A precious metal-containing hydrocracking catalyst, its preparation method and application, and a method for hydrocracking treatment of residue oil.

Abstract

This invention relates to the field of hydrocracking catalysts, and discloses a hydrocracking catalyst, its preparation method and application, and a method for hydrocracking treatment of residue oil. The hydrocracking catalyst contains molecular sieves, silicon-modified alumina, and active metal components. Optionally, the hydrocracking catalyst also contains alumina and / or additives. Based on the total weight of the hydrocracking catalyst, the content of the molecular sieve is 5-25 wt%, the content of the silicon-modified alumina is 59-80 wt%, and the content of the alumina is 0-20 wt%. The content of the active metal component, calculated as oxides, is 0.1-1.5 wt%, and the content of the additives, calculated as oxides, is 0-1.0 wt%. The catalyst provided by this invention has the advantages of large specific surface area, large pore volume, large pore size, and high metal utilization. When used in the hydrocracking treatment of residue oil, this hydrocracking catalyst exhibits high activity and can improve naphtha selectivity.

Description

Technical Field

[0001] This invention relates to the field of hydrocracking catalysts, specifically to a hydrocracking catalyst, its preparation method and application, and a method for hydrocracking treatment of residue oil. Background Technology

[0002] As global oil becomes heavier and of lower quality, the demand structure for petroleum products is changing, with naphtha demand continuously increasing. Maximizing the production of light naphtha fractions from residue hydrocracking has become an important development direction for integrated refining and chemical technology. Noble metal catalysts (such as Pd and Pt-based catalysts) have attracted widespread attention in the field of hydrocracking due to their excellent hydrogen activation and hydrodehydrogenation performance.

[0003] However, existing single precious metal catalysts have significant drawbacks when processing complex residue oil systems: due to the high adsorption strength of the precious metal active center for hydrocarbon molecules and the lack of inhibition of other side reactions, the yield of C1-C4 gas is too high. Although the light naphtha fraction is improved to some extent, the product distribution is wide and the aromatic potential content in the heavy naphtha is severely lost, which cannot meet the feedstock needs of downstream reforming units.

[0004] More importantly, single precious metal catalysts exhibit poor resistance to impurities in residue hydrotreating reactions and are prone to reversible deactivation. This is because heavy components, colloids, asphaltenes, and other macromolecules in the residue strongly adsorb or polymerize on the active sites of the precious metal, resulting in the covering of active sites and making it difficult for the catalyst to meet the long-term operation requirements of industrial plants. Therefore, how to maintain the high activity of precious metals while precisely controlling the pore structure, surface acidity distribution, and interaction forces between the support and the precious metal, and improving the catalyst's resistance to deactivation, remains a pressing technical challenge in this field. Summary of the Invention

[0005] The purpose of this invention is to improve the utilization rate and selectivity of precious metal hydrogenation catalysts for naphtha while maintaining high intrinsic activity.

[0006] To achieve the above objectives, the first aspect of the present invention provides a noble metal hydrocracking catalyst, which contains a molecular sieve, silicon-modified alumina, and an active metal component, and optionally also contains alumina and / or an additive. Based on the total weight of the hydrocracking catalyst, the content of the molecular sieve is 5-25 wt%, the content of the silicon-modified alumina is 59-80 wt%, and the content of the alumina is 0-20 wt%; the content of the active metal component (calculated as oxide) is 0.1-1.5 wt%; and the content of the auxiliary agent (calculated as oxide) is 0-1.0 wt%. The active metal component is a noble metal component; the noble metal component is a combination of a first metal element and a second metal element; the first metal element is at least one of Pd and Pt, the second metal element is Ag; and the mass ratio of the content of the second metal element (calculated as oxide) to the content of the first metal element (calculated as oxide) is 2.35-2.6. The specific surface area of ​​the silicon-modified alumina is ≥490 m². 2 / g, pore volume ≥0.9 cm³ 3 / g, pore size ≥8nm, silicon dioxide content is 38-45wt%.

[0007] A second aspect of the present invention provides a method for preparing the hydrocracking catalyst described in the first aspect, the method comprising: (1) Molecular sieve, silicon-modified alumina, methylcellulose, guar gum powder, nitric acid, and optionally added alumina and / or auxiliary precursor solution are first mixed to obtain mixture I; (2) The mixture I is sequentially shaped, dried, and subjected to a first calcination to obtain a carrier; (3) The support is impregnated in an impregnation solution containing a precursor of noble metal components, and then subjected to a second calcination to obtain the hydrocracking catalyst; The conditions for the first and second calcinations each independently include: heating to 240-260℃ at a rate of 4-6℃ / min and holding for 50-70min; then heating to 390-410℃ at a rate of 2.2-2.6℃ / min and holding for 50-70min; and then heating to 540-560℃ at a rate of 1.5-1.7℃ / min and holding for 5-7h.

[0008] The third aspect of this invention provides the application of the hydrocracking catalyst described in the first aspect or the precious metal-containing hydrocracking catalyst prepared by the method described in the second aspect in the hydrocracking treatment of residue oil.

[0009] A fourth aspect of the present invention provides a method for hydrocracking of residual oil, the method comprising: In the presence of a catalyst and hydrogen, the residue oil is subjected to hydrocracking to obtain hydrocracking products. The catalyst is the hydrocracking catalyst described in the first aspect or the hydrocracking catalyst prepared by the method described in the second aspect of claim.

[0010] The catalyst provided by this invention has the advantages of large specific surface area, large pore volume, large pore size, and high metal utilization. When this hydrocracking catalyst is used for the hydrocracking of residue oil, it has high activity, which can improve the selectivity of naphtha, especially the selectivity of light naphtha, expand the adaptability of feedstock oil, and increase naphtha production. In addition, the catalyst has stable catalytic performance, which can significantly extend the service life of the catalyst and reduce the overall cost of use. Detailed Implementation

[0011] 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.

[0012] As mentioned above, the first aspect of the present invention provides a hydrocracking catalyst of noble metal, which contains molecular sieve, silicon-modified alumina, and active metal components, and optionally also contains alumina and / or additives. Based on the total weight of the hydrocracking catalyst, the content of the molecular sieve is 5-25 wt%, the content of the silicon-modified alumina is 59-80 wt%, and the content of the alumina is 0-20 wt%; the content of the active metal component (calculated as oxide) is 0.1-1.5 wt%; and the content of the auxiliary agent (calculated as oxide) is 0-1.0 wt%. The active metal component is a noble metal component; the noble metal component is a combination of a first metal element and a second metal element; the first metal element is at least one of Pd and Pt, the second metal element is Ag; and the mass ratio of the content of the second metal element (calculated as oxide) to the content of the first metal element (calculated as oxide) is 2.35-2.6. The specific surface area of ​​the silicon-modified alumina is ≥490 m². 2 / g, pore volume ≥0.9 cm³ 3 / g, pore size ≥8nm, silicon dioxide content is 38-45wt%.

[0013] The optional inclusion mentioned in this invention means that it may or may not be included.

[0014] In this invention, the molecular sieve, silicon-modified alumina, and alumina can be obtained by purchasing commercially available materials or by preparing them using methods known in the art.

[0015] In this invention, the silicon-modified alumina can provide more acidic sites and a larger specific surface area and pore volume. Using specific silicon-modified alumina can help improve the activity and stability of the catalyst and the selectivity of naphtha.

[0016] Preferably, the content of the active metal component, calculated as oxide, is 0.5-1.0 wt% based on the total weight of the hydrocracking catalyst. The inventors have found that, under this preferred condition, the hydrocracking catalyst exhibits higher hydrocracking catalytic activity and higher selectivity.

[0017] Preferably, the specific surface area of ​​the hydrocracking catalyst is 200-450 m². 2 / g, pore volume 0.3-0.7cm 3 / g, with a pore size of 5-7nm.

[0018] Preferably, the alumina has a pore size ≥ 10 nm and a pore volume ≥ 1.2 cm³. 3 / g, specific surface area ≥450 m² 2 / g. Under these preferred conditions, alumina can provide a large specific surface area and pore volume for the catalyst, further promoting the dispersion of active metals on alumina and improving the activity and stability of the catalyst.

[0019] Preferably, the molecular sieve is selected from at least one of ultrastable Y-type molecular sieve, ZSM-5 molecular sieve, SAPO molecular sieve and MCM-41 mesoporous molecular sieve.

[0020] Preferably, the ultrastable Y-type molecular sieve has a silicon-to-aluminum molar ratio ≥30 and a specific surface area ≥700 m². 2 / g.

[0021] More preferably, the silicon-to-aluminum molar ratio in the ultrastable Y-type molecular sieve is 35-45, and the specific surface area is 700-800 m². 2 / g. The inventors discovered that, under this preferred condition, the activity and selectivity of the catalyst can be further improved.

[0022] In this invention, the silicon-aluminum molar ratio refers to the molar ratio of silicon oxide to aluminum oxide.

[0023] In preferred embodiments, the ZSM-5 molecular sieve has a silica-alumina molar ratio ≥260 and a specific surface area ≥300 m². 2 / g.

[0024] In a preferred embodiment, the additive is selected from at least one of phosphorus, boron, and titanium.

[0025] Preferably, the sodium oxide content in the molecular sieve, the silicon-modified alumina, and the alumina is ≤0.1wt%.

[0026] As previously described, a second aspect of the present invention provides a method for preparing the hydrocracking catalyst described in the first aspect, the method comprising: (1) Molecular sieve, silicon-modified alumina, methylcellulose, guar gum powder, nitric acid, and optionally added alumina and / or auxiliary precursor solution are first mixed to obtain mixture I; (2) The mixture I is sequentially shaped, dried, and subjected to a first calcination to obtain a carrier; (3) The support is impregnated in an impregnation solution containing a precursor of noble metal components, and then subjected to a second calcination to obtain the hydrocracking catalyst; The conditions for the first and second calcinations each independently include: heating to 240-260℃ at a rate of 4-6℃ / min and holding for 50-70min; then heating to 390-410℃ at a rate of 2.2-2.6℃ / min and holding for 50-70min; and then heating to 540-560℃ at a rate of 1.5-1.7℃ / min and holding for 5-7h.

[0027] The inventors of this invention discovered during the preparation of the hydrocracking catalyst that controlling the conditions of the first calcination can further yield a support with a larger specific surface area, pore volume, and pore size. After the support is impregnated with the active metal component, the control of the calcination conditions has a certain impact on the performance of the obtained hydrocracking catalyst. Based on this, the second calcination is carried out in stages under specified temperature and time conditions, which can maintain the performance of the support and improve the catalytic performance of the catalyst during the calcination process.

[0028] In a preferred embodiment, the amounts of the molecular sieve, silicon-modified alumina, active metal component, and optionally added alumina and additives are controlled such that, based on the total weight of the hydrocracking catalyst, the content of the molecular sieve is 5-25 wt%, the content of the silicon-modified alumina is 59-80 wt%, the content of the alumina is 0-20 wt%, the content of the active metal component (calculated as oxide) is 0.1-1.5 wt%, and the content of the additives (calculated as oxide) is 0-1.0 wt%.

[0029] More preferably, the amount of the active metal component is controlled such that the content of the active metal component, calculated as oxide, is 0.5-1.0 wt% based on the total weight of the hydrocracking catalyst.

[0030] In this invention, the molecular sieve, silicon-modified alumina, and alumina in step (1) are the same as those in the first aspect, which has already been described and will not be repeated here.

[0031] Preferably, the precursor solution of the auxiliary agent is selected from at least one of phosphoric acid, boric acid, and titanium oxalate.

[0032] The present invention does not have any particular requirements for the first mixing method, as long as the molecular sieve, silicon-modified alumina, methylcellulose, guar gum powder, nitric acid, and optionally added alumina and auxiliary precursor solution can be mixed evenly. Those skilled in the art should not understand this as a limitation of the present invention.

[0033] Preferably, based on a total weight of 100g for the molecular sieve, silicon-modified alumina, and alumina, the amount of methylcellulose used is 0.4-0.6g, the amount of guar gum powder used is 0.4-0.6g, and the amount of nitric acid used is 80-90mL.

[0034] Preferably, the concentration of the nitric acid is 3-5 wt%.

[0035] The present invention does not specifically limit the molding method described in step (2). Molding methods conventionally defined in the art are applicable to the present invention, such as pressing, rolling, extrusion, etc.

[0036] In a preferred embodiment, in step (2), the drying conditions include a temperature of 80-120°C and a time of 3-8 hours. More preferably, the drying operation includes drying the shaped product at 80°C for 3-4 hours, and then drying it at 120°C for 3-4 hours.

[0037] Preferably, the carrier is shaped like a sphere, a cylindrical strip, a clover, or a toothed ball.

[0038] In this invention, the active component is introduced in step (3) through an impregnation solution containing an active metal component precursor. Any impregnation solution containing an active component precursor conventionally defined in the art is applicable to this invention. Preferably, in step (3), the impregnation solution containing the active metal component precursor is composed of an impregnation solution containing a noble metal component precursor.

[0039] Preferably, in step (3), the impregnation solution containing the noble metal component precursor is an aqueous solution containing a first metal element precursor and a second metal element precursor.

[0040] In a preferred embodiment, in the impregnation solution containing the noble metal component precursor, the concentration of the first metal element precursor is 0.004-0.006 g / mL, and the concentration of the second metal element precursor is 0.009-0.01 g / mL.

[0041] In a preferred embodiment, the contents of the first metal element precursor and the second metal element precursor in the impregnation solution containing the noble metal component precursor are controlled such that the mass ratio of the content of the second metal element (calculated as oxide) to the content of the first metal element (calculated as oxide) is 2.35-2.6.

[0042] Preferably, the first metal element precursor is at least one of palladium precursor and platinum precursor, and the second metal element precursor is silver precursor.

[0043] Preferably, the palladium precursor, platinum precursor, and silver precursor are soluble salts of the corresponding metal active components. More preferably, the palladium precursor is palladium nitrate, the silver precursor is silver nitrate, and the platinum precursor is platinum nitrate.

[0044] Preferably, the impregnation is performed using equal-volume impregnation.

[0045] Preferably, in step (3), the conditions for impregnation include: a temperature of 20-30°C and a time of 1-2 hours.

[0046] In a preferred embodiment, the method further includes: after impregnation, drying the impregnated product, then drying it at 80°C for 3-4 hours, drying it at 120°C for 3-4 hours, and then performing the second calcination.

[0047] The present invention does not have any special requirements for the drying method and conditions, and those skilled in the art can use the technical means known in the art.

[0048] The method provided by this invention involves first molding and then impregnating an acidic component material, and specifically controlling the reaction conditions of the first and second calcinations to produce a catalyst containing precious metals such as Pd, Pt, and Ag, which has a larger pore volume, pore size, and specific surface area, making it suitable for single-stage hydrotreating of heavier and lower-quality residue oil fractions.

[0049] As previously stated, the third aspect of this invention provides the application of the hydrocracking catalyst described in the first aspect or the precious metal-containing hydrocracking catalyst prepared by the method described in the second aspect in the hydrocracking treatment of residue oil.

[0050] As described above, a fourth aspect of the present invention provides a method for hydrocracking of residue oil, the method comprising: In the presence of a catalyst and hydrogen, the residue oil is subjected to hydrocracking to obtain hydrocracking products. The catalyst is the hydrocracking catalyst described in the first aspect or the hydrocracking catalyst prepared by the method described in the second aspect of claim.

[0051] Preferably, the conditions for the hydrocracking treatment include: a reaction pressure of 8.0-12.0 MPa, a reaction temperature of 350-400 °C, and a volume hourly space velocity of 1.5-2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is 700:1-900:1.

[0052] The present invention will be described in detail below through examples. Unless otherwise specified, all reagents used in the present invention are analytical grade reagents. In the following examples, unless a specific reaction temperature is specified, the reaction is carried out at room temperature (24±1℃).

[0053] Ultra-stable Y-type molecular sieve: silica-alumina molar ratio of 40, specific surface area of ​​712.8 m². 2 / g, purchased from Auscatalytic Materials (Dalian) Co., Ltd.

[0054] Silicon-modified alumina: specific surface area 495.8 m² 2 / g, pore volume 1.02 cm³ 3 / g, pore size 8.234nm, silica content 40wt%; model SIRAL 40 (product number 545100), purchased from SASOL.

[0055] Alumina: pore size 10.577 nm, pore volume 1.21 cm³ 3 / g, with a specific surface area of ​​456.02 m². 2 / g, type: special pseudoboehmite, purchased from Hejin Juhua Aluminum Co., Ltd.

[0056] ZSM-5 molecular sieve: silica-alumina molar ratio of 260, specific surface area of ​​300 m² / g. 2 / g, model / grade NZ-HZ5-005, purchased from Zhuoyue Chemical New Materials (Shanghai) Co., Ltd.

[0057] SAPO-34 molecular sieve: silica-alumina molar ratio of 0.6, specific surface area of ​​620 m². 2 / g, model / grade NZ-HSP34-002, purchased from Zhuoyue Chemical New Materials (Shanghai) Co., Ltd.

[0058] The specific surface area, pore volume, and pore size of the molecular sieve, silicon-modified alumina, alumina, and the prepared catalyst were measured using a fully automated adsorption instrument according to the low-temperature nitrogen adsorption-desorption method.

[0059] Nitric acid: A nitric acid aqueous solution with a mass concentration of 5 wt%.

[0060] Example 1 (1) Mix 40g of ultrastable Y molecular sieve, 160g of silicon-modified alumina, 1g of guar gum powder and 1g of carboxymethyl cellulose evenly, add 180mL of 5wt% nitric acid for the first mixing, and obtain mixture I; (2) The mixture I was extruded into strips using a 1.2mm clover perforated plate, dried, and then dried at 80°C for 3 hours, and then dried at 120°C for 3 hours. The mixture was then calcined in a muffle furnace to obtain the carrier. The conditions for the first calcination were as follows: the temperature was increased to 250℃ at a rate of 5℃ / min and held for 60 min; then the temperature was increased to 400℃ at a rate of 2.5℃ / min and held for 60 min; then the temperature was increased to 550℃ at a rate of 1.6℃ / min and held for 6 h. (3) Dissolve 0.3 g of palladium nitrate dihydrate and 0.45 g of silver nitrate in 50 g of water to obtain an impregnation solution containing a precursor of noble metal components; Take 60 g of the support and impregnate it with an impregnation solution containing a precursor of noble metal components at room temperature for 1.5 h. After impregnation, air dry it. First, dry it at 80 °C for 3 h, and then dry it at 120 °C for 4 h. Then, perform a second calcination in a muffle furnace and cool it to room temperature to obtain catalyst C1. The conditions for the second calcination were as follows: the temperature was increased to 250℃ at a rate of 5℃ / min and held for 60 min; then the temperature was increased to 400℃ at a rate of 2.5℃ / min and held for 60 min; and then the temperature was increased to 550℃ at a rate of 1.6℃ / min and held for 6 h.

[0061] Examples 2 to 5 and Comparative Examples 1 to 4 were all carried out using methods similar to those in Example 1, except that the types and amounts of each raw material were different. The specific differences are shown in Table 1. Any parts not listed are the same as those in Example 1.

[0062] Table 1

[0063] Continued from Table 1

[0064] Example 6 The method is similar to that in Example 1, except that the conditions for the second calcination in step (3) are different. The conditions for the second calcination in this example include: heating from room temperature to 250°C and holding for 60 minutes; then heating to 550°C and holding for 6 hours. The remaining steps were the same as in Example 1, and catalyst C6 was obtained.

[0065] Test case The catalysts (C1 to C6, DC1 to DC4) prepared in the above examples were evaluated for solvent deasphalting hydrocracking reaction in a 30 mL reactor. The hydrocracking conditions were: reaction pressure 10 MPa, reaction temperature 385 °C, and volume hourly space velocity 2 h⁻¹. -1 The hydrogen-to-oil volume ratio was 800:1, and the catalyst loading was 10g. Before evaluation, the catalyst was activated under the following conditions: in a mixed atmosphere of nitrogen and hydrogen with a volume ratio of 1:1, the temperature was raised to 250℃ and the pressure was 3.0MPa for 8 hours for reduction.

[0066] The properties of solvent-deasphalted oil (feedstock oil) are shown in Table 2, the composition and properties of the catalyst are shown in Table 3, and the composition of the products after hydrocracking and the evaluation results of the catalyst are shown in Table 4.

[0067] The single-pass conversion rate (%) is calculated as follows: (feed mass of raw materials - mass of unreacted raw materials) / feed mass of raw materials × 100%.

[0068] Table 2 Properties of Crude Oil

[0069] Table 3

[0070] Continued from Table 3

[0071] Table 4

[0072] As can be seen from the results in Table 1, the catalyst provided by this invention for the hydrocracking of solvent-deasphalted oil has the characteristics of high conversion rate and good naphtha selectivity, and the yield of light naphtha is above 9.8 wt%.

[0073] 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 catalyst containing a noble metal, characterized in that, The hydrocracking catalyst contains molecular sieves, silicon-modified alumina, and active metal components, and optionally also contains alumina and / or additives. Based on the total weight of the hydrocracking catalyst, the content of the molecular sieve is 5-25 wt%, the content of the silicon-modified alumina is 59-80 wt%, and the content of the alumina is 0-20 wt%; the content of the active metal component (calculated as oxide) is 0.1-1.5 wt%; and the content of the auxiliary agent (calculated as oxide) is 0-1.0 wt%. The active metal component is a noble metal component; the noble metal component is a combination of a first metal element and a second metal element; the first metal element is at least one of Pd and Pt, the second metal element is Ag; and the mass ratio of the content of the second metal element (calculated as oxide) to the content of the first metal element (calculated as oxide) is 2.35-2.

6. The specific surface area of ​​the silicon-modified alumina is ≥490 m². 2 / g, pore volume ≥0.9 cm³ 3 / g, pore size ≥8nm, silicon dioxide content is 38-45wt%.

2. The hydrocracking catalyst according to claim 1, characterized in that, Based on the total weight of the hydrocracking catalyst, the content of the active metal component, calculated as oxide, is 0.5-1.0 wt%. And / or, the specific surface area of ​​the hydrocracking catalyst is 200-450 m². 2 / g, pore volume 0.3-0.7cm 3 / g, with a pore size of 5-7nm.

3. The hydrocracking catalyst according to claim 1, characterized in that, The alumina has a pore size ≥ 10 nm and a pore volume ≥ 1.2 cm³. 3 / g, specific surface area ≥450 m² 2 / g.

4. The hydrocracking catalyst according to any one of claims 1-3, characterized in that, The molecular sieve is selected from at least one of ultrastable Y-type molecular sieve, ZSM-5 molecular sieve, SAPO molecular sieve and MCM-41 mesoporous molecular sieve.

5. The hydrocracking catalyst according to claim 4, characterized in that, The ultrastable Y-type molecular sieve has a silicon-to-aluminum molar ratio ≥30 and a specific surface area ≥700 m². 2 / g; And / or, the ZSM-5 molecular sieve has a silica-alumina molar ratio ≥260 and a specific surface area ≥300 m². 2 / g.

6. The hydrocracking catalyst according to any one of claims 1-3, characterized in that, The additive is selected from at least one of phosphorus, boron, and titanium; And / or, in the molecular sieve, the silicon-modified alumina and the alumina, the sodium oxide content is ≤0.1wt%.

7. A method for preparing the hydrocracking catalyst according to any one of claims 1-6, characterized in that, The method includes: (1) Molecular sieve, silicon-modified alumina, methylcellulose, guar gum powder, nitric acid, and optionally added alumina and / or auxiliary precursor solution are first mixed to obtain mixture I; (2) The mixture I is sequentially shaped, dried, and subjected to a first calcination to obtain a carrier; (3) The support is impregnated in an impregnation solution containing a precursor of noble metal components, and then subjected to a second calcination to obtain the hydrocracking catalyst; The conditions for the first and second calcinations each independently include: heating to 240-260℃ at a rate of 4-6℃ / min and holding for 50-70min; then heating to 390-410℃ at a rate of 2.2-2.6℃ / min and holding for 50-70min; and then heating to 540-560℃ at a rate of 1.5-1.7℃ / min and holding for 5-7h.

8. The method according to claim 7, characterized in that, In step (2), the drying conditions include: a temperature of 80-120°C and a time of 3-8 hours; Preferably, in step (3), the conditions for impregnation include: a temperature of 20-30°C and a time of 1-2 hours.

9. The application of the hydrocracking catalyst according to any one of claims 1-6 or the precious metal-containing hydrocracking catalyst prepared by the method according to any one of claims 7-8 in the hydrocracking treatment of residue oil.

10. A method for hydrocracking residue oil, characterized in that, The method includes: In the presence of a catalyst and hydrogen, the residue oil is subjected to hydrocracking to obtain hydrocracking products. The catalyst is the hydrocracking catalyst according to any one of claims 1-6 or the hydrocracking catalyst prepared by the method according to any one of claims 7-8; Preferably, the conditions for the hydrocracking treatment include: a reaction pressure of 8.0-12.0 MPa, a reaction temperature of 350-400 °C, and a volume hourly space velocity of 1.5-2.5 h⁻¹. -1 The hydrogen-to-oil volume ratio is 700:1-900:1.

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