A hydrogenation catalyst for polycyclic aromatic hydrocarbons, its preparation method and application

Abstract

This invention discloses a hydrogenation catalyst for polycyclic aromatic hydrocarbons (PAHs), its preparation method, and its applications. The PAH hydrogenation catalyst comprises: a) a porous metal oxide support, and b) at least one metal element selected from Group VIII; the molar ratio of metal atoms to oxygen atoms in the catalyst support is at least 0.5% lower than the stoichiometric ratio. The catalyst provided by this invention exhibits high conversion and selectivity in the PAH hydrogenation reaction, with minimal loss of monocyclic aromatic hydrocarbons.

Description

Technical Field

[0001] This invention relates to the field of hydrogenation of polycyclic aromatic hydrocarbons, and more specifically to a hydrogenation catalyst for polycyclic aromatic hydrocarbons, its preparation method, and its application. Background Technology

[0002] Polycyclic aromatic hydrocarbons (PAHs) refer to a class of hydrocarbons including naphthalene-based bicyclic aromatics and anthracene- and phenanthrene-based tricyclic aromatics. A portion of PAHs originates from coal tar, a byproduct of coal coking, typically containing 10 wt% naphthalene. The 200–250°C fraction obtained during coal tar distillation is called the naphthalene oil fraction, containing approximately 50 wt% naphthalene. Another portion of PAHs comes from the heavy aromatic fractions (boiling range 205–360°C) obtained from processes such as catalytic reforming, catalytic cracking, and hydrocarbon pyrolysis, with methylnaphthalene contents (mass %) of approximately 55%, 35%, and 45%, respectively. With the increasing depth of petroleum refining and stricter environmental standards for vehicle fuels, the utilization of low-quality hydrocarbons rich in PAHs is attracting growing attention.

[0003] Currently, the utilization of these polycyclic aromatic hydrocarbons (PAHs) is limited to their use as blending components in fuels or direct combustion in chemical plants. However, this approach not only wastes petroleum resources but also easily leads to serious environmental problems. In recent years, converting these PAHs into high-value-added products has become an important utilization pathway, especially the conversion of these PAHs into products with high market demand, such as BTX, which has attracted increasing attention. Hydrocracking is an important route for converting PAHs into BTX. The key control target for the catalysts used in this type of reaction is to selectively hydrogenate PAHs to monocyclic aromatic hydrocarbons, rather than excessively hydrogenating them to cycloalkanes, which directly affects the yield of BTX products.

[0004] CN109529926A discloses a catalyst for the hydrocracking of naphthalene to produce light aromatics, with Ni and W as active components and Hβ / Al-SBA-15 composite molecular sieve as support. The catalyst exhibits good naphthalene hydrocracking performance and long lifespan.

[0005] CN112536040A discloses a method for preparing a hydrogenation catalyst for polycyclic aromatic hydrocarbons. By forming a relatively stable foliated silicate phase, the active metal is embedded in the catalyst bulk phase as a bulk component, thus preventing the agglomeration of the active metal during the reaction process.

[0006] In summary, current research on hydrogenation catalysts for polycyclic aromatic hydrocarbons focuses primarily on their conversion rate and stability, with relatively few publications addressing highly selective hydrogenation catalysts for polycyclic aromatic hydrocarbons. Summary of the Invention

[0007] To address the problems of low selectivity and easy loss of monocyclic aromatic hydrocarbons in the hydrogenation reaction of polycyclic aromatic hydrocarbons in existing technologies, this invention provides a new catalyst for the hydrogenation of polycyclic aromatic hydrocarbons, its preparation method, and its application. This catalyst has the characteristics of high conversion and selectivity in the hydrogenation reaction of polycyclic aromatic hydrocarbons, and the monocyclic aromatic hydrocarbons are not easily lost.

[0008] To solve the above-mentioned technical problems, the first aspect of the present invention provides a hydrogenation catalyst for polycyclic aromatic hydrocarbons, comprising:

[0009] a) Porous metal oxide carrier

[0010] b) At least one metallic element selected from Group VIII;

[0011] The molar ratio of metal atoms to oxygen atoms in the catalyst support is at least 0.5% lower than the stoichiometric ratio.

[0012] Furthermore, the molar ratio of metal atoms to oxygen atoms in the catalyst support is more than 1.5% lower than the stoichiometric ratio, and more preferably 2.0% to 15%. Herein, the stoichiometric ratio refers to the ratio of metal atoms to oxygen atoms in the inherent chemical formula of the metal oxide.

[0013] Furthermore, the porous metal oxide support in the catalyst is treated with an inert atmosphere.

[0014] Furthermore, the porous metal oxide support is selected from at least one of alumina, titanium oxide, zinc oxide, zirconium oxide, and cerium oxide, wherein the stoichiometric ratio is the ratio of metal atoms to oxygen atoms in the metal oxide, such as the stoichiometric ratio of Ti to O in TiO2 being 1:2, the stoichiometric ratio of Ce to O in CeO2 being 1:2, the stoichiometric ratio of Zr to O in ZrO2 being 1:2, the stoichiometric ratio of Zn to O in ZnO being 1:1, and the stoichiometric ratio of Al to O in Al2O3 being 2:3.

[0015] Furthermore, in the catalyst, the proportion of group VIII metal clusters with a particle size of 0.1-2 nm is more than 80%.

[0016] Furthermore, the Group VIII metal is selected from at least one of Pt, Pd, and Ir. The content of the supported Group VIII metal, by weight fraction, is 0.01%-5% of the total weight of the catalyst.

[0017] Furthermore, the inert atmosphere is selected from at least one of N2, Ar, and He, preferably Ar.

[0018] Furthermore, the inert atmosphere treatment conditions are: calcination at a temperature of 300-700℃ for 1-10 hours, preferably 2-6 hours.

[0019] Furthermore, the form in which the group VIII metal exists in the catalyst is not limited; it can be an oxide or a metallic element.

[0020] A second aspect of the present invention provides a method for preparing the above-mentioned hydrogenation catalyst for polycyclic aromatic hydrocarbons, comprising:

[0021] (1) The porous metal oxide support was treated under an inert atmosphere to prepare support I;

[0022] (2) Prepare a metal salt solution containing group VIII metals, load it onto support I, and dry it to obtain the catalyst.

[0023] Further, in step (1), the inert atmosphere is selected from at least one of N2, Ar, and He, preferably Ar.

[0024] Further, in step (1), the inert atmosphere treatment conditions are: calcination at a temperature of 300-700℃ for 1-10 hours, preferably 2-6 hours.

[0025] Further, in step (1), the porous metal oxide carrier is selected from at least one of alumina, titanium oxide, zinc oxide, zirconium oxide, and cerium oxide, preferably at least one of alumina or titanium oxide.

[0026] Further, in step (2), the metal salt is selected from at least one of chloroplatinic acid, nitroplatinum ammonium, palladium chloride, palladium nitrate, iridium chloride, and chloroiridium acid.

[0027] Furthermore, in step (2), the loading method is one of impregnation, exchange, or precipitation.

[0028] Furthermore, in step (2), after loading the metal, the catalyst is dried at 50-90℃ for 2-5 hours.

[0029] A third aspect of the present invention provides the application of the described polycyclic aromatic hydrocarbon hydrogenation catalyst in the hydrogenation reaction of polycyclic aromatic hydrocarbons.

[0030] Furthermore, the reactants are toluene and polycyclic aromatic hydrocarbons, wherein the polycyclic aromatic hydrocarbon is naphthalene, and the weight percentage of naphthalene is 1%-15%.

[0031] Furthermore, before the catalyst is used in the reaction, it is first subjected to a reduction treatment under the following conditions: in a reducing atmosphere, at 200-450°C for 1-3 hours, and the reduction temperature of the reduction pretreatment is lower than the inert atmosphere treatment temperature described in step (1) of the catalyst preparation method.

[0032] Furthermore, the reaction conditions are as follows: reaction temperature 100-550℃, reaction pressure 1.0-5.0 MPa, hydrogen-to-hydrocarbon molar ratio 1-8, and feed weight hourly space velocity 0.5-20 h⁻¹. -1 .

[0033] Compared with the prior art, the present invention has the following advantages:

[0034] 1. The inventors of this invention discovered that by treating the support with an inert atmosphere, lattice oxygen is lost, introducing defects on or near the surface. The electron cloud density of atoms near these defects changes, allowing the precursor of the metal component to selectively adsorb onto these regions of changed charge density on the support surface during loading, thereby controlling the distribution of the metal component. Metal active sites are important adsorption sites in the reaction, and the charge density around them directly affects the adsorption performance of these sites for reactant molecules. Therefore, by controlling the dispersion of metal clusters on the support surface, and thus adjusting the charge density around the metal active sites, selective adsorption of monocyclic aromatic hydrocarbons and polycyclic aromatic hydrocarbons can be achieved, thereby improving the selective hydrogenation of polycyclic aromatic hydrocarbons and reducing the loss of monocyclic aromatic hydrocarbons.

[0035] 2. The preparation method provided by this invention is simple to operate, economical and feasible, and easy to apply industrially.

[0036] 3. The hydrogenation catalyst for polycyclic aromatic hydrocarbons provided by this invention is used in the hydrogenation reaction of polycyclic aromatic hydrocarbons and has the characteristics of high conversion rate and selectivity, and minimal loss of monocyclic aromatic hydrocarbons. Attached Figure Description

[0037] Figure 1 This is a scanning transmission electron microscope image of the catalyst in Example 1. Detailed Implementation

[0038] The technical solution of the present invention will be further illustrated below with reference to the embodiments, but it is not limited to the following embodiments.

[0039] In the method of this invention, the X-ray photoelectron spectroscopy (XPS) spectrometer used is a PerkinElmer PHI 5000C ESCA instrument, with an emission source of Mg Kα (hν = 1253.6 eV), an operating voltage of 14 kV, and an operating current of 20 mA. In this invention, the molar ratio of metal elements to oxygen elements in the examples and comparative examples is calculated from the peak area quantitative results after peak separation of the XPS spectra, as shown in Table 1. The stoichiometric ratio of metal elements to oxygen elements is calculated according to their chemical formulas.

[0040] In the method of this invention, scanning transmission electron microscopy (STEM) is performed on a Tecnai G2F20 S-TWIN high-resolution transmission electron microscope from FEI Corporation with a working voltage of 200kV. The particle size and proportion of metal clusters in the catalyst described in the examples are obtained by measurement and calculation using STEM results.

[0041]

Example 1

[0042] Ten grams of titanium dioxide support were dried at 120°C for 3 hours, then treated at 550°C in an Ar atmosphere for 3 hours to obtain a defective support A1. Support A1 was then impregnated with an equal volume of chloroplatinic acid and dried at 60°C for 3 hours. This yielded a metal-dispersed catalyst B1 with a platinum content of 0.25% (wt). The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 2. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, as detailed in the STEM image of the catalyst. Figure 1 .

[0043] Three grams of metal-dispersed catalyst B1 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0044]

Example 2

[0045] Three grams of metal-dispersed catalyst B1 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 90:10 (by weight). The reaction performance is shown in Table 1.

[0046]

Example 3

[0047] 10 g of alumina support was dried at 120 °C for 3 hours, then treated at 550 °C in an Ar atmosphere for 3 hours to obtain a defective support A3. An equal volume of support A3 was impregnated with chloroplatinic acid and dried at 60 °C for 3 hours. A metal-dispersed catalyst B3 with a platinum content of 0.3% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 2 / 3. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0048] Three grams of metal-dispersed catalyst B3 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0049]

Example 4

[0050] 10 g of zinc oxide support was dried at 120 °C for 3 hours, then treated at 550 °C in an Ar atmosphere for 3 hours to obtain defective support A4. Support A4 was then impregnated with an equal volume of chloroplatinic acid and dried at 60 °C for 3 hours. A metal-dispersed catalyst B4 with a platinum content of 1.5% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 1. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0051] Three grams of metal-dispersed catalyst B4 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0052]

Example 5

[0053] Ten grams of zirconia support were dried at 120°C for 3 hours, then treated at 550°C in an Ar atmosphere for 3 hours to obtain defective support A5. Support A5 was then impregnated with an equal volume of chloroplatinic acid and dried at 60°C for 3 hours. This yielded a metal-dispersed catalyst B5 with a platinum content of 0.25% (wt). The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 2. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0054] Three grams of metal-dispersed catalyst B5 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0055]

Example 6

[0056] 10 g of cerium oxide support was dried at 120 °C for 3 hours, then treated at 550 °C in an Ar atmosphere for 3 hours to obtain defective support A6. Support A6 was then impregnated with an equal volume of chloroplatinic acid and dried at 60 °C for 3 hours. This yielded a metal-dispersed catalyst B6 with a platinum content of 0.25% (wt). The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 2. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0057] Three grams of metal-dispersed catalyst B6 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0058]

Example 7

[0059] Ten grams of titanium dioxide support were dried at 120°C for 3 hours, then treated at 550°C in an Ar atmosphere for 3 hours to obtain a defective support A7. An equal volume of support A7 was impregnated with palladium chloride and dried at 60°C for 3 hours. A metal-dispersed catalyst B7 with a palladium content of 0.25% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 2. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0060] Three grams of metal-dispersed catalyst B7 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0061]

Example 8

[0062] Ten grams of titanium dioxide support were dried at 120°C for 3 hours, then treated at 550°C in an Ar atmosphere for 3 hours to obtain a defective support A8. An equal volume of support A8 was impregnated with iridium chloride and dried at 60°C for 3 hours. A metal-dispersed catalyst B8 with a palladium content of 0.25% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is 1 / 2. The proportion of metal clusters with a particle size of 0.1-2 nm in the catalyst is over 80%, and its STEM characterization results are consistent with... Figure 1 The catalyst in Example 1 is similar.

[0063] Three grams of metal-dispersed catalyst B8 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0064] Comparative Example 1

[0065] Ten grams of titanium dioxide support were impregnated with a certain volume of chloroplatinic acid solution and dried at 60°C for 3 hours. Catalyst B9 with a platinum content of 0.1% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst is basically close to the molar ratio of metal atoms to oxygen atoms in the catalyst support obtained from XPS results.

[0066] Three grams of catalyst B9 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-hydrogen molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0067] Comparative Example 2

[0068] Ten grams of titanium dioxide support were impregnated with an equal volume of palladium chloride solution and dried at 60°C for 3 hours. Catalyst B10 with a palladium content of 0.1% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is approximately close to the molar ratio of metal atoms to oxygen atoms in the catalyst obtained from XPS results.

[0069] Three grams of catalyst B10 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0MPa, the hydrogen-hydrogen molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1.

[0070] Comparative Example 3

[0071] Ten grams of titanium dioxide support were impregnated with an equal volume of iridium chloride solution and dried at 60°C for 3 hours. Catalyst B11 with an iridium content of 0.1% (wt) was obtained. The molar ratio of metal atoms to oxygen atoms in the catalyst support, obtained from XPS results, is shown in Table 1. Furthermore, the stoichiometric molar ratio of metal atoms to oxygen atoms in the catalyst support is essentially close to the molar ratio of metal atoms to oxygen atoms in the catalyst obtained from XPS results.

[0072] Three grams of catalyst B11 were placed in a reactor, and hydrogen gas was introduced for reduction at 450°C for 3 hours. The temperature was then lowered to 370°C, and hydrogen gas and a material containing toluene and naphthalene were introduced to investigate the activity. The reaction conditions are described below: total weight hourly space velocity (WHSV) of 10 h⁻¹. -1 The reaction temperature was 370℃, the reaction pressure was 3.0 MPa, the hydrogen-to-hydrocarbon molar ratio was 3.0, and the reactants were toluene:naphthalene = 95:5 (by weight). The reaction performance is shown in Table 1. The value of H2 / (H1+H2) represents the proportion of naphthalene hydrogenation in the total hydrogenation of the aromatic ring (toluene and naphthalene), used to illustrate the selectivity of fused-ring hydrogenation. When the selectivity of fused-ring hydrogenation increases, the selectivity of monocyclic hydrogenation decreases, thus indicating that monocyclic aromatic hydrocarbons are less likely to be lost.

[0073] Table 1

[0074]

[0075] The specific 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 combining the 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. An application of a hydrogenation catalyst for polycyclic aromatic hydrocarbons in the hydrogenation reaction of polycyclic aromatic hydrocarbons, wherein, The hydrogenation catalyst for polycyclic aromatic hydrocarbons comprises: a) Porous metal oxide carriers, b) At least one metallic element selected from Group VIII; The porous metal oxide support is selected from at least one of alumina, titanium oxide, zinc oxide, zirconium oxide, and cerium oxide; the group VIII metal is selected from at least one of Pt, Pd, and Ir. The molar ratio of metal atoms to oxygen atoms in the catalyst support is less than 2.0% to 15% of the stoichiometric ratio. The porous metal oxide support in the catalyst is calcined in an inert atmosphere (Ar) at a temperature of 300-550℃ for 1-10 hours. In the catalyst, the proportion of group VIII metal clusters with a particle size of 0.1-2 nm is more than 80%.

2. The application according to claim 1, characterized in that, The content of group VIII metals supported is 0.01%-5% of the total weight of the catalyst, by weight fraction.

3. The application according to claim 1 or 2, characterized in that, The preparation method of the hydrogenation catalyst for polycyclic aromatic hydrocarbons includes: (1) The porous metal oxide support was treated under an inert atmosphere to prepare support I; (2) Prepare a metal salt solution containing group VIII metals, load it onto support I, and dry it to obtain the catalyst.

4. The application according to claim 3, characterized in that, In step (1), the inert atmosphere is selected from Ar; the conditions for the inert atmosphere treatment are: calcination at a temperature of 300-550℃ for 1-10 h.

5. The application according to claim 3, characterized in that, In step (2), the metal salt is selected from at least one of chloroplatinic acid, nitroplatinum ammonium, palladium chloride, palladium nitrate, iridium chloride, and chloroiridium acid.

6. The application according to claim 3, characterized in that, In step (2), after loading the metal, the catalyst is dried at 50-90℃ for 2-5 hours.

7. The application according to claim 1, characterized in that, The reactants are toluene and polycyclic aromatic hydrocarbons.

8. The application according to claim 1, characterized in that, The reaction conditions are as follows: reaction temperature 100-550℃, reaction pressure 1.0-5.0 MPa, hydrogen-to-hydrocarbon molar ratio 1-8, and feed weight hourly space velocity 0.5-20 h⁻¹. -1 .

Images