Polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, method for preparing the same, and use thereof

Abstract

The application provides a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst and a preparation method and application thereof. A co-precipitation combined with impregnation method is used, a phosphate precursor of MoP is prepared through co-precipitation and calcination, Ce(NO)3 is loaded on the phosphate precursor of MoP through impregnation, and a precursor of a Ce2O3 / MoP dual-component catalyst is prepared through calcination and oxidation. Then, the precursor is reduced by hydrogen to prepare the catalyst. Finally, the hydrogenation reaction is carried out in a fixed bed reactor, that is, the temperature and pressure of the reactor are adjusted to the reaction temperature and pressure, and the hydrogenation reaction of the polycyclic aromatic hydrocarbon organic liquid is carried out. The polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, the catalyst composition of which is MoP and Ce2O3, that is, trivalent cerium oxide is loaded on MoP, does not need an additional support, has high stability, and exhibits high activity to polycyclic aromatic hydrocarbons under relatively mild conditions. In addition, the catalyst has the characteristics of low price and simple preparation method, and can replace expensive noble metals for organic liquid hydrogen storage.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of heterogeneous catalytic hydrogenation, in particular to a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst and a preparation method and application thereof. BACKGROUND

[0002] Hydrogen energy, as a clean, efficient, safe and sustainable secondary energy, can be obtained through various ways such as primary energy, secondary energy and industrial fields, and is an important medium for the third energy revolution in the direction of low carbonization, carbonization and low pollution, and is therefore regarded as the most potential clean energy in the 21st century. A complete hydrogen energy system includes upstream hydrogen source development and hydrogen production, midstream hydrogen storage and hydrogen transportation, and downstream hydrogen application. Hydrogen storage and transportation is the "link" and "bottleneck" connecting the upstream and downstream of hydrogen energy. Common hydrogen storage technologies mainly include pressurized gaseous hydrogen storage, cryogenic liquefied hydrogen storage, metal alloy hydrogen storage, carbon material hydrogen storage, complex hydrogen storage, glass microsphere hydrogen storage and organic liquid hydrogen storage, etc. At present, hydrogen is mainly stored in the form of high-pressure gas, but the gaseous hydrogen storage method has the smallest hydrogen storage density and has the risk of leakage. The preparation cost of adsorbed hydrogen storage materials such as metal alloys is high and there are problems of industrialization difficulty. Organic liquid hydrogen storage technology realizes the purpose of hydrogenation and dehydrogenation by means of the reversible reaction of some olefins, alkynes or aromatic hydrocarbons and hydrogen. Compared with other hydrogen storage methods, organic liquid hydrogen storage has the following characteristics: (1) the catalytic process is reversible, the reactants and products can be recycled, and the hydrogen storage density is high; (2) hydrogen carrier storage, transportation and maintenance are safe and convenient, the storage equipment is simple, and it is especially suitable for long-distance hydrogen energy transportation in the form of organic liquid by pipeline or can solve the problem of uneven distribution of energy in different regions; (3) high hydrogen storage efficiency: for example, if the heat released during the hydrogenation of benzene can be completely recovered, the efficiency of the entire cycle process can reach 98%; (4) in principle, it can be stored and transported at normal temperature and pressure like gasoline and diesel, and it is safe.

[0003] Organic liquid hydrogen storage technology mainly realizes the storage and release of hydrogen by means of the reversible hydrogenation and dehydrogenation reaction of unsaturated organic liquids (such as toluene, naphthalene, ethyl carbazole, etc.) as hydrogen storage agents and corresponding saturated substances (such as methylcyclohexane, decalin, dodecahydroethyl carbazole, etc.) as hydrogen carriers and hydrogen. The most studied organic liquid is aromatic and nitrogen-containing heterocyclic compounds, among which polycyclic aromatic hydrocarbons are potential good hydrogen storage and release systems due to their easy availability, wide source, suitable melting and boiling point interval and high dehydrogenation conversion rate. A key to organic liquid hydrogen storage and release technology is to develop a hydrogenation / dehydrogenation catalyst with high conversion rate, high selectivity and high stability.

[0004] The main organic liquid hydrogen storage catalysts are noble metal catalysts. Although noble metals have excellent hydrogenation and dehydrogenation catalytic activity, they are expensive and have poor sulfur and nitrogen tolerance, and are easily deactivated due to hydrogenolysis and coking. In non-noble metal organic liquid hydrogenation catalysts, the most studied is Ni-based catalyst. However, Ni-based catalysts often exhibit very low activity. Therefore, the development of non-noble metal catalysts with high stability and high activity is an important problem to be solved for low-cost organic liquid hydrogen storage technology. SUMMARY

[0005] The technical problem to be solved by the present application is to provide a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, which uses a non-noble metal catalyst with low price, high stability and high activity, can catalyze the hydrogenation of polycyclic aromatic hydrocarbons at a lower temperature in a fixed bed reactor, and has high conversion rate.

[0006] The present application provides a preparation method of a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, comprising the following steps:

[0007] a1. Dissolve (NH4)6Mo7O 24 ·4H2O and (NH4)2HPO4 in deionized water in a molar ratio of Mo:P = 1:1, continuously stir to form a mixed solution, evaporate the mixed solution to dryness, dry the obtained solid, then calcine at 400-600℃ for 2-5h, and grind to obtain solid product A;

[0008] a2. Prepare a Ce(NO)3·6H2O aqueous solution according to a molar ratio of Ce to Mo in the solid product A of Ce / Mo≤0.45, and add the solid product A to the aqueous solution, immerse for 10-15h, then dry, and calcine at 400-600℃ for 2-5h to obtain a precursor B;

[0009] a3. After tabletting and crushing the precursor B, place it in the constant temperature zone of a fixed bed reactor, adjust the hydrogen pressure to 0.8-1.2MPa, the hydrogen flow rate to 100-200mL / min, heat the fixed bed reactor from room temperature to 110-130℃ at a rate of 3-5℃ / min, maintain for 1-1.5h, then heat to 300-500℃ at a rate of 8-12℃ / min, and finally heat to 600-700℃ at a rate of 1-2℃ / min, maintain for 1-3h, to obtain the catalyst.

[0010] Preferably, the concentration of (NH4)2HPO4 in the mixed solution in step a1 is 0.25g / mL.

[0011] Preferably, the concentration of the Ce(NO)3 aqueous solution in step a2 is 0.5mol / L.

[0012] Preferably, the drying temperature in the step a1 and step a2 is 120℃, and the drying time is 12h.

[0013] The application further discloses a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, which comprises two components of Ce2O3 and MoP, wherein the Ce2O3 is loaded on the MoP, the molar ratio of Mo / P is 1, and the molar ratio of Ce / Mo is not higher than 0.45.

[0014] The application further discloses an application of the polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, which is applied to a hydrogenation reaction of a polycyclic aromatic hydrocarbon organic liquid.

[0015] b1. placing the hydrogenation catalyst in a constant temperature zone of a fixed bed reactor, adjusting the reaction temperature of the fixed bed reactor to 100-240℃, and adjusting the reaction pressure to 1.0-10.0 MPa;

[0016] b2. according to the volume ratio of hydrogen:polycyclic aromatic hydrocarbon organic liquid=(100-1000):1, introducing the polycyclic aromatic hydrocarbon organic liquid into the fixed bed reactor to perform the hydrogenation reaction.

[0017] Preferably, the liquid hourly space velocity of the polycyclic aromatic hydrocarbon organic liquid in the step b2 is 0.5-150h -1 .

[0018] The working principle of the application is as follows: the preparation method of the polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst of the application adopts a co-precipitation combined with impregnation method to prepare a catalyst precursor, and then adopts a hydrogen atmosphere programmed reduction method to reduce the precursor into a catalyst. The co-precipitation combined with impregnation method is as follows: first, a phosphate precursor of MoP is prepared through co-precipitation and calcination, then Ce(NO)3 is loaded on the phosphate precursor of MoP through impregnation, and then a Ce2O3 / MoP two-component catalyst precursor is prepared through calcination and oxidation. The catalyst is prepared through reduction, that is, the catalyst precursor is reduced into a catalyst through a hydrogen atmosphere programmed reduction method in a fixed bed reactor. Then, the hydrogenation reaction is performed in the fixed bed reactor, that is, the reactor temperature is adjusted to the reaction temperature and pressure, and the hydrogenation reaction of the polycyclic aromatic hydrocarbon organic liquid is performed. The hydrogenation reaction conditions are as follows: the temperature is 100-240℃, the pressure is 1.0-10.0 MPa, the volume ratio of hydrogen to polycyclic aromatic hydrocarbon organic liquid is 100-1000, and the liquid hourly space velocity is 0.5-150h -1 . The polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst is composed of Ce2O3 and MoP, wherein the Ce2O3 is loaded on the MoP, the molar ratio of Mo / P is 1, and the molar ratio of Ce / Mo is not higher than 0.45.

[0019] The polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst provided by the application has the advantages that the catalyst composition is MoP and Ce2O3, that is, trivalent cerium oxide is loaded on MoP, no additional support is needed, the stability is high, and the catalyst shows high activity to polycyclic aromatic hydrocarbons under relatively mild conditions. In addition, the catalyst has the characteristics of low price and simple preparation method, and can replace expensive noble metals for organic liquid hydrogen storage. BRIEF DESCRIPTION OF DRAWINGS

[0020] Figure 1 is a XRD spectrum of the catalyst obtained from the precursor prepared in Example 1, Comparative Example 1 and Comparative Example 2 by temperature programmed reduction;

[0021] Figure 2 is an XPS spectrum in the Ce 3d binding energy range of the catalyst obtained from the precursor prepared in Example 1 by temperature programmed reduction;

[0022] Figure 3 is the conversion of 1-methylnaphthalene on MoP, Ce2O3-MoP and Ce2O3 / MoP catalysts;

[0023] Figure 4 is the conversion of 1-methylnaphthalene on Ce2O3 / MoP catalyst at different temperatures. DETAILED DESCRIPTION

[0024] In order to make the technical scheme of the application easier to understand, the technical scheme of the application is described clearly and completely in the form of specific embodiments in combination with the drawings.

[0025] I. Specific embodiments of the application

[0026] Example 1:

[0027] A. Preparation of polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst (adopting the method of co-precipitation combined with impregnation to prepare the precursor of Ce2O3 / MoP two-component catalyst):

[0028] a1. Dissolve (NH4)6Mo7O 24 ·4H2O and (NH4)2HPO4 in deionized water in a molar ratio of Mo:P = 1:1, continuously stir to form a mixed solution, the concentration of (NH4)2HPO4 in the mixed solution is 0.25 g / mL, evaporate the mixed solution to dryness after complete dissolution, dry the obtained solid at 120℃ for 12h, then calcine at 500℃ for 3h, and grind to obtain solid product A;

[0029] a2. A Ce(NO)3-6H2O aqueous solution with a concentration of 0.5 mol / L was prepared according to a molar ratio of Ce to Mo in the solid product A of Ce / Mo = 0.45, and solid product A was added to the solution, impregnated for 12 h, then dried at 120°C for 12 h, and calcined at 500°C for 3 h to obtain a precursor B, i.e., a precursor of a Ce2O3 / MoP dual-component catalyst;

[0030] a3. After tabletting and crushing, the precursor B was placed in a constant temperature zone of a fixed bed reactor, the hydrogen pressure was adjusted to 1.0 MPa, the hydrogen flow rate was 150 mL / min, the fixed bed reactor was heated from room temperature to 120°C at a rate of 4°C / min, maintained for 1 h, then heated to 400°C at a rate of 10°C / min, and finally heated to 650°C at a rate of 1°C / min, maintained for 2 h to prepare a Ce2O3 / MoP catalyst sample 1.

[0031] B. Hydrogenation of polycyclic aromatic hydrocarbon organic liquid using the hydrogenation catalyst:

[0032] b1. The reaction temperature of the fixed bed reactor was adjusted to 180°C, and the reaction pressure was adjusted to 5.0 MPa;

[0033] b2. The polycyclic aromatic hydrocarbon organic liquid was introduced into the fixed bed reactor at a volume ratio of hydrogen:polycyclic aromatic hydrocarbon organic liquid = 500:1 for hydrogenation reaction, and the liquid hourly space velocity of the polycyclic aromatic hydrocarbon organic liquid was 100 h -1 .

[0034] Example 2:

[0035] A. Preparation of polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst (precursor of Ce2O3 / MoP dual-component catalyst prepared by co-precipitation combined with impregnation):

[0036] a1. (NH4)6Mo7O 24 ·4H2O and (NH4)2HPO4 were dissolved in deionized water at a molar ratio of Mo:P = 1:1, and mixed to form a mixed solution, the concentration of (NH4)2HPO4 in the mixed solution was 0.25 g / mL, and after complete dissolution, the mixed solution was evaporated to dryness, the obtained solid was dried at 120°C for 12 h, then calcined at 400°C for 5 h, and finely ground to obtain a solid product A;

[0037] a2. A Ce(NO)3-6H2O aqueous solution with a concentration of 0.5 mol / L was prepared according to a molar ratio of Ce to Mo in the solid product A of Ce / Mo = 0.3, and solid product A was added to the solution, impregnated for 12 h, then dried at 120°C for 12 h, and calcined at 600°C for 2 h to obtain a precursor B, i.e., a precursor of a Ce2O3 / MoP dual-component catalyst;

[0038] a3. The precursor B was placed in the constant temperature zone of the fixed bed reactor after tabletting and crushing, the hydrogen pressure was adjusted to 0.8 MPa, the hydrogen flow rate was 100 mL / min, the fixed bed reactor was heated from room temperature to 110°C at a rate of 3°C / min, maintained for 1.2 h, then heated to 300°C at a rate of 8°C / min, and finally heated to 600°C at a rate of 1.5°C / min, maintained for 1 h, to obtain a Ce2O3 / MoP catalyst sample 2.

[0039] B. Hydrogenation of polycyclic aromatic organic liquid using hydrogenation catalyst:

[0040] b1. The reaction temperature of the fixed bed reactor was adjusted to 100°C, and the reaction pressure was adjusted to 3.0 MPa;

[0041] b2. The polycyclic aromatic organic liquid was introduced into the fixed bed reactor for hydrogenation reaction at a hydrogen:polycyclic aromatic organic liquid ratio of 100:1 by volume, and the liquid hourly space velocity of the polycyclic aromatic organic liquid was 50 h -1 .

[0042] Example 3:

[0043] A. Preparation of polycyclic aromatic organic liquid hydrogenation catalyst (precursor of Ce2O3 / MoP dual-component catalyst prepared by co-precipitation combined with impregnation):

[0044] a1. (NH4)6Mo7O 24 ·4H2O and (NH4)2HPO4 were dissolved in deionized water at a molar ratio of Mo:P = 1:1, and continuously stirred to form a mixed solution, the concentration of (NH4)2HPO4 in the mixed solution was 0.25 g / mL, after complete dissolution, the mixed solution was evaporated to dryness, the obtained solid was dried at 120°C for 12 h, then calcined at 600°C for 2 h, and finely ground to obtain solid product A;

[0045] a2. According to the molar ratio of Ce to Mo in solid product A Ce / Mo = 0.15, a Ce(NO)3·6H2O aqueous solution with a concentration of 0.5 mol / L was prepared, and solid product A was added to it, impregnated for 12 h, then dried at 120°C for 12 h, and finally calcined at 400°C for 5 h to obtain precursor B, i.e. the precursor of Ce2O3 / MoP dual-component catalyst;

[0046] a3. The precursor B was placed in the constant temperature zone of the fixed bed reactor after tabletting and crushing, the hydrogen pressure was adjusted to 1.0 MPa, the hydrogen flow rate was 150 mL / min, the fixed bed reactor was heated from room temperature to 120 °C at a rate of 4 °C / min, maintained for 1 h, then heated to 400 °C at a rate of 10 °C / min, finally heated to 650 °C at a rate of 1 °C / min, maintained for 2 h, to prepare the catalyst Ce2O3 / MoP sample 3.

[0047] B. Hydrogenation of polycyclic aromatic hydrocarbon organic liquid using the hydrogenation catalyst:

[0048] b1. The reaction temperature of the fixed bed reactor was adjusted to 240 °C, and the reaction pressure was adjusted to 10.0 MPa;

[0049] b2. The polycyclic aromatic hydrocarbon organic liquid was introduced into the fixed bed reactor for hydrogenation reaction at a volume ratio of hydrogen:polycyclic aromatic hydrocarbon organic liquid = 1000:1, and the liquid hourly space velocity of the polycyclic aromatic hydrocarbon organic liquid was 150 h -1 .

[0050] II. Comparative experiment:

[0051] Comparative Example 1:

[0052] A. Preparation of Comparative Sample 1 (precursor of MoP single-component catalyst prepared by coprecipitation method):

[0053] a1. (NH4)6Mo7O 24 ·4H2O and (NH4)2HPO4 were dissolved in deionized water at a molar ratio of Mo:P = 1:1, and stirred constantly to form a mixed solution, the concentration of (NH4)2HPO4 in the mixed solution was 0.25 g / mL, after complete dissolution, the mixed solution was evaporated to dryness, the obtained solid was dried at 120 °C for 12 h, then calcined at 500 °C for 3 h, and finely ground to obtain a solid product, which was the precursor of the MoP single-component catalyst;

[0054] a2. The precursor B was placed in the constant temperature zone of the fixed bed reactor after tabletting and crushing, the hydrogen pressure was adjusted to 1.0 MPa, the hydrogen flow rate was 150 mL / min, the fixed bed reactor was heated from room temperature to 120 °C at a rate of 4 °C / min, maintained for 1 h, then heated to 400 °C at a rate of 10 °C / min, finally heated to 650 °C at a rate of 1 °C / min, maintained for 2 h, to prepare the MoP catalyst, i.e. Comparative Sample 1.

[0055] B. Hydrogenation of polycyclic aromatic hydrocarbon organic liquid using the hydrogenation catalyst:

[0056] The operation steps of hydrogenation in this comparative example are the same as those in Specific Example 1.

[0057] Comparative Example 2:

[0058] A. Preparation of Comparative Sample 2 (precursor of Ce2O3-MoP dual-component catalyst prepared by coprecipitation method):

[0059] a1. (NH4)6Mo7O24H2O, (NH4)2HPO4 and Ce(NO)3-6H2O were dissolved in deionized water in a molar ratio of Mo:P:Ce = 1:1:0.45, and mixed to form a mixed solution under constant stirring. The concentration of (NH4)2HPO4 in the mixed solution was 0.25 g / mL. After complete dissolution, the mixed solution was evaporated to dryness. The obtained solid was dried at 120°C for 12 h, then calcined at 500°C for 3 h, and finely ground to obtain a solid product, which was the precursor of Ce2O3-MoP dual-component catalyst; 24

[0060] a2. The Ce2O3-MoP precursor was placed in the constant temperature zone of a fixed bed reactor after tabletting and crushing. The hydrogen pressure was adjusted to 1.0 MPa, and the hydrogen flow rate was 150 mL / min. The fixed bed reactor was heated from room temperature to 120°C at a rate of 4°C / min, maintained for 1 h, then heated to 400°C at a rate of 10°C / min, and finally heated to 650°C at a rate of 1°C / min, maintained for 2 h, to obtain the Ce2O3-MoP catalyst, which was Comparative Sample 2.

[0061] B. Hydrogenation of polycyclic aromatic organic liquid using hydrogenation catalyst:

[0062] The operation steps of hydrogenation in this comparative example were the same as in Specific Example 1.

[0063] III. Performance detection and analysis:

[0064] Figure 1 XRD patterns of Catalyst Sample 1 (Ce2O3 / MoP catalyst), Comparative Sample 1 (MoP catalyst) and Comparative Sample 2 (Ce2O3-MoP catalyst). In the XRD patterns of the three catalysts, only diffraction peaks attributed to MoP (PDF 65-6024) were observed. It can be seen that the three phosphate precursors were all converted to MoP phase after programmed temperature reduction.

[0065] Figure 2 XPS spectrum of Ce2O3 / MoP catalyst in the range of Ce 3d binding energy, two peaks were detected at binding energies of 903.4 and 885.2 eV, respectively, indicating that cerium oxide existed in the form of Ce2O3 (Surf. Interface Anal. 2008, 40, 264).

[0066] Figure 3 ​Conversion of 1-methylnaphthalene over MoP, Ce2O3-MoP and Ce2O3 / MoP catalysts. The conversion of 1-methylnaphthalene over MoP and Ce2O3-MoP catalysts is less than 5% at 200°C. The conversion of 1-methylnaphthalene over Ce2O3 / MoP catalyst is significantly higher than that over MoP and Ce2O3-MoP catalysts. Figure 3 As can be seen, the conversion of 1-methylnaphthalene over MoP and Ce2O3-MoP catalysts is less than 5% at 200°C. The conversion of 1-methylnaphthalene over Ce2O3 / MoP catalyst is significantly higher than that over MoP and Ce2O3-MoP catalysts.

[0067] Figure 4 Conversion of 1-methylnaphthalene over Ce2O3 / MoP catalyst at different temperatures. As can be seen, the conversion of 1-methylnaphthalene decreases significantly with the increase of temperature when the temperature is higher than 240°C. This is because the hydrogenation of polycyclic aromatic hydrocarbons is an exothermic reaction, and the reverse reaction, i.e. dehydrogenation reaction, will be facilitated at the teaching temperature. Therefore, for the hydrogenation of 1-methylnaphthalene and other polycyclic aromatic hydrocarbons, the reaction temperature should not be too high.

[0068] It should be noted that the embodiments described herein are only part of the embodiments of the present application, not all the implementation manners of the present application, and the embodiments are only exemplary, and the role is only to provide a more intuitive and clear way to understand the content of the present application, and is not a limitation on the technical solutions of the present application. Without departing from the concept of the present application, all other embodiments that can be thought of by those of ordinary skill in the art without creative labor, and other simple replacements and various changes of the technical solutions of the present application, all belong to the protection scope of the present application.

Claims

1. A process for the preparation of a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst, characterized in that, The method comprises the following steps: a1. (NH4)6Mo7O 24 • 4H2O and (NH4)2HPO4are dissolved in deionized water, and the mixture is stirred constantly to form a mixed solution. The mixed solution is evaporated to dryness, and the obtained solid is dried and then calcined at 400-600°C for 2-5h, and ground to obtain a solid product A; a2. According to the molar ratio of Ce to Mo in the solid product A, 0.15≤Ce / Mo≤0.45, an aqueous solution of Ce(NO3)3·6H2O is prepared, and the solid product A is added to the solution, impregnated for 10-15 h, then dried, and then calcined at 400-600 ℃ for 2-5 h to obtain a precursor B; a3. After the precursor B is pressed and crushed, it is placed in a constant temperature zone of a fixed bed reactor, the hydrogen pressure is adjusted to 0.8-1.2 MPa, the hydrogen flow rate is adjusted to 100-200 mL / min, the fixed bed reactor is heated from room temperature to 110-130 ℃ at a rate of 3-5 ℃ / min, maintained for 1-1.5 h, then heated to 300-500 ℃ at a rate of 8-12 ℃ / min, and finally heated to 600-700 ℃ at a rate of 1-2 ℃ / min, maintained for 1-3 h to obtain a catalyst.

2. The process for preparing a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to claim 1, characterized by, The concentration of (NH4)2HPO4 in the mixed solution in step a1 is 0.25 g / mL.

3. The process for preparing a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to claim 1, characterized by, The concentration of the aqueous solution of Ce(NO3)3·6H2O in step a2 is 0.5 mol / L.

4. The process for preparing a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to claim 1, characterized by, The drying temperature in steps a1 and a2 is 120 ℃, and the drying time is 12 h.

5. A polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst characterized by, The hydrogenation catalyst is prepared according to the method for preparing the polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to any one of claims 1-4, and comprises two components of Ce2O3 and MoP, wherein the Ce2O3 is loaded on the MoP, the molar ratio of Mo / P is 1, and the molar ratio of Ce / Mo is 0.15≤Ce / Mo≤0.

45.

6. Use of a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst as claimed in claim 5, characterized in that, The polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to claim 5 is applied to a hydrogenation reaction of a polycyclic aromatic hydrocarbon organic liquid, and the hydrogenation reaction is carried out in a fixed bed reactor, and the specific steps are as follows: b1. The hydrogenation catalyst is placed in a constant temperature zone of a fixed bed reactor, and the reaction temperature of the fixed bed reactor is adjusted to 100-240 ℃, and the reaction pressure is adjusted to 1.0-10.0 MPa; b2. According to the volume ratio of hydrogen:polycyclic aromatic hydrocarbon organic liquid=(100-1000):1, the polycyclic aromatic hydrocarbon organic liquid is introduced into the fixed bed reactor for hydrogenation reaction.

7. The use of a polycyclic aromatic hydrocarbon organic liquid hydrogenation catalyst according to claim 6, wherein The liquid hourly space velocity of the polycyclic aromatic hydrocarbon organic liquid in step b2 is from 0.5 to 150 h -1 .

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