controlled such that the conversion rate of the hydrocracking reaction zone is 60% to 80%.

[0036] The method for calculating the yield of liquid products from hydrocracking products according to the present invention is as follows: yield of liquid products = mass of liquid products obtained after gas-liquid separation of hydrocracking products / mass of refinery light oil * 100%.

[0037] The method for calculating the mass yield of n-butane in the gaseous product of the present invention is as follows: mass of n-butane in the gaseous product / mass of the refinery light oil * 100%.

[0038] The method for calculating the sum of the mass yields of C4 components in the gaseous product of the present invention is as follows: (sum of the mass of C4 components in the gaseous product / mass of the refinery light oil) * 100%.

[0039] The method of the present invention may further include preheating the refinery light oil, either alone or together with hydrogen, before introducing it into the hydrocracking reaction zone for hydrocracking; for example, preheating it in a heater; and then introducing the preheated material into the hydrocracking reaction zone for the hydrocracking reaction. The present invention does not have particular requirements for the preheating temperature; it can be the temperature required for the hydrocracking reaction or slightly lower.

[0040] Preferably, the refinery light oil has a carbon number of C5 to C12, an alkanes content of 30% to 100% by weight, a cycloalkanes content of 0% to 70% by weight, and an aromatics content of 0% to 10% by weight.

[0041] More preferably, the alkanes content of the refinery light oil is 30% to 60% by weight; even more preferably, it is 35% to 55% by weight.

[0042] More preferably, the cycloalkanes content of the refinery light oil is 2% to 60% by weight; even more preferably, it is 35% to 55% by weight.

[0043] More preferably, the aromatic content of the refinery light oil is 0.1% to 8% by weight; even more preferably, it is 0.5% to 7% by weight.

[0044] Preferably, the density of the refinery light oil at 20°C is 0.70-0.75 g / cm³. 3 .

[0045] In a preferred embodiment, the refinery light oil is selected from at least one of reforming residue oil, straight-run naphtha, DCC gasoline hydrotreating unit residue oil, and hydrocracking naphtha.

[0046] According to a preferred embodiment, the nitrogen content in the refinery light oil is ≤20 μg / g.

[0047] In a particularly preferred embodiment, the pressure of the hydrocracking reaction is ≤8.0 MPa.

[0048] According to a preferred embodiment, the hydrocracking reaction is carried out at a temperature of 280–420°C, a pressure of 0.2–8.0 MPa, and a volume hourly space velocity of 0.1–20.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100–2000.

[0049] Preferably, a hydrogenation protection catalyst is packed upstream of the hydrocracking catalyst; based on the total catalyst volume in the hydrocracking reaction zone being 100%, the packing volume of the hydrogenation protection catalyst is 1% to 50%, and the packing volume of the hydrocracking catalyst is 50% to 99%.

[0050] Preferably, in the hydrocracking catalyst, the support further contains a heat-resistant inorganic oxide, which is selected from at least one of silicon oxide and aluminum oxide.

[0051] In a particularly preferred embodiment, the active metal element in the active metal component of the hydrocracking catalyst is selected from at least two of Group VIB and Group VIII metal elements; based on the total weight of the hydrocracking catalyst, the content of the Group VIB metal element is 5 wt% to 35 wt% and the content of the Group VIII metal element is 1 wt% to 8 wt% in terms of oxides.

[0052] Particularly preferably, in the hydrocracking catalyst, the content of the acidic component is 45% to 70 wt%, based on 100% of the weight of the support of the hydrocracking catalyst.

[0053] In a preferred embodiment, the hydrogenation protection catalyst contains a protective agent support and a protective agent active metal component. The protective agent support is alumina, and the protective agent active metal component contains at least one element selected from Group VIII metals and at least one element selected from Group VIB metals.

[0054] Particularly preferably, in the hydroprotection catalyst, based on the total weight of the hydroprotection agent, the content of the Group VIII metal element, calculated as oxides, is 0.3 wt% to 5 wt%, and the content of the Group VIB metal element is 1 wt% to 30 wt%. More preferably, in the hydroprotection catalyst, based on the total weight of the hydroprotection agent, the content of the Group VIB metal element, calculated as oxides, is 26 wt% to 30 wt%.

[0055] Preferably, in the hydrogenation protection catalyst, the active metal component of the protective agent contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

[0056] The gas-liquid separation of the present invention can be performed, for example, in a separator (e.g., a high-pressure separator). The gaseous product obtained after the gas-liquid separation can be purified and recycled back to the unit for the hydrocracking reaction. The liquid product obtained after the gas-liquid separation is preferably subjected to further fractionation to obtain the light naphtha product and the gaseous product with a propane content of not less than 40 wt%.

[0057] The light naphtha product obtained by this invention can be mixed with feedstock as unconverted oil according to production needs, and then recycled to the reaction system for complete conversion, or it can be withdrawn from the device. This invention does not have any particular requirements in this regard.

[0058] The following combination Figure 1 The schematic diagram of the process flow shown provides a preferred embodiment of a hydrocracking method for hydrocarbon conversion according to the present invention. Specifically, the method includes:

[0059] (1) Under low-pressure hydrogen conditions, refinery light oil is introduced into heater 4 for preheating via pipeline 1, feedstock pump 2 and pipeline 3 in sequence, and hydrogen is introduced into heater 4 via pipeline 16 to obtain preheated material; the preheated material is introduced into hydrocracking reaction zone 6, which is filled with hydrocracking protection catalyst and hydrocracking catalyst in sequence, via pipeline 5 to carry out hydrocracking reaction to obtain hydrocracking products;

[0060] (2) The hydrocracking products are introduced into the high-pressure separator 8 via pipeline 7 for gas-liquid phase separation; the gas phase flowing out of the high-pressure separator 8 enters the gas purification unit 10 via pipeline 9, and the purified gas can be recycled back into the reaction system as circulating hydrogen via pipeline 11; the liquid phase flowing out of the high-pressure separator 8 enters the fractionation unit 13 via pipeline 12, and the propane-rich gas phase exits the device via pipeline 14; after fractionation by the fractionation unit, light naphtha containing C5 and above components is drawn out from pipeline 15. This part of light naphtha can also be mixed with the feed oil from the pipeline as unconverted oil according to production needs, and then recycled to the reaction system for full conversion.

[0061] The present invention will be described in detail below through examples. In the following examples, unless otherwise specified, the raw materials used are all commercially available products.

[0062] Unless otherwise specified, the following examples all use Figure 1 The process flow shown is followed.

[0063] The properties of the refinery light oil (aromatic raffinate) used are listed in Table 1; the catalysts used are listed in Table 2.

[0064] The catalysts provided in Table 2 were all prepared using methods known in the art, such as the preparation method provided in the literature with publication number CN112742440A.

[0065] Table 1: Refinery Light Oil

[0066]

[0067] Table 2: Catalyst Information

[0068]

[0069]

[0070] Example 1

[0071] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0072] The distribution and properties of the obtained products are listed in Table 4.

[0073] Example 2

[0074] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0075] The distribution and properties of the obtained products are listed in Table 4.

[0076] Example 3

[0077] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0078] The distribution and properties of the obtained products are listed in Table 4.

[0079] Example 4

[0080] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0081] The distribution and properties of the obtained products are listed in Table 4.

[0082] Example 5

[0083] use Figure 1The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0084] The distribution and properties of the obtained products are listed in Table 4.

[0085] Comparative Example 1

[0086] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0087] The distribution and properties of the obtained products are listed in Table 4.

[0088] Comparative Example 2

[0089] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0090] The distribution and properties of the obtained products are listed in Table 4.

[0091] Comparative Example 3

[0092] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0093] The distribution and properties of the obtained products are listed in Table 4.

[0094] Comparative Example 4

[0095] use Figure 1 The process flow shown is illustrated, and the relevant process parameters are listed in Table 3. The reaction products can be fractionated into gases and a small amount of light naphtha fraction.

[0096] The distribution and properties of the obtained products are listed in Table 4.

[0097] Table 3

[0098]

[0099] The percentage of catalyst loading volume in Table 3 is calculated based on the total catalyst loading volume of the hydrocracking reaction.

[0100] Table 3 (continued)

[0101]

[0102] The percentage of catalyst loading volume in Table 3 is calculated based on the total catalyst loading volume of the hydrocracking reaction.

[0103] Table 4

[0104]

[0105]

[0106] In Table 4, the selectivity of normal C4 = yield of normal C4 / (yield of normal C4 + yield of isomer C4). Table 4 (continued)

[0107] Comparative Example 1 Comparative Example 2 Comparative Example 3 Comparative Example 4 C1, mass% 0.12 0.17 0.11 0.14 C2, mass % 1.01 2.01 1.05 1.83 C3, mass % 19.24 19.35 3.84 16.43 Ortho-C4, mass % 8.48 4.9 3.34 4.33 Heterogeneous C4, mass % 10.24 5.58 5.69 5.02 Selectivity of ortho-C4, % 45.30 46.76 36.99 46.31 C3 content in gaseous products, wt%. 49.22 60.45 27.37 59.21 C5 and above hydrocarbons, by mass % 60.91 67.99 85.97 72.25

[0108] In Table 4, the selectivity of normal C4 is calculated as: yield of normal C4 / (yield of normal C4 + yield of isomer C4).

[0109] As shown in Tables 3 and 4, the scheme of the present invention can obtain a high yield of propane product, and the selectivity for n-butane is very high.

[0110] Furthermore, as can be seen from the results of Example 5 of the present invention, the refining temperature required for the non-preferred hydrorefining agent is slightly higher than that for the preferred hydrorefining catalyst (Example 2), but under the premise that the refining depth is similar and the hydrocracking catalyst remains unchanged, the product distribution obtained in the cracking section does not change much.

[0111] The preferred embodiments of the present invention have been described in detail above; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various technical features in any other suitable manner. These simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. A hydrocracking method for hydrocarbon conversion, characterized in that, The method includes: (1) Under low-pressure hydrogenation conditions, refinery light oil is introduced into a hydrocracking reaction zone packed with hydrocracking catalyst to carry out hydrocracking reaction, and hydrocracking products are obtained; the refinery light oil has a saturated hydrocarbon content of 90wt%~100wt%; the hydrocracking catalyst contains an active metal component and a support, the support contains an acidic component, the acidic component is a ZSM molecular sieve and / or a modified product of ZSM molecular sieve; the active metal component, calculated as oxides, is 10wt%~50wt% based on 100% of the weight of the hydrocracking catalyst; the acidic component, calculated as acidic components, is 45wt%~80wt% based on 100% of the weight of the support of the hydrocracking catalyst. The refinery light oil has a carbon number of C5 to C12, an alkane content of 35% to 55% by weight, a cycloalkanes content of 35% to 55% by weight, and an aromatics content of 0% to 10% by weight; the hydrocracking reaction pressure is ≤8.0 MPa; (2) The hydrocracking products are subjected to gas-liquid separation and fractionation in sequence to obtain light naphtha products and gaseous products containing propane and n-butane, wherein the propane content in the gaseous products is not less than 50 wt% and the n-butane selectivity is not less than 48%; The n-butane selectivity = (mass yield of n-butane in the gaseous product / sum of mass yields of C4 components in the gaseous product) * 100%; The conditions for the hydrocracking reaction are controlled such that the conversion rate in the hydrocracking reaction zone is 40% to 98%. The conversion rate = (1 - mass percentage of C5 and above hydrocarbons in the liquid product of the hydrocracking product * yield of the liquid product of the hydrocracking product / mass percentage of C5 and above hydrocarbons in the refinery light oil) * 100%; The yield of the liquid product from the hydrocracking product is calculated as follows: Liquid product yield = Mass of the liquid product obtained after gas-liquid separation of the hydrocracking product / Mass of the refinery light oil * 100%.

2. The hydrocracking method according to claim 1, characterized in that, The conditions of the hydrocracking reaction are controlled such that the conversion rate of the hydrocracking reaction zone is 60% to 80%.

3. The hydrocracking method according to claim 1, characterized in that, The refinery light oil is selected from at least one of reforming residue oil, straight-run naphtha, DCC gasoline hydrotreating unit residue oil, and hydrocracking naphtha.

4. The hydrocracking method according to claim 1, characterized in that, The nitrogen content in the refinery's light oil is ≤20 μg / g.

5. The hydrocracking method according to any one of claims 1-4, characterized in that, The hydrocracking reaction is carried out at a temperature of 280–420 °C, a pressure of 0.2–8.0 MPa, and a volume hourly space velocity of 0.1–20.0 h⁻¹. -1 The hydrogen-to-oil volume ratio is 100-2000.

6. The hydrocracking method according to any one of claims 1-4, characterized in that, A hydrogenation protection catalyst is packed upstream of the hydrocracking catalyst; based on the total catalyst volume in the hydrocracking reaction zone being 100%, the packing volume of the hydrogenation protection catalyst is 1% to 50%, and the packing volume of the hydrocracking catalyst is 80% to 99%.

7. The hydrocracking method according to any one of claims 1-4, characterized in that, In the hydrocracking catalyst, the support also contains a heat-resistant inorganic oxide, which is selected from at least one of silicon oxide and aluminum oxide.

8. The hydrocracking method according to any one of claims 1-4, characterized in that, In the hydrocracking catalyst, the active metal element in the active metal component is selected from at least two of Group VIB and Group VIII metal elements; based on the total weight of the hydrocracking catalyst, the content of Group VIB metal elements is 5wt% to 35wt% and the content of Group VIII metal elements is 1wt% to 8wt% in terms of oxides.

9. The hydrocracking method according to claim 6, characterized in that, The hydrogenation protection catalyst contains a hydrogenation protection catalyst support and a hydrogenation protection catalyst active metal component. The hydrogenation protection catalyst support is alumina, and the hydrogenation protection catalyst active metal component contains at least one element selected from Group VIII metals and at least one element selected from Group VIB metals.

10. The hydrocracking method according to claim 9, characterized in that, In the hydrogenation protection catalyst, based on the total weight of the hydrogenation protection catalyst, the content of the Group VIII metal element is 0.3wt% to 5wt% and the content of the Group VIB metal element is 1wt% to 30wt% in terms of oxides.

11. The hydrocracking method according to claim 10, characterized in that, In the hydrogenation protection catalyst, based on the total weight of the hydrogenation protection catalyst, the content of the Group VIB metal element, calculated as oxide, is 26wt% to 30wt%.

12. The hydrocracking method according to claim 9 or 10, characterized in that, In the hydrogenation protection catalyst, the active metal component of the hydrogenation protection catalyst contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

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