Hydrocracking method for hydrocarbon conversion

Abstract

The invention relates to the technical field of refinery light oil hydro-conversion, 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 to carry out a hydrocracking reaction under a low-pressure hydrogen condition to obtain a hydrocracking product; and sequentially carrying out gas-liquid separation and fractionation on the hydrocracking product to obtain a light naphtha product and a gas product rich in propane. According to the method disclosed by the invention, the saturated hydrocarbon is converted into the small molecular hydrocarbon under the low-pressure hydrocracking condition, particularly the propane yield and the n-butane selectivity are maximized, and high-quality raw materials can be provided for chemical engineering devices.

Description

Technical Field

[0001] The invention relates to the technical field of refinery light oil hydroconversion, and in particular to a hydrocracking method for hydrocarbon conversion. Background Art

[0002] In recent years, the energy consumption structure has shifted toward clean and environmentally friendly energy such as natural gas and electricity. The demand for fuel oil represented by gasoline has gradually peaked. Refinery light oil represented by light naphtha and aromatic raffinate oil is in urgent need of a high-value utilization method.

[0003] At the same time, the market demand for chemical products has increased year by year, driving the increase in the production scale of chemical materials represented by ethylene and propylene. The best raw materials for chemical plants such as ethylene plants are low-carbon normal alkanes. Therefore, using low-sulfur and low-nitrogen naphtha fractions as raw materials to produce propane and produce a portion of low-carbon normal hydrocarbons as by-products can provide high-quality raw materials for chemical plants and solve the problem of excess low-value-added naphtha fraction resources in refineries.

[0004] Existing hydrocracking units mainly use wax oil or diesel, which needs to be refined before cracking, and the unit pressure is often 10.0-15.0MPa. In addition, the mass fraction of isomerized hydrocarbons in light naphtha produced by conventional hydrocracking units is about 40%-60%, and the mass fraction of normal hydrocarbons is only 10%-20%, which cannot be used as high-quality chemical materials.

[0005] CN106062148A discloses a process for converting hydrocarbons into olefins, wherein a hydrocarbon raw material represented by naphtha is separated into multiple streams classified by carbon number through a hydrocracking unit, and the appropriate streams are fed to subsequent steam cracking, propane dehydrogenation and butane dehydrogenation units to produce olefins. The conditions of the hydrocracking unit in the method include a temperature of 470-550°C, a pressure of 0.6-3.0 MPa gauge pressure and a temperature of 0.2-10 h -1 Mass airspeed.

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

[0007] WO2019162392A1 discloses a method for converting the paraffins and cycloalkanes of naphtha raw materials into propane by hydrocracking. The naphtha raw materials without olefins are mixed with hydrogen and heated at a temperature of 200 to 600°C, a pressure of 1 to 10 MPa, and a feed mass space velocity of 0.1 to 10.0 h / min. -1 The hydrocracking reaction is carried out on a bifunctional catalyst under the condition of a hydrogen-to-oil molar ratio of 1 to 1000, and 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 by hydrogenation of light hydrocarbons, wherein the light hydrocarbon raw material, hydrogen-rich gas and circulating light hydrocarbon are heated, and then catalytic cracking reaction is carried out under acidic catalyst conditions, and the reaction product is cooled and fractionated to obtain dry gas, propane and aromatic gasoline components. The raw material of the method is a raw material with an alkane content greater than 50wt% and a carbon number range of C4 to C13, the reaction temperature is 250 to 550°C, the pressure is 0.01 to 5.0MPa, and the mass space velocity is 0.1 to 5.0h -1 , the hydrogen-to-oil ratio is 30 to 800:1, and the catalyst is a HZSM-5 molecular sieve.

[0009] However, the above-mentioned prior arts all have defects such as harsh reaction conditions and limited adaptability of raw materials. Summary of the invention

[0010] The purpose of the present invention is to provide a method for converting low-carbon hydrocarbons to produce propane and normal butane in order to solve the problem of excess light alkanes in refineries.

[0011] In order to achieve the above object, the present invention provides a hydrocracking method for hydrocarbon conversion, which comprises:

[0012] (1) Under low-pressure hydrogen conditions, introducing refinery light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst for hydrocracking reaction to obtain a hydrocracking product; the refinery light oil has a saturated hydrocarbon content of 90 wt% to 100 wt%; the hydrocracking catalyst contains an active metal component and a carrier, the carrier contains an acidic component, and the acidic component is a ZSM molecular sieve and / or a modified product of a ZSM molecular sieve; based on the weight of the hydrocracking catalyst as 100%, the content of the active metal component in terms of oxide is 10 wt% to 50 wt%; based on the weight of the carrier of the hydrocracking catalyst as 100%, the content of the acidic component is 45 wt% to 80 wt%;

[0013] (2) subjecting the hydrocracking product to gas-liquid separation and fractionation in sequence to obtain a light naphtha product and a gas product containing propane and normal butane, wherein the propane content in the gas product is not less than 50 wt % and the normal butane selectivity is not less than 48%;

[0014] The n-butane selectivity = the mass yield of n-butane in the gas product / the sum of the mass yield of C4 components in the gas product*100%;

[0015] wherein the conditions of the hydrocracking reaction are controlled so that the conversion rate of the hydrocracking reaction zone is 40% to 98%;

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

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

[0018] The method of the present invention realizes the conversion of saturated hydrocarbons into small molecule hydrocarbons under low-pressure hydrocracking conditions of low-nitrogen naphtha raw materials, especially maximizes the yield of propane and the selectivity of n-butane, and can provide high-quality raw materials for chemical plants. BRIEF DESCRIPTION OF THE DRAWINGS

[0019] Figure 1 It is a schematic flow diagram of a hydrocracking method for hydrocarbon conversion described in the present invention.

[0020] Description of Reference Numerals

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

[0022] 2: Raw 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 DESCRIPTION

[0028] The endpoints and any values ​​of the ranges disclosed in this article 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 each range, the endpoint values ​​of each range and the individual point values, and the individual point values ​​can be combined with each other to obtain one or more new numerical ranges, which should be considered as specifically disclosed in this article.

[0029] As mentioned above, the present invention provides a hydrocracking method for hydrocarbon conversion, which comprises:

[0030] (1) Under low-pressure hydrogen conditions, introducing refinery light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst for hydrocracking reaction to obtain a hydrocracking product; the refinery light oil has a saturated hydrocarbon content of 90 wt% to 100 wt%; the hydrocracking catalyst contains an active metal component and a carrier, the carrier contains an acidic component, and the acidic component is a ZSM molecular sieve and / or a modified product of a ZSM molecular sieve; based on the weight of the hydrocracking catalyst as 100%, the content of the active metal component in terms of oxide is 10 wt% to 50 wt%; based on the weight of the carrier of the hydrocracking catalyst as 100%, the content of the acidic component is 45 wt% to 80 wt%;

[0031] (2) subjecting the hydrocracking product to gas-liquid separation and fractionation in sequence to obtain a light naphtha product and a gas product containing propane and normal butane, wherein the propane content in the gas product is not less than 50 wt % and the normal butane selectivity is not less than 48%;

[0032] The n-butane selectivity = the mass yield of n-butane in the gas product / the sum of the mass yield of C4 components in the gas product*100%;

[0033] wherein the conditions of the hydrocracking reaction are controlled so that the conversion rate of the hydrocracking reaction zone is 40% to 98%;

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

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

[0036] The calculation method of the yield of the liquid product of the hydrocracking product of the present invention is: the yield of the liquid product = the mass of the liquid product obtained after gas-liquid separation of the hydrocracking product / the mass of the refinery light oil * 100%.

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

[0038] The calculation method of the sum of the mass yields of the C4 components in the gas product of the present invention is: the sum of the mass of the C4 components in the gas product / the mass of the refinery light oil*100%.

[0039] The method of the present invention may also include, before introducing the refinery light oil into the hydrocracking reaction zone for the hydrocracking reaction, preheating the refinery light oil alone or together with hydrogen, for example, introducing it into a heating furnace for preheating treatment; and then introducing the preheated material into the hydrocracking reaction zone for the hydrocracking reaction. The present invention has no special requirements for the preheating temperature, which can be the temperature required for the hydrocracking reaction or slightly lower than the temperature required for the hydrocracking reaction.

[0040] Preferably, the carbon number of the refinery light oil is C5 to C12, the paraffin content is 30% to 100% by weight, the cycloparaffin content is 0% to 70% by weight, and the aromatic content is 0% to 10% by weight.

[0041] More preferably, the paraffin content of the refinery light oil is 30 wt% to 60 wt%; further preferably, it is 35 wt% to 55 wt%.

[0042] More preferably, the cycloparaffin content of the refinery light oil is 2 wt% to 60 wt%; further preferably, it is 35 wt% to 55 wt%.

[0043] More preferably, the aromatics content of the refinery light oil is 0.1 wt% to 8 wt%; further preferably, it is 0.5 wt% to 7 wt%.

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

[0045] Preferably, the refinery light oil is selected from at least one of reforming raffinate, straight-run naphtha, DCC gasoline hydrogenation unit raffinate, and hydrocracking naphtha.

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

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

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

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

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

[0051] In a particularly preferred case, in the hydrocracking catalyst, the active metal elements in the active metal component are selected from at least two of Group VIB metal elements 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 oxide.

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

[0053] Preferably, the hydrogenation protection catalyst contains a protectant carrier and a protectant active metal component, the protectant carrier is alumina, and the protectant active metal component contains at least one element selected from Group VIII metal elements and at least one element selected from Group VIB metal elements.

[0054] Particularly preferably, in the hydrogenation protection catalyst, based on the total weight of the hydrogenation protection agent, the content of the metal element of Group VIII is 0.3wt% to 5wt% in terms of oxide, and the content of the metal element of Group VIB is 1wt% to 30wt%. Further preferably, in the hydrogenation protection catalyst, based on the total weight of the hydrogenation protection agent, the content of the metal element of Group VIB is 26wt% to 30wt% in terms of oxide.

[0055] Preferably, in the hydrogenation protection catalyst, the protective agent active metal component 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 carried out in a separator (e.g., a high-pressure separator) for example. The gas product obtained after the gas-liquid separation can be recycled back to the device for the hydrocracking reaction after purification. The liquid product obtained after the gas-liquid separation is preferably further fractionated to obtain the light naphtha product and the gas product having a propane content of not less than 40wt%.

[0057] The light naphtha product obtained in the present invention can be mixed with the raw oil as unconverted oil according to production needs, and then circulated to the reaction system for full conversion, or it can be led out of the device. The present invention has no special requirements for this.

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

[0059] (1) Under low-pressure hydrogen conditions, refinery light oil is introduced into a heating furnace 4 through pipeline 1, feed oil pump 2 and pipeline 3 in sequence for preheating, and hydrogen is introduced into the heating furnace 4 through pipeline 16 to obtain preheated materials; the preheated materials are introduced into a hydrocracking reaction zone 6 filled with a hydroprotection catalyst and a hydrocracking catalyst in sequence through pipeline 5 for hydrocracking reaction to obtain hydrocracking products;

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

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

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

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

[0064] The catalysts provided in Table 2 are all prepared by methods known in the art, for example, they can be prepared by the preparation method provided in the document with publication number CN112742440A.

[0065] Table 1: Refinery Light Oil

[0066]

[0067] Table 2: Catalyst conditions

[0068]

[0069]

[0070] Example 1

[0071] use Figure 1 The process flow shown in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

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

[0082] Example 5

[0083] use Figure 1The process flow shown in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

[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 in the figure is carried out, and the process parameters and other information involved are listed in Table 3. The reaction product can be divided into gas and a small amount of light naphtha fraction by fractionation.

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

[0097] Table 3

[0098]

[0099] The catalyst loading volume percentages in Table 3 are calculated based on the total catalyst loading volume for the hydrocracking reaction.

[0100] Table 3 (Continued)

[0101]

[0102] The catalyst loading volume percentages in Table 3 are calculated based on the total catalyst loading volume for the hydrocracking reaction.

[0103] Table 4

[0104]

[0105]

[0106] Selectivity of normal C4 in Table 4 = yield of normal C4 / (yield of normal C4+yield of isomeric 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 Normal C4, mass% 8.48 4.9 3.34 4.33 Isomerized C4, mass% 10.24 5.58 5.69 5.02 Selectivity of normal C4, % 45.30 46.76 36.99 46.31 C3 content in gas products, wt% 49.22 60.45 27.37 59.21 C5 and above hydrocarbons, mass % 60.91 67.99 85.97 72.25

[0108] Selectivity of normal C4 in Table 4 = yield of normal C4 / (yield of normal C4+yield of isomeric C4)

[0109] It can be seen from Table 3 and Table 4 that the scheme of the present invention can obtain a propane product with a higher yield, and the selectivity of n-butane is very high.

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

[0111] The preferred embodiments of the present invention are described in detail above, but the present invention is not limited thereto. Within the technical concept of the present invention, the technical solution of the present invention can be subjected to a variety of simple modifications, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be regarded as the contents disclosed by the present invention and belong to 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 hydrogen conditions, introducing refinery light oil into a hydrocracking reaction zone filled with a hydrocracking catalyst for hydrocracking reaction to obtain a hydrocracking product; the refinery light oil has a saturated hydrocarbon content of 90 wt% to 100 wt%; the hydrocracking catalyst contains an active metal component and a carrier, the carrier contains an acidic component, and the acidic component is a ZSM molecular sieve and / or a modified product of a ZSM molecular sieve; based on the weight of the hydrocracking catalyst as 100%, the content of the active metal component in terms of oxide is 10 wt% to 50 wt%; based on the weight of the carrier of the hydrocracking catalyst as 100%, the content of the acidic component is 45 wt% to 80 wt%; (2) subjecting the hydrocracking product to gas-liquid separation and fractionation in sequence to obtain a light naphtha product and a gas product containing propane and normal butane, wherein the propane content in the gas product is not less than 50 wt % and the normal butane selectivity is not less than 48%; The n-butane selectivity = the mass yield of n-butane in the gas product / the sum of the mass yield of C4 components in the gas product*100%; wherein the conditions of the hydrocracking reaction are controlled so that the conversion rate of the hydrocracking reaction zone is 40% to 98%; The conversion rate = (1-the mass percentage of C5 and above hydrocarbons in the liquid product of the hydrocracking product*the yield of the liquid product of the hydrocracking product / the mass percentage of C5 and above hydrocarbons in the refinery light oil)*100%.

2. The hydrocracking method according to claim 1, characterized in that: The conditions of the hydrocracking reaction are controlled so 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 carbon number of the refinery light oil is C5 to C12, the paraffin content is 30% to 100% by weight, the cycloparaffin content is 0% to 70% by weight, and the aromatic content is 0% to 10% by weight; Preferably, the refinery light oil is selected from at least one of reforming raffinate, straight-run naphtha, DCC gasoline hydrogenation unit raffinate, and hydrocracking naphtha.

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

5. The hydrocracking method according to any one of claims 1 to 4, characterized in that: The pressure of the hydrocracking reaction is ≯8.0 MPa.

6. The hydrocracking method according to any one of claims 1 to 4, characterized in that: The temperature of the hydrocracking reaction is 280-420°C, the pressure is 0.2-8.0 MPa, and the volume space velocity is 0.1-20.0 h -1 , the volume ratio of hydrogen to oil is 100~2000.

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

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

9. The hydrocracking method according to any one of claims 1 to 8, characterized in that: In the hydrocracking catalyst, the active metal elements in the active metal component are selected from at least two of Group VIB metal elements 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 oxide.

10. The hydrocracking method according to claim 7, characterized in that: The hydrogenation protection catalyst contains a protection agent carrier and a protection agent active metal component. The protection agent carrier is alumina. The protection agent active metal component contains at least one element selected from Group VIII metal elements and at least one element selected from Group VIB metal elements.

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 agent, the content of the metal element of Group VIII is 0.3wt% to 5wt%, and the content of the metal element of Group VIB is 1wt% to 30wt% in terms of oxide; Preferably, in the hydrogenation protection catalyst, the content of the VIB group metal element is 26 wt% to 30 wt% in terms of oxide, based on the total weight of the hydrogenation protection agent.

12. The hydrocracking method according to claim 10 or 11, characterized in that: In the hydrogenation protection catalyst, the protective agent active metal component contains at least one of nickel and cobalt, and at least one of molybdenum and tungsten.

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