Wax oil hydrocracking catalyst and preparation and application thereof

Abstract

The invention discloses a wax oil hydrocracking catalyst and preparation and application thereof, and the wax oil hydrocracking catalyst mainly comprises the following components by weight: 1-30 parts of a mesoporous-microporous SBA-15 / HY composite molecular sieve; 15 to 40 parts of amorphous silica-alumina; 5 to 30 parts of mesoporous alumina; 10-30 parts of an oxide of a metal W or Mo; 1-8 parts of oxide of metal Co or Ni; 1.0 to 5.0 parts of an extrusion aid; 3-8 parts of an adhesive; the mesoporous-microporous SBA-15 / HY composite molecular sieve is prepared under the action of ultrasonic emulsification. The wax oil hydrocracking catalyst provided by the invention can stably operate for a long period when being used for processing an inferior wax oil raw material.

Description

Technical Field

[0001] The invention relates to a wax oil hydrocracking catalyst and its preparation and application. Background Art

[0002] Hydrocracking technology is one of the important means of deep processing of heavy oil. It has many advantages such as strong raw material adaptability, flexible processing scheme, high yield of liquid products, and good product quality. In particular, heavy naphtha has a high potential content of aromatics, and is a high-quality raw material for catalytic reforming to produce aromatics or high-octane gasoline. Hydrogenated tail oil and light naphtha are rich in paraffins and are high-quality feeds for steam cracking ethylene units. At the same time, they can also produce high-quality 3# jet fuel and clean diesel blending components that meet the National VI standard. Hydrocracking technology has gradually developed into a key secondary processing technology for modern refining enterprises to directly produce clean oil products and high-quality chemical raw materials from inferior wax oil. It is also the core of refining structure adjustment, transformation and upgrading. The core of hydrocracking technology is the development and optimization of high-performance hydrocracking catalysts.

[0003] The hydrocracking catalysts used in industrial applications mainly include alumina, molecular sieves, active metals and silicon-alumina oxides, among which alumina, molecular sieves and silicon-alumina oxides constitute the carrier. The main function of the carrier is to provide suitable acidic sites during the hydrocracking reaction to promote the chemical bond breaking of heavy oil molecules and provide abundant specific surface area. The active metal mainly provides hydrogenation function. The acidic components of the hydrocracking catalysts prepared by existing methods are mostly borne by Y-type molecular sieves, Y molecular sieves and β molecular sieves, and Y molecular sieves and SAPO-34 molecular sieves. Summary of the invention

[0004] The present invention is made in order to increase the surface hydroxyl density of the hydrocracking catalyst carrier, improve the metal dispersion in the catalyst, reduce the interaction between the carrier and the metal in the catalyst, improve the synergistic effect of the hydrogenation center and the acid center while improving the metal utilization, so that the hydrocracking catalyst can process inferior wax oil raw materials stably for a long period of time.

[0005] As a first aspect of the present invention, it relates to a wax oil hydrocracking catalyst, which mainly comprises the following components by weight: 1 to 30 parts of meso-microporous SBA-15 / HY composite molecular sieve; 15 to 40 parts of amorphous silica-alumina; 5 to 30 parts of mesoporous alumina; 10 to 30 parts of metal W or Mo oxide; 1 to 8 parts of metal Co or Ni oxide; 1.0 to 5.0 parts of extrusion aid; 3 to 8 parts of adhesive;

[0006] The meso-microporous SBA-15 / HY composite molecular sieve is prepared under ultrasonic emulsification.

[0007] In one or some optional embodiments, the meso-microporous SBA-15 / HY composite molecular sieve has a grain size of 150-300 nm and a specific surface area of ​​510-550 m 2 / g, the pore volume is 0.60~0.75ml / g, the pore size distribution is 7.5~8.5nm, and the total acid content is 0.18~0.28mmol / g.

[0008] In one or some optional embodiments, the specific surface area of ​​the amorphous silicon aluminum is 200 to 550 m 2 / g.

[0009] In one or some optional embodiments, the specific surface area of ​​the mesoporous alumina is 250 to 450 m 2 / g.

[0010] In one or some optional embodiments, the extrusion aid is at least one of starch, sesbania powder, polyethylene glycol, and methyl cellulose.

[0011] In one or some optional embodiments, the adhesive is made of an inorganic acid and / or an organic acid; the inorganic acid is at least one of hydrochloric acid, nitric acid, phosphoric acid and sulfuric acid; the organic acid is at least one of formic acid, acetic acid, citric acid and tartaric acid.

[0012] In one or some preferred embodiments, the content of the metal W or Mo oxide is 18 to 28 parts.

[0013] In one or some preferred embodiments, the content of the metal Co or Ni oxide is 3 to 6 parts.

[0014] In one or some preferred embodiments, the content of the extrusion aid is 2 to 4 parts.

[0015] As a second aspect of the present invention, it relates to a method for preparing the above-mentioned wax oil hydrocracking catalyst, which method comprises:

[0016] Amorphous silica-alumina, mesoporous alumina, meso-microporous SBA-15 / HY composite molecular sieve, a binder and an extrusion aid are uniformly mixed, extruded into strips (for example, cylindrical, three-leaf clover or four-leaf clover), dried and calcined to obtain a carrier;

[0017] A dipping solution is prepared by using a compound containing metal W or Mo oxide and metal Co or Ni oxide components and a strong electronegative organic complexing agent;

[0018] The carrier is impregnated with the impregnation solution, and after drying and calcination, a wax oil hydrocracking catalyst is obtained.

[0019] In one or some optional embodiments, the organic complexing agent is at least one of ethylene glycol, propylene glycol, and ethylenediammonium tetraacetic acid.

[0020] As a third aspect of the present invention, it relates to the use of the above-mentioned wax oil hydrocracking catalyst in a wax oil hydrocracking process.

[0021] The invention adopts macroporous amorphous silica-alumina and mesoporous alumina as main carriers and meso-microporous SBA-15 / HY composite molecular sieve as acidic components, thereby optimizing the pore structure and acidic properties of the hydrocracking catalyst; in the hydrocracking process of inferior wax oil, the internal diffusion performance of polycyclic aromatic hydrocarbons in the molecular sieve has a very important influence on the activity of the catalyst; compared with conventional amorphous silica-alumina and alumina, macroporous amorphous silica-alumina, mesoporous alumina and meso-microporous SBA-15 / HY composite molecular sieve have more mesoporous structures, which are beneficial to improving the diffusion rate and ring-opening cracking ability of polycyclic aromatic hydrocarbons and cycloalkanes. In addition, the meso-microporous SBA-15 / HY composite molecular sieve used in the present invention is prepared under ultrasonic emulsification, which makes the composite molecular sieve fit more evenly, thereby making the composite molecular sieve have a smaller grain size, a uniform and regular particle size, and a more concentrated specific surface area, pore volume and pore size distribution range. Therefore, the carrier and catalyst prepared from the meso-microporous SBA-15 / HY composite molecular sieve can expose more acidic centers, increase the accessibility of reactants and catalysts, and the catalyst performance is stable and the activity is higher.

[0022] The present invention uses a strongly electronegative organic complexing agent during the metal impregnation process, thereby increasing the hydroxyl density on the carrier surface, improving the metal dispersion, and reducing the interaction between the carrier and the metal. While improving the metal utilization rate, the synergistic effect of the hydrogenation center and the acid center is also improved, so that the hydrocracking catalyst can process inferior wax oil raw materials and operate stably for a long period of time.

[0023] The wax oil hydrocracking catalyst provided by the present invention can effectively inhibit over-cracking in the hydrocracking reaction of low-quality wax oil rich in macromolecules, improve the conversion selectivity of wax oil macromolecular reactants to target products, increase the production of naphtha as a reforming raw material, light naphtha and cracking tail oil as ethylene cracking raw materials, and produce aviation kerosene as No. 3 jet fuel in the process of wax oil hydrocracking, and effectively improve the smoke point of aviation kerosene and reduce the freezing point of aviation kerosene.

[0024] The wax oil hydrocracking catalyst provided by the invention is suitable for the production process of producing high-quality chemical raw materials and aviation kerosene by hydrocracking of wax oil distillate at 220-570 DEG C. The naphtha yield after hydrocracking is generally 50-60wt%, the aromatic potential of heavy naphtha is greater than 45%, and the sulfur and nitrogen contents are both less than 0.5μg / g; the aviation kerosene yield is 10-15wt%, the smoke point is greater than 25.5mm, the freezing point is less than -60DEG C, and the flash point is greater than 50DEG C; the National VI clean diesel yield is 8-15%, and the diesel cetane number is 62.2; the light naphtha+tail oil yield is 15-20%, and the BMCI value of the tail oil can be reduced to below 10. Both the light naphtha and the tail oil can be used as high-quality ethylene cracking raw materials with low BMCI value. The technology can reduce diesel and increase the production of chemical raw materials at the same time, which is conducive to the transformation of oil refining to chemical industry. DETAILED DESCRIPTION

[0025] The following is a detailed description of the embodiments of the present invention: The embodiments of the present invention are implemented on the premise of the technical solution of the present invention, and detailed implementation methods and processes are given, but the protection scope of the present invention is not limited to the following embodiments. The process parameters for which specific conditions are not specified in the following embodiments are generally based on conventional conditions.

[0026] The endpoints and any values ​​of the ranges disclosed in the present invention 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 regarded as specifically disclosed in the present invention.

[0027] The inventors implemented the relevant technical scheme with reference to patent CN201410711529 and found that the hydrocracking catalyst carrier prepared by the scheme has low mesoporous channel content, and the metal loading method adopts the conventional equal volume impregnation method, with high metal content, resulting in low specific surface area of ​​the carrier material after metal loading. The inventors implemented the relevant technical scheme with reference to patent CN200710064672.9 and found that the impregnation method for loading metal is the conventional equal volume impregnation method or the excess saturation impregnation method, with high metal content, resulting in low specific surface area of ​​the carrier material after metal loading. The inventors implemented the relevant technical scheme with reference to patent CN201811521961.1 and found that the method is only a mechanical mixing of Y molecular sieve and SAPO-34 molecular sieve, while the present technology adopts meso-microporous SBA-15 / HY composite molecular sieve as the acidic component, with high mesoporous channel content and large average pore size, which is suitable for the hydrocracking process of inferior wax oil raw materials rich in polycyclic aromatic hydrocarbons. The inventor implemented the relevant technical scheme with reference to patent CN201811522285.X and found that the method is only a mechanical mixture of Y molecular sieve and SAPO-34 molecular sieve. Compared with the present technology, the mesoporous channel content is low and it is mainly used to produce more intermediate distillates. The inventor implemented the relevant technical scheme with reference to patent WO2020119754A1 and found that the method for preparing hydrocracking catalyst contains acid optimization of SAPO-34 molecular sieve, but only silane is used as a regulator in the synthetic material, which is costly and not conducive to reducing catalyst costs and popularizing industrialization. The inventor implemented the relevant technical scheme with reference to patent CN105709844A and found that the catalyst prepared by the method has low selectivity for aviation kerosene. The inventor implemented the relevant technical scheme with reference to patent CN104667969B and found that the catalyst prepared by the method has relatively low selectivity for oil.

[0028] Since the above methods did not meet the inventor's expectations, the inventor made the present invention after further research and development.

[0029] The properties of the macroporous amorphous silica-alumina and mesoporous alumina used in the examples of the present invention are shown in Table 1; the properties of the conventional amorphous silica-alumina and alumina used in the comparative examples of the present invention are shown in Table 2.

[0030] Table 1 Properties of macroporous amorphous silica-alumina and mesoporous alumina

[0031] project Macroporous amorphous silicon aluminum project Mesoporous Alumina Pore ​​size distribution, nm Pore ​​size distribution, nm 2-4 10.0 2-10 3.7 4-10 59.2 10-20 90.5 10-60 30.8 20-50 5.8 Pore ​​volume, mL / g 0.88 Pore ​​volume, mL / g 1.13 <![CDATA[S BET ,m 2 / g]]> 325 <![CDATA[S BET ,m 2 / g]]> 388

[0032] Table 2 Properties of conventional amorphous silicon aluminum and aluminum oxide

[0033] project Conventional amorphous silicon aluminum project Conventional Alumina Pore ​​size distribution, nm Pore ​​size distribution, nm 2-4 34.5 2-10 15.7 4-10 57.9 10-20 46.8 10-60 7.6 20-50 37.5 Pore ​​volume, mL / g 0.66 Pore ​​volume, mL / g 0.67 <![CDATA[S BET ,m 2 / g]]> 268 <![CDATA[S BET ,m 2 / g]]> 256

[0034] The meso-microporous SBA-15 / HY composite molecular sieve used in the embodiment of the present invention is prepared by the following method:

[0035] S1: nonionic surfactant P123, inorganic acid and water are mixed, stirred at 20-40°C, and then silicon source is added to carry out hydrolysis reaction at 30-60°C under ultrasonic emulsification conditions for 4-16 hours, and solid hydrolysis product and mother liquor are obtained after filtration;

[0036] S2 adds the mother liquor into the reactor, and then adds 20-70% P123, 10-60% inorganic acid and 10-40% water based on the amount of P123, inorganic acid and water added in S1, stirring at 20-30°C, and then adds silicon source at 30-60°C for hydrolysis reaction under ultrasonic emulsification conditions, and obtains solid hydrolysis product and mother liquor after filtration;

[0037] S3 repeats S2 for 5 to 20 times, combines all the solid hydrolyzates obtained, and hydrothermally crystallizes the combined solid hydrolyzates with a small amount of mother liquor to obtain a crystallized product;

[0038] S4 Under room temperature conditions, the crystallized product is dissolved in hydrochloric acid solution, stirred for 8 to 16 hours, and then HY molecular sieve is added. After stirring for 4 to 6 hours, the mixture is filtered, dried, and calcined to obtain the meso-microporous SBA-15 / HY composite molecular sieve.

[0039] The silicon source involved in the above method can be methyl orthosilicate, ethyl orthosilicate, butyl orthosilicate, silica sol or water glass; the inorganic acid involved in the above method can be hydrochloric acid, phosphoric acid, nitric acid or carbonic acid.

[0040] The properties of the meso-microporous SBA-15 / HY composite molecular sieve prepared by the above method are shown in Table 3.

[0041] Table 3 Properties of the meso-microporous SBA-15 / HY composite molecular sieve of the present invention

[0042] project Meso-microporous SBA-15 / HY composite molecular sieve <![CDATA[Specific surface area, m 2 / g]]> 510-550 Pore ​​volume, ml / g 0.60-0.75 Average pore size, nm 7.5-8.5 Grain size, nm 150-300 B acid, mmol / g 0.06-0.10 L acid, mmol / g 0.13-0.18 Total acid content, mmol / g 0.18-0.28

[0043] Example 1

[0044] 32g of meso-microporous SBA-15 / HY composite molecular sieve (its properties are shown in Table 3), 74g of mesoporous alumina (Henghuan Aluminum, its properties are shown in Table 1), 86g of macroporous amorphous silica-alumina (Henghuan Aluminum, its properties are shown in Table 1) and 5.0g of sesbania powder (Dongfang Huabo) were mixed evenly, and a mixed solution prepared by 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water was added dropwise, stirred evenly, kneaded on a twin-screw extruder, and then extruded into 1.5mm cylinders, dried at 110℃ for 2h, and calcined at 550℃ in air atmosphere for 4h to prepare a carrier. Then, an impregnation solution prepared by 100mL of water, 8g of ethylenediammonium tetraacetic acid, 26g of nickel nitrate and 37g of ammonium metatungstate was used to impregnate the carrier for 2h, dried at 120℃ for 4h, and calcined at 500℃ in air atmosphere for 4h to prepare catalyst A, whose physical and chemical properties are shown in Table 4.

[0045] Example 2

[0046] 26g of meso-microporous SBA-15 / HY composite molecular sieve (its properties are shown in Table 3), 74g of mesoporous alumina (Henghuan Aluminum, its properties are shown in Table 1), 86g of macroporous amorphous silica-alumina (Henghuan Aluminum, its properties are shown in Table 1) and 5.0g of sesbania powder (Dongfang Huabo) were mixed, and a mixed solution prepared by 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water was added dropwise, stirred evenly, kneaded on a twin-screw extruder, extruded into 1.5mm cylinders, dried at 110℃ for 2h, and calcined at 550℃ in air atmosphere for 4h to prepare a carrier. Then, an impregnation solution prepared by 100mL of water, 5g of propylene glycol, 26g of nickel nitrate and 37g of ammonium metatungstate was used to impregnate the carrier for 2h, dried at 120℃ for 4h, and calcined at 500℃ in air atmosphere for 4h to prepare catalyst B, whose physical and chemical properties are shown in Table 4.

[0047] Example 3

[0048] 38g of meso-microporous SBA-15 / HY composite molecular sieve (its properties are shown in Table 3), 74g of mesoporous alumina (Henghuan Aluminum, its properties are shown in Table 1), 86g of macroporous amorphous silica-alumina (Henghuan Aluminum, its properties are shown in Table 1) and 5.0g of sesbania powder (Dongfang Huabo) were mixed, and a mixed solution prepared by 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water was added dropwise. After stirring evenly, the mixture was kneaded on a twin-screw extruder, extruded into 1.5mm cylindrical shapes, dried at 110℃ for 2h, and calcined at 550℃ in air atmosphere for 4h to prepare a carrier. Then, an impregnation solution prepared by 100mL of water, 5g of propylene glycol, 26g of nickel nitrate and 37g of ammonium metatungstate was used to impregnate the carrier for 2h, dried at 120℃ for 4h, and calcined at 500℃ in air atmosphere for 4h to prepare catalyst C, whose physical and chemical properties are shown in Table 4.

[0049] Example 4

[0050] 32g of meso-microporous SBA-15 / HY composite molecular sieve (its properties are shown in Table 3), 74g of mesoporous alumina (Henghuan Aluminum, its properties are shown in Table 1), 86g of macroporous amorphous silica-alumina (Henghuan Aluminum, its properties are shown in Table 1) and 5.0g of sesbania powder (Dongfang Huabo) were mixed, and a mixed solution prepared by 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water was added dropwise, stirred evenly, kneaded on a twin-screw extruder, extruded into 1.5mm cylindrical shapes, dried at 110℃ for 2h, and calcined at 550℃ in air atmosphere for 4h to prepare a carrier. Then, the catalyst was impregnated with an impregnation solution prepared by dissolving 26g of nickel nitrate and 37g of ammonium metatungstate in 100mL of water for 2h, dried at 120℃ for 4h, and calcined at 500℃ in air atmosphere for 4h to prepare a catalyst D, whose physical and chemical properties are shown in Table 4.

[0051] Comparative Example 1

[0052] 25g of conventional Y molecular sieve, 75g of conventional alumina (its properties are shown in Table 2), 90g of conventional amorphous silica-alumina (its properties are shown in Table 2) and 5.0g of sesbania powder (Oriental glass) were added dropwise to a mixed solution of 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water, stirred evenly, kneaded on a twin-screw extruder, extruded into 1.5mm cylindrical shapes, dried at 110°C for 2h, and calcined at 550°C in air atmosphere for 4h to prepare a carrier. Then, the catalyst was impregnated with an impregnation solution prepared by dissolving 26g of nickel nitrate and 37g of ammonium metatungstate in 100mL of water for 2h, dried at 120°C for 4h, and calcined at 500°C in air atmosphere for 4h to prepare a catalyst E, the physical and chemical properties of which are shown in Table 4.

[0053] Comparative Example 2

[0054] 32g of conventional Y molecular sieve, 72g of conventional alumina (its properties are shown in Table 2), 85g of conventional amorphous silica-alumina (its properties are shown in Table 2) and 5.0g of sesbania powder (Oriental glass) were mixed, and a mixed solution of 4.5g of concentrated nitric acid (96wt%), 4.2g of citric acid and 105g of water was added dropwise and stirred evenly, and then kneaded on a twin-screw extruder, extruded into 1.5mm cylindrical shapes, dried at 110℃ for 2h, and calcined at 550℃ in air atmosphere for 4h to prepare a carrier. Then, the catalyst was impregnated with an impregnation solution prepared by dissolving 26g of nickel nitrate and 37g of ammonium metatungstate in 100mL of water for 2h, dried at 120℃ for 4h, and calcined at 500℃ in air atmosphere for 4h to prepare a catalyst F, whose physical and chemical properties are shown in Table 4.

[0055] Table 4 is a table showing the physical and chemical properties of catalysts A to F prepared in Examples 1 to 4 and Comparative Examples 1 to 2.

[0056] Table 4 Physicochemical properties of catalysts

[0057]

[0058] From the analysis of Table 4, it can be seen that the pore size (2-60nm), volume, specific surface area, pore volume, strength and other properties of catalysts A, B, C, and D prepared in Examples 1 to 4 of the present invention are significantly higher than those of catalysts E and F prepared in Comparative Examples 1 and 2, and the total acid content is also slightly higher, but the amount of active metal components is equivalent.

[0059] Example 5

[0060] This example introduces the evaluation results of the catalyst for treating low-quality wax oil.

[0061] The catalysts A to F prepared in Examples 1 to 4 and Comparative Examples 1 to 2 were crushed into particles with a length of 2 to 3 mm, and compared and evaluated on a 200 mL fixed bed hydrogenation device using straight run diesel as a raw material, with 100 mL of the catalyst loaded. The catalysts were sulfurized with kerosene containing 2% carbon disulfide, and the reaction conditions after sulfurization may be: reaction temperature 320 to 400°C, hydrogen partial pressure 14 to 18 MPa, cracking hydrogen to oil volume ratio 800 to 1500:1, liquid hourly volume space velocity 1.0 to 3.0 h -1 .

[0062] The main properties of the feedstock oil used in this example are shown in Table 5, and the catalyst performance evaluation results are shown in Table 6.

[0063] Table 5 Main properties of wax oil raw materials

[0064]

[0065] Table 6 Comparative evaluation of catalyst performance

[0066]

[0067] Note: Reaction pressure 15.0MPa, cracking reaction temperature 372℃, hydrogen-oil volume ratio 1500:1, volume space velocity 1.5h -1 It can be seen from Table 6 that under the same evaluation process conditions, compared with the catalysts E and F prepared in Comparative Examples 1 and 2, the catalysts A to D prepared in Examples 1 to 4 of the present invention have high liquid yield, high total yield of chemical raw materials, and low BMCI value of tail oil when treating inferior wax oil; the heavy naphtha has high aromatic potential, that is, the catalyst provided by the invention has excellent hydrocracking performance and good selectivity for target chemical raw materials products, which can help the transformation and upgrading of oil refining to chemical industry.

[0068] Although the specific embodiments of the present invention have been described in detail, it will be understood by those skilled in the art. According to all the teachings disclosed, various modifications and replacements can be made to those details, and these changes are all within the protection scope of the present invention. The full scope of the present invention is given by the attached claims and any equivalents thereof.

Claims

1. A wax oil hydrocracking catalyst, characterized in that: The wax oil hydrocracking catalyst mainly comprises the following components by weight: 1 to 30 parts of meso-microporous SBA-15 / HY composite molecular sieve; 15-40 parts of amorphous silicon aluminum; 5-30 parts of mesoporous alumina; 10 to 30 parts of metal W or Mo oxide; 1 to 8 parts of metal Co or Ni oxide; 1.0-5.0 parts of extrusion aid; 3 to 8 parts of adhesive; The meso-microporous SBA-15 / HY composite molecular sieve is prepared under ultrasonic emulsification.

2. The wax oil hydrocracking catalyst according to claim 1, characterized in that The crystal size of the meso-microporous SBA-15 / HY composite molecular sieve is 150-300 nm, and the specific surface area is 510-550 m 2 / g, the pore volume is 0.60~0.75ml / g, the pore size distribution is 7.5~8.5nm, and the total acid content is 0.18~0.28mmol / g.

3. The wax oil hydrocracking catalyst according to claim 1, characterized in that The specific surface area of ​​the amorphous silicon aluminum is 200 to 550 m 2 / g.

4. The wax oil hydrocracking catalyst according to claim 1, characterized in that The specific surface area of ​​the mesoporous alumina is 250 to 450 m 2 / g.

5. The wax oil hydrocracking catalyst according to claim 1, characterized in that The extrusion aid is at least one of starch, sesbania powder, polyethanol and methyl cellulose.

6. The wax oil hydrocracking catalyst according to claim 1, characterized in that The adhesive is made of inorganic acid and / or organic acid; the inorganic acid is at least one of hydrochloric acid, nitric acid, phosphoric acid and sulfuric acid; the organic acid is at least one of formic acid, acetic acid, citric acid and tartaric acid.

7. The wax oil hydrocracking catalyst according to claim 1, characterized in that The content of the metal W or Mo oxide is 18 to 28 parts.

8. The wax oil hydrocracking catalyst according to claim 1, characterized in that The content of the metal Co or Ni oxide is 3 to 6 parts.

9. The wax oil hydrocracking catalyst according to claim 1, characterized in that The content of the extrusion aid is 2 to 4 parts.

10. A method for preparing the wax oil hydrocracking catalyst according to any one of claims 1 to 9, characterized in that: The method comprises: Amorphous silicon-alumina, alumina, meso-microporous SBA-15 / HY composite molecular sieve, adhesive and extrusion aid are uniformly mixed, extruded into strips, dried and calcined to obtain a carrier; A dipping solution is prepared by using a compound containing metal W or Mo oxide and metal Co or Ni oxide components and a strong electronegative organic complexing agent; The carrier is impregnated with the solution, and after drying and calcination, a wax oil hydrocracking catalyst is obtained.

11. The method according to claim 10, characterized in that The organic complexing agent is at least one of ethylene glycol, glycerol, and ethylenediammonium tetraacetic acid.

12. Use of the wax oil hydrocracking catalyst according to any one of claims 1 to 9 in a wax oil hydrocracking process.

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