A hydrogenation catalyst for a raw material rich in bicyclic aromatic hydrocarbons, and a preparation method and application thereof

Abstract

The present disclosure relates to a hydrogenation catalyst for a raw material rich in bicyclic aromatic hydrocarbons, the hydrogenation catalyst comprising a carrier and an active metal component supported on the carrier; the active metal component comprising a Group VIII metal element and a Group VIB metal element; the carrier comprising an acidic component and a heat-resistant inorganic oxide matrix, the acidic component being a molecular sieve with an N value greater than 0.6 and an I value greater than 1; the N value being defined as the ratio of the adsorption amount of the bicyclic aromatic hydrocarbons and derivatives thereof on the molecular sieve to be tested to the adsorption amount of the bicyclic aromatic hydrocarbons and derivatives thereof on a standard molecular sieve, the standard molecular sieve being a HY molecular sieve with a SiO2 and Al2O molar ratio of 5.4 and a unit cell constant of 24.60 angstroms; the I value being defined as the ratio of the square of the adsorption amount of methylindane on the molecular sieve to be tested to the product of the adsorption amount of tetralin and the adsorption amount of butylbenzene on the molecular sieve to be tested. The catalyst of the present disclosure can improve the yield of methylindane type substances produced from bicyclic aromatic hydrocarbon materials.

Description

Technical Field

[0001] This disclosure relates to the field of catalysts, and more specifically, to a hydrogenation catalyst for bicyclic aromatic hydrocarbon-rich feedstocks, its preparation method, and its application. Background Technology

[0002] With the demand for refined oil products gradually reaching saturation, and the standard for aromatic content in diesel fuel approaching zero in various standards, the utilization of bicyclic catalytic diesel fuel has attracted considerable attention. Based on the compositional characteristics of catalytic diesel fuel rich in bicyclic aromatics and the characteristics of bicyclic aromatic hydrocarbon hydrogenation reactions, it is possible to consider hydrogenating bicyclic catalytic diesel fuel to prepare methyl indenhydride-like substances. This is not only a valuable chemical raw material but can also be used as a feedstock for the production of BTX-like substances. Molecular sieves are key to controlling the hydrogenation reaction process.

[0003] In existing technologies, the use of Y-type and Beta-type molecular sieve catalysts is frequently reported, for example:

[0004] Chinese patent document CN106268922 discloses a hydrogenation catalyst and its application. The hydrogenation catalyst contains a support and at least one metal component selected from Group VIII and at least one metal component selected from Group VIB. The support contains alumina, Y-type molecular sieve, and silica. Based on the support, the content of Y-type molecular sieve is 3% to 70% by weight, the content of alumina is 20% to 94% by weight, and the content of silica is 3% to 40% by weight. The characteristic feature is that the support is obtained by mixing, molding, drying, and calcining Y-type molecular sieve with boehmite. The boehmite includes PB1. Characterized by X-ray diffraction, the κ1 and κ2 of PB1 are greater than 1 and less than or equal to 3, respectively, where κ1 = h2 / h1 and κ2 = h3 / h2. h1, h2, and h3 are the peak heights of three diffraction peaks at 2θ angles of 24-30°, 35-41°, and 46-52° in the X-ray diffraction pattern of PB1. When this catalyst is used to process catalytic cracking tail oil under medium-pressure conditions, the relative reduction in the balanced aromatic content of the tail oil can reach 10% to 35%.

[0005] Chinese patent document CN107999120 discloses a hydrated alumina composition, its preparation method, a molded body, its preparation method, and its applications. The composition contains hydrated alumina, a Beta molecular sieve, and a compound having at least two proton acceptor sites, and the composition's molecular weight is 5 or less. This document also discloses a hydrogenation catalytic catalyst using a molded body formed from the hydrated alumina composition as a support, its preparation method, and a hydrocracking method. The catalyst using the molded body prepared from this hydrated alumina composition as a support exhibits higher catalytic activity in the hydrocracking of hydrocarbon oils.

[0006] The acidic components of existing catalysts are mainly Y-type or Beta-type catalysts. Although they can produce gasoline, diesel, or BTX, the yield of methyl indenium compounds is low. Summary of the Invention

[0007] The purpose of this disclosure is to provide a hydrotreating catalyst to improve the yield of methyl indane compounds (including branched methyl indane) produced from bicyclic aromatic hydrocarbon feedstocks.

[0008] To achieve the above objectives, the first aspect of this disclosure provides a hydrogenation catalyst for a feedstock rich in bicyclic aromatic hydrocarbons, the hydrogenation catalyst comprising a support and an active metal component supported on the support; the active metal component comprising Group VIII metal elements and Group VIB metal elements; the support comprising an acidic component and a heat-resistant inorganic oxide matrix, the acidic component being a molecular sieve with an N value greater than 0.6 and an I value greater than 1;

[0009] The N value of a certain molecular sieve to be tested is defined as the ratio of the adsorption amount of the molecular sieve to bicyclic aromatic hydrocarbons and their derivatives to that of a standard molecular sieve. The standard molecular sieve is a HY molecular sieve with a SiO2 to Al2O molar ratio of 5.4 and a cell constant of 24.60 Å. The I value of a certain molecular sieve to be tested is defined as the ratio of the square of the adsorption amount of the molecular sieve to methyl indene to the product of the adsorption amount of the molecular sieve to tetrahydronaphthalene and the adsorption amount of the molecular sieve to butylbenzene.

[0010] Optionally, the acidic component has an I value of 1-100 and an N value of 0.6-100; preferably, the acidic component has an I value of 1-10 and an N value of 0.6-10; the acidic component has a pore volume of 0.4-0.8 cm³. 3 / g, acid density is 0.8-2.5μmol / m 2 .

[0011] Optionally, the acidic component is selected from one of OSB-1 molecular sieve, Linde Type A molecular sieve, SSZ-35 molecular sieve, ITQ-52 molecular sieve, SSZ-59 molecular sieve, SSZ-53 molecular sieve, SSZ-23 molecular sieve, SSZ-44 molecular sieve, SSZ-52 molecular sieve, CIT-1 molecular sieve, and AlPO-52 molecular sieve.

[0012] Optionally, based on the total weight of the carrier, the content of the acidic component is 30-90% by weight, preferably 45-80% by weight; and the content of the heat-resistant inorganic oxide matrix is ​​10-70% by weight, preferably 20-55% by weight.

[0013] Optionally, based on the total weight of the catalyst and calculated as oxides, the catalyst contains 1-10% by weight of a Group VIII metal and 2-40% by weight of a Group VIB metal; preferably, the catalyst contains 1-6% by weight of a Group VIII metal and 5-25% by weight of a Group VIB metal.

[0014] Optionally, the heat-resistant inorganic oxide matrix is ​​selected from at least one of alumina, silicon oxide, and silicon-alumina.

[0015] A second aspect of this disclosure provides a method for preparing the above-mentioned hydrogenation catalyst, the method comprising:

[0016] S1. The heat-resistant inorganic oxide matrix and molecular sieve are mixed, kneaded, and extruded to obtain an extruded strip; the extruded strip is subjected to a first drying and a first calcination to obtain a carrier;

[0017] S2. The carrier is impregnated with an aqueous solution of a compound containing a Group VIII metal and a Group VIB metal to obtain an impregnated carrier; the impregnated carrier is then subjected to a second drying and activation treatment.

[0018] Optionally, the weight ratio of the heat-resistant inorganic oxide matrix to the molecular sieve is 1-7:9-3.

[0019] Optionally, in step S1, the conditions for the first drying treatment include: a drying temperature of 80-300℃, preferably 100-200℃; and a drying time of 1-12 hours, preferably 2-8 hours; the conditions for the first calcination include: a calcination temperature of 350-850℃, preferably 450-650℃; and a calcination time of 1-12 hours, preferably 2-6 hours; in step S2, the conditions for the impregnation include: an impregnation temperature of 20-150℃; and an impregnation time of 1-6 hours; the conditions for the second drying include: a temperature of 100-300℃, preferably 100-200℃; and a time of 2-8 hours; and the conditions for the activation treatment include: a temperature of 250-650℃, preferably 300-500℃; and a time of 1-12 hours, preferably 2-6 hours.

[0020] A third aspect of this disclosure provides a method for hydrocracking a feedstock oil rich in bicyclic aromatics, wherein the feedstock oil and hydrogen are contacted with the aforementioned hydrocracking catalyst and subjected to a hydrocracking reaction.

[0021] Through the above technical solution, this disclosure effectively controls the reaction depth and improves the conversion depth and isomer selectivity of bicyclic aromatics by regulating the matching of the molecular sieve pore structure with different reaction intermediates in the ring-opening process of aromatic hydrogenation. The catalyst disclosed herein can improve the yield of methylindane-like substances, including branched methylindane, produced from bicyclic aromatic materials, and can be used in the hydrogenation of low-grade diesel oil to produce methylindane-like substances.

[0022] Other features and advantages of this disclosure will be described in detail in the following detailed description section. Detailed Implementation

[0023] The following provides a detailed description of specific embodiments of this disclosure. It should be understood that the specific embodiments described herein are for illustrative and explanatory purposes only and are not intended to limit this disclosure.

[0024] The first aspect of this disclosure provides a hydrogenation catalyst for a bicyclic aromatic hydrocarbon-rich feedstock, the hydrogenation catalyst comprising a support and an active metal component supported on the support; the active metal component comprising Group VIII metal elements and Group VIB metal elements; the support comprising an acidic component and a heat-resistant inorganic oxide matrix, the acidic component being a molecular sieve with an N value greater than 0.6 and an I value greater than 1;

[0025] The N value of a certain molecular sieve to be tested is defined as the ratio of the adsorption amount of the molecular sieve to bicyclic aromatic hydrocarbons and their derivatives to that of a standard molecular sieve. The standard molecular sieve is a HY molecular sieve with a SiO2 to Al2O molar ratio of 5.4 and a cell constant of 24.60 Å. The I value of a certain molecular sieve to be tested is defined as the ratio of the square of the adsorption amount of the molecular sieve to methyl indene to the product of the adsorption amount of the molecular sieve to tetrahydronaphthalene and the adsorption amount of the molecular sieve to butylbenzene.

[0026] This disclosure improves the catalyst's conversion ability for indane molecules by selecting molecular sieves with higher N and I values, thereby providing a catalyst with high indane selectivity that can be used in the hydrocracking process of inferior diesel oil, thus achieving the maximum conversion of bicyclic aromatics.

[0027] The method for testing the N-value adsorption molar ratio disclosed herein is as follows: First, accurately measure 100 mL of naphthalene solution at room temperature, then add a fixed amount of molecular sieve material (5 g), and stir under an inert gas (N2) atmosphere at 1 atm for 360°C in a sealed environment for 10 hours. Then filter the solution, dilute the filtrate to the correct volume, cool to room temperature, and measure the solution volume again using a graduated cylinder to obtain the adsorption volume difference ΔV. 测试分子筛 The formula for calculating N is:

[0028] N=(ΔV 测试分子筛* M测试分子筛 ) / (ΔV Y型分子筛* M Y型分子筛 )

[0029] Where ΔV 测试分子筛 , ΔV Y型分子筛 To test the volume difference in adsorption of tetrahydronaphthalene between molecular sieves and Y-type molecular sieves, M 测试分子筛 M Y型分子筛 To test the molar mass of molecular sieves and Y-type molecular sieves.

[0030] The I-value adsorption molar ratio test method disclosed herein is as follows: First, accurately measure 100 mL of tetrahydronaphthalene solution, methylindene, and butylbenzene (at room temperature), respectively. Then, add a quantitative amount of molecular sieve material (5 g). Under inert gas (N2) protection, at 1 atm, and constant temperature and stirring at 360°C for 10 hours, the mixture is then filtered. The filtrate is re-diluted to the required volume and cooled to room temperature. The volume of the solution is then measured again using a graduated cylinder to obtain the adsorption volume difference ΔV. 测试分子筛_甲基茚满 ΔV 测试分子筛_四氢萘 ΔV 测试分子筛_丁基苯 The formula for calculating the I value is:

[0031] SQN=ΔV 测试分子筛_丁基苯 2 / (ΔV 测试分子筛_甲基茚满* ΔV 测试分子筛_四氢萘 )

[0032] Where ΔV 测试分子筛_四氢萘 ΔV must be greater than 0 测试分子筛_丁基苯 It can be equal to 0.

[0033] In a preferred embodiment of this disclosure, the acidic component has an I value of 1-100 and an N value of 0.6-100; more preferably, the acidic component has an I value of 1-10 and an N value of 0.6-10; optionally, the pore volume of the acidic component can be 0.4-0.8 cm³. 3 / g, acid density can be 0.8-2.5μmol / m 2 .

[0034] According to this disclosure, the acidic component may be selected from one of OSB-1 molecular sieve, Linde Type A molecular sieve, SSZ-35 molecular sieve, ITQ-52 molecular sieve, SSZ-59 molecular sieve, SSZ-53 molecular sieve, SSZ-23 molecular sieve, SSZ-44 molecular sieve, SSZ-52 molecular sieve, CIT-1 molecular sieve, and AlPO-52 molecular sieve.

[0035] According to this disclosure, based on the total weight of the carrier, the content of the acidic component can be 30-90% by weight, preferably 45-80% by weight; the content of the heat-resistant inorganic oxide matrix can be 10-70% by weight, preferably 20-55% by weight.

[0036] According to this disclosure, based on the total weight of the catalyst and calculated as oxides, the catalyst may contain 1-10% by weight of Group VIII metals and 2-40% by weight of Group VIB metals; preferably, the catalyst may contain 1-6% by weight of Group VIII metals and 5-25% by weight of Group VIB metals.

[0037] According to this disclosure, the heat-resistant inorganic oxide matrix can be selected from at least one of alumina, silicon oxide, and silicon-alumina. The alumina is selected from one or more transition phases of γ, η, θ, δ, and χ, or it can be alumina containing one or more transition phases of γ, η, θ, δ, and χ selected from silicon, titanium, magnesium, boron, zirconium, thorium, niobium, and rare earth additives, preferably γ-alumina and γ-alumina containing one or more additives selected from silicon, phosphorus, titanium, magnesium, boron, zirconium, thorium, niobium, and rare earth. These can be commercially available or obtained using any existing method. Silicon-alumina preferably has a pseudo-boehmite structure and can also be commercially available or prepared using any existing technology. For example, the Siral series of commercially available silicon-alumina products manufactured by Condea GmbH in Germany have a pseudo-boehmite structure and can be used in this disclosure.

[0038] The catalyst provided in this disclosure can be used in any reactor capable of contacting the feedstock with the catalyst under hydrotreating conditions, for example, in a fixed-bed reactor, a moving-bed reactor, or a fluidized-bed reactor. Other types of hydrocarbon feedstocks can also be directly processed for hydrotreating. The hydrocarbon feedstock can also be various heavy mineral oils or synthetic oils or their mixed distillate fractions, such as those selected from crude oil, distillate oils, solvent-refined oils, wax pastes, under-wax oils, Fischer-Tropsch synthetic oils, coal liquefaction oils, light deasphalted oils, and heavy deasphalted oils. It is particularly suitable for hydrotreating or hydrocracking processes of diesel oil, especially inferior diesel oil rich in bicyclic aromatics.

[0039] A second aspect of this disclosure provides a method for preparing the above-mentioned hydrogenation catalyst, the method comprising:

[0040] S1. The heat-resistant inorganic oxide matrix and molecular sieve are mixed, kneaded, and extruded to obtain an extruded strip; the extruded strip is subjected to a first drying and a first calcination to obtain a carrier;

[0041] S2. The carrier is impregnated with an aqueous solution of a compound containing a Group VIII metal and a Group VIB metal to obtain an impregnated carrier; the impregnated carrier is then subjected to a second drying and activation treatment.

[0042] According to this disclosure, the weight ratio of the heat-resistant inorganic oxide matrix to the molecular sieve can be 1-7:9-3.

[0043] According to this disclosure, in step S1, the conditions for the first drying treatment may include: a drying temperature of 80-300℃, preferably 100-200℃; and a drying time of 1-12 hours, preferably 2-8 hours; the conditions for the first calcination may include: a calcination temperature of 350-850℃, preferably 450-650℃; and a calcination time of 1-12 hours, preferably 2-6 hours; in step S2, the conditions for the impregnation may include: an impregnation temperature of 20-150℃; and an impregnation time of 1-6 hours; the conditions for the second drying may include: a temperature of 100-300℃, preferably 100-200℃; and a time of 2-8 hours; the conditions for the activation treatment may include: a temperature of 250-650℃, preferably 300-500℃; and a time of 1-12 hours, preferably 2-6 hours.

[0044] A third aspect of this disclosure provides a method for hydrocracking a feedstock oil rich in bicyclic aromatics, wherein the feedstock oil and hydrogen are contacted with the aforementioned hydrocracking catalyst to carry out a hydrocracking reaction. Optionally, the hydrocracking reaction is carried out using a fixed-bed single-stage series process and a diesel cycle process.

[0045] The present disclosure will be further illustrated by the following examples, but the present disclosure is not limited thereto.

[0046] Unless otherwise specified, all reagents used in the examples are chemically pure.

[0047] The adsorption molar ratio test method disclosed herein is as follows: First, accurately measure 100 mL of tetrahydronaphthalene solution, methylindene, and butylbenzene at room temperature. Then, add a quantitative amount of molecular sieve material (5 g). Under inert gas (N2) protection, at 1 atm, and constant temperature and stirring at 360°C for 10 hours, filter the solution, dilute the filtrate to the correct volume, cool to room temperature, and measure the solution volume again using a graduated cylinder. The pore volume is determined by BET, and the acidity is determined by NH3-TPD.

[0048] The properties of molecular sieves are listed in Table 1.

[0049] The adsorption molar ratio test method disclosed herein is as follows: First, accurately measure 100 mL of tetrahydronaphthalene solution at room temperature, then add a quantitative amount of molecular sieve material (1 g), and stir under an inert gas (N2) atmosphere at 1 atm for 360°C in a sealed environment for 10 hours. Then filter, dilute the filtrate to the correct volume, cool to room temperature, and measure the solution volume again using a graduated cylinder. The pore volume is determined by BET, and the acidity is determined by NH3-TPD.

[0050] Examples 1-3 illustrate the catalysts and their preparation methods provided in this disclosure.

[0051] Example 1

[0052] 130.2 g of pseudoboehmite (Catalyst Changling Branch) with a dry basis of 70% and 118.0 g of ITQ-52 molecular sieve with a dry basis of 80% were weighed and extruded into a three-lobed strip with an outer circle diameter of 1.6 mm on an extruder. The strip was dried at 120℃ for 3 hours and calcined at 600℃ for 4 hours to obtain catalyst support Z1.

[0053] 100 g of support Z1 was impregnated for 3 hours in 78 mL of a mixed solution containing molybdenum trioxide, basic nickel carbonate, and phosphoric acid, with molybdenum O3 (192.3 g / L), NiO3 (8.5 g / L), and P2O5 (38.5 g / L), respectively. After drying at 120 °C for 2 hours, it was calcined at 450 °C for 3 hours to obtain catalyst C1. The composition based on the catalyst is shown in Table 2.

[0054] Example 2

[0055] 130.2 g of pseudoboehmite (Catalyst Changling Branch) with a dry basis of 70% and 113.7 g of SSZ-44 molecular sieve (marked as A) with a dry basis of 83% were weighed and extruded into a three-lobed strip with an outer circle diameter of 1.6 mm on an extruder. The strip was dried at 120℃ for 3 hours and calcined at 600℃ for 4 hours to obtain catalyst support Z2.

[0056] 100 g of support Z2 was impregnated for 3 hours in 83 mL of a mixed solution containing molybdenum trioxide, basic nickel carbonate, and phosphoric acid, with molybdenum O3 (180.7 g / L), NiO (36.1 g / L), and P2O5 (36.1 g / L), respectively. After drying at 120 °C for 2 hours, it was calcined at 450 °C for 3 hours to obtain catalyst C2. The composition based on the catalyst is shown in Table 2.

[0057] Comparative Example 1

[0058] 130.2 g of pseudoboehmite (Catalyst Changling Branch) with a dry basis of 70% and 110.6 g of Y molecular sieve with a dry basis of 85% were weighed and extruded into a three-lobed strip with an outer circle diameter of 1.6 mm on an extruder. The strip was dried at 120°C for 3 hours and calcined at 600°C for 4 hours to obtain catalyst support Zd.

[0059] 100 g of support Zd1 was impregnated for 3 hours in 80 mL of a mixed solution containing molybdenum trioxide, basic nickel carbonate, and phosphoric acid, with molybdenum O3 (187.5 g / L), NiO (37.5 g / L), and P2O5 (37.5 g / L), respectively. After drying at 120 °C for 2 hours, it was calcined at 450 °C for 3 hours to obtain catalyst DC. The composition of the calcined catalyst is shown in Table 2.

[0060] Table 1

[0061] ITQ-52 0.501 1.478 0.75 2.01 SSZ-44 0.578 1.430 0.74 3.75 Y 0.510 1.522 1.00 1.28

[0062] Table 2

[0063]

[0064]

[0065] Test case

[0066] This test example is used to illustrate the performance of the catalyst provided in this disclosure.

[0067] Using 99% pure tetrahydronaphthalene as raw material (analytical grade), the reaction performance of catalysts C1, C2, and DC provided by this invention was evaluated in a micro-fixed bed reactor. The catalyst loading was 1.0 g, and the reaction conditions were 330℃~390℃ and 4.0 MPa. For better comparison, the following three performance indicators are given and defined, and the results are listed in Table 3.

[0068]

[0069] The yield of indane compounds is the mass fraction of the product containing 1-methylindane, 2-methylindane, etc.

[0070] Indane product selectivity = Indane product yield / Tetrahydronaphthalene conversion × 100%.

[0071] Table 3

[0072] Indene product yield Baseline × 107.7% Baseline × 120.2% benchmark Indane product selectivity Baseline × 158.8% Baseline × 186.9% benchmark

[0073] The results in Table 3 show that, compared with existing catalysts, the catalyst provided in this disclosure has higher cyclic isomerization activity and selectivity in the hydrogenation of bicyclic aromatic hydrocarbons or materials rich in bicyclic aromatic hydrocarbons, such as diesel fuel, and can obtain higher yields and selectivity of indane-like products with five-membered ring structures.

[0074] The preferred embodiments of this disclosure have been described in detail above. However, this disclosure is not limited to the specific details of the above embodiments. Within the scope of the technical concept of this disclosure, various simple modifications can be made to the technical solutions of this disclosure, and these simple modifications all fall within the protection scope of this disclosure.

[0075] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, this disclosure will not describe the various possible combinations separately.

[0076] Furthermore, various different embodiments of this disclosure can be combined in any way, as long as they do not violate the spirit of this disclosure, they should also be regarded as the content disclosed in this disclosure.

Claims

1. A hydrogenation catalyst for feedstocks rich in bicyclic aromatic hydrocarbons, characterized in that, The hydrogenation catalyst comprises a support and an active metal component supported on the support; the active metal component comprises Group VIII and Group VIB metal elements; the support comprises an acidic component and a heat-resistant inorganic oxide matrix, wherein the acidic component is a molecular sieve with an I value of 1-100 and an N value of 0.6-100, and the N value of the acidic component is greater than 0.6 and the I value is greater than 1; the acidic component is an ITQ-52 molecular sieve; and the pore volume of the acidic component is 0.4-0.8 cm³. 3 / g, acid density is 0.8-2.5μmol / m 2 ; The N value of a certain molecular sieve to be tested is defined as the ratio of the adsorption amount of the molecular sieve to bicyclic aromatic hydrocarbons and their derivatives to that of a standard molecular sieve. The standard molecular sieve is a HY molecular sieve with a SiO2 to Al2O3 molar ratio of 5.4 and a cell constant of 24.60 Å. The I value of a certain molecular sieve to be tested is defined as the ratio of the square of the adsorption amount of the molecular sieve to methyl indene to the product of the adsorption amount of the molecular sieve to tetrahydronaphthalene and the adsorption amount of the molecular sieve to butylbenzene. Based on the total weight of the catalyst, and calculated as oxides, the catalyst contains 1-10% by weight of Group VIII metals and 2-40% by weight of Group VIB metals.

2. The hydrogenation catalyst according to claim 1, wherein, The acidic component has an I value of 1-10 and an N value of 0.6-10.

3. The hydrogenation catalyst according to claim 1, wherein, Based on the total weight of the carrier, the content of the acidic component is 30-90% by weight; the content of the heat-resistant inorganic oxide matrix is ​​10-70% by weight.

4. The hydrogenation catalyst according to claim 3, wherein, Based on the total weight of the carrier, the content of the acidic component is 45-80% by weight; the content of the heat-resistant inorganic oxide matrix is ​​20-55% by weight.

5. The hydrogenation catalyst according to claim 1, wherein, Based on the total weight of the catalyst, and calculated as oxides, the catalyst contains 1-6% by weight of Group VIII metals and 5-25% by weight of Group VIB metals.

6. The hydrogenation catalyst according to claim 1, wherein, The heat-resistant inorganic oxide matrix is ​​selected from at least one of alumina, silicon oxide, and silicon-alumina.

7. A method for preparing the hydrogenation catalyst according to any one of claims 1-6, characterized in that, The method includes: S1. The heat-resistant inorganic oxide matrix and molecular sieve are mixed, kneaded, and extruded to obtain an extruded strip; the extruded strip is subjected to a first drying and a first calcination to obtain a carrier; S2. The carrier is impregnated with an aqueous solution of a compound containing a Group VIII metal and a Group VIB metal to obtain an impregnated carrier; the impregnated carrier is then subjected to a second drying and activation treatment.

8. The method according to claim 7, wherein, The weight ratio of the heat-resistant inorganic oxide matrix to the molecular sieve is 1-7:9-3.

9. The method according to claim 7, wherein, In step S1, the conditions for the first drying treatment include: a drying temperature of 80-300℃ and a drying time of 1-12 hours; the conditions for the first calcination include: a calcination temperature of 350-850℃ and a calcination time of 1-12 hours. In step S2, the conditions for impregnation include: an impregnation temperature of 20-150℃ and an impregnation time of 1-6 hours; the conditions for the second drying include: a temperature of 100-300℃ and a time of 2-8 hours; and the conditions for the activation treatment include: a temperature of 250-650℃ and a time of 1-12 hours.

10. The method according to claim 7, wherein, In step S1, the conditions for the first drying treatment include: a drying temperature of 100-200℃ and a drying time of 2-8 hours; the conditions for the first calcination include: a calcination temperature of 450-650℃ and a calcination time of 2-6 hours. In step S2, the conditions for the second drying include a temperature of 100-200℃; the conditions for the activation treatment include a temperature of 300-500℃ and a time of 2-6 hours.

11. A method for hydrocracking feedstock oil rich in bicyclic aromatics, characterized in that, The method includes: contacting the feedstock oil and hydrogen with the hydrocracking catalyst according to any one of claims 1-6 and carrying out a hydrocracking reaction.

Images