A catalyst for the hydroconversion of cashew nut shell oil and its preparation method

Abstract

This invention provides a highly efficient catalyst for the hydroconversion of cashew nut shell oil and its preparation method. The catalyst comprises: a hydroconversion active component Pt, a catalyst support EU-1 type zeolite molecular sieve, and a catalyst modifier MO2 (M=Zr). 4+ Ti 4+ Ce 4+ The active hydrogenation component Pt, modifier MO2, and EU-1 zeolite molecular sieve were co-impregnated and dried to obtain a catalyst precursor. The precursor was then calcined to obtain the PtO2-MO2 / EU-1 catalyst. Through the unique pore structure of the EU-1 zeolite molecular sieve and the synergistic effect between different metals, the catalyst of this invention achieves highly efficient hydrogenation conversion of cashew nutshell oil and has a long service life.

Description

Technical Field

[0001] This invention belongs to the field of biomass oil hydrogenation conversion technology, specifically relating to a cashew nut shell oil hydrogenation conversion catalyst and its preparation method. Background Technology

[0002] Cashew shell oil is obtained by pressing cashew shells and is a byproduct of cashew processing. Natural cashew shell oil mainly consists of cashew phenol, cashew acid, and cardiotonic phenols, with cashew acid accounting for over 90% of the total content. During heating, the carboxyl group of cashew acid is removed, converting it into cashew phenol, and 20%-30% cashew shell resin is also generated. Further hydrogenation of cashew phenol produces pentadecylcyclohexane, an important organic chemical raw material intermediate, which can also be used as a liquid alkane fuel.

[0003] Catalytic hydrogenation is a crucial process in petrochemicals, generally referring to the addition reaction of alkenes, alkynes, and other hydrocarbons with hydrogen in the presence of a hydrogenation catalyst to produce the corresponding alkanes. Commonly used catalytic hydrogenation metals include W, Mo, Co, and Ni. Noble metals include Pt and Pd. The hydrogenation activity is closely related to the chemical characteristics of the element. A necessary condition for a hydrogenation reaction is that the reactants can be adsorbed onto the catalyst surface at a certain rate. After adsorption, weak bonds are formed between the adsorbed molecules and the catalyst surface, followed by desorption. Generally, metals suitable as catalysts should have a cubic or hexagonal crystal lattice. W, Mo, and Fe are elements that form a body-centered cubic lattice; Pt, Pd, and Ni are elements that have a face-centered cubic lattice.

[0004] Amorphous aluminum silicate, magnesium silicate, and various molecular sieves are commonly used catalyst supports in recent years, such as alumina, activated carbon, and diatomaceous earth; acidic supports include aluminum silicate and molecular sieves. In general reactions, the support itself is inactive, but it can provide a large specific surface area, allowing the active components to be well dispersed on the surface.

[0005] Studies have shown that, by comparing product selectivity and yield, noble metal catalysts can provide high catalytic efficiency and stable catalytic activity, superior to traditional transition metal catalysts. Because the d-electron orbitals of noble metals are not fully filled, their surfaces readily adsorb reactants, facilitating the formation of "active compounds." They also possess properties such as high-temperature resistance, oxidation resistance, and corrosion resistance, making them widely used in hydrogenation, deoxygenation, and isomerization reactions. Furthermore, noble metals can activate H2 and oxygen-containing groups, promoting the HDO (hydrodeoxygenation) reaction. The high electronegativity of noble metal elements allows them to easily lose electrons in chemical reactions, forming active sites. These active sites can interact with reactant molecules, promoting the chemical reaction. Simultaneously, the active components of noble metals can effectively absorb and transfer energy, lowering the activation energy of reactant molecules, thereby improving catalytic efficiency.

[0006] Compared to single-metal catalysts, multi-metal catalysts offer several advantages. Multi-metal catalysts can improve catalytic efficiency through synergistic effects between different metals. These synergies can stem from electron transfer, synergistic adsorption, and interactions between the metals, resulting in higher reaction rates and better selectivity. Combinations of different metals can effectively prevent catalyst sintering and coking, extending catalyst lifespan. By rationally selecting different metals, optimization can be performed for different reaction types and conditions, thereby achieving a wider range of selective catalytic reactions. Summary of the Invention

[0007] The purpose of this invention is to provide a method for preparing a catalyst for the hydroconversion of cashew nutshell oil. This catalyst can stably carry out the hydroconversion of cashew nutshell oil, with a feed conversion rate of over 95%, high selectivity for pentadecylcyclohexane (over 75%), and good isomerization activity in the high-temperature range, achieving a pentadecylcyclohexane isomer yield of up to 41.6%. This solves the problems of harsh reaction conditions, low catalyst activity, and poor selectivity for the target product in traditional cashew nutshell oil hydroconversion processes.

[0008] To achieve the above objectives, the present invention adopts the following technical solution:

[0009] A catalyst for the hydroconversion of cashew nutshell oil, comprising a hydroconversion active component Pt, a catalyst support of EU-1 type zeolite molecular sieve, and a catalyst modifier MO2; wherein M in the catalyst modifier MO2 is one of Zr, Ti, or Ce.

[0010] The loading of the hydrogenation active component Pt on the catalyst support EU-1 type zeolite molecular sieve is 0.1wt%~1wt%, preferably 0.3wt%~0.5wt%; the hydrogenation active component Pt is derived from one of chloroplatinic acid hexahydrate, tetraammineplatinum nitrate, and tetraammineplatinum chloride.

[0011] The catalyst modifier MO2 is loaded at a rate of 5wt% to 20wt% on the catalyst support EU-1 type zeolite molecular sieve; the catalyst modifier MO2 is derived from one of zirconium oxychloride octahydrate, zirconium nitrate, titanium tetrachloride, tetrabutyl titanate, titanium isopropoxide, cerium nitrate, and cerium acetate.

[0012] The catalyst support EU-1 type zeolite molecular sieve has a silica-alumina ratio of 20~100, preferably 30~50.

[0013] The preparation method of the above-mentioned cashew nut shell oil hydroconversion catalyst includes the following steps:

[0014] (1) Add an equal volume of deionized water to the hydrogenation active component Pt, catalyst modifier MO2 and catalyst support EU-1 type zeolite molecular sieve, place them on a magnetic stirrer and stir and soak for 12~24h at a stirring speed of 500~800r / min, and then slowly evaporate the deionized water in a constant temperature water bath at 50~80℃.

[0015] (2) The sample obtained in step (1) is dried at 80~140℃ to obtain the catalyst precursor;

[0016] (3) The catalyst precursor obtained in step (2) is calcined and then cooled to room temperature to obtain PtO2-MO2 / EU-1 catalyst; the calcination temperature is 450~600℃ and the calcination time is 3~6h.

[0017] The pore volume of the PtO2-MO2 / EU-1 catalyst is 0.14–0.20 cm³. 3 / g, with an average pore size of 1.5–2.0 nm and a specific surface area of ​​150 m². 2 / g~200m 2 / g.

[0018] Application of a PtO2-MO2 / EU-1 catalyst prepared by the above method in the hydroconversion of cashew nut shell oil.

[0019] The specific steps involve reacting the PtO2-MO2 / EU-1 catalyst in a fixed-bed tubular reactor under the following conditions: reduction time 2–5 h, reduction temperature 450–600 °C, reaction pressure 2–8 MPa, reaction temperature 200–400 °C, and a mass hourly space velocity (MSV) of 1–4 h⁻¹ for the cashew phenol feedstock. -1 The gas space velocity of hydrogen is 500-2000 h⁻¹. -1 .

[0020] The cashew phenol raw material has a mass percentage concentration of 0-40 wt%.

[0021] The beneficial effects of this invention are as follows:

[0022] (1) The catalyst support EU-1 type zeolite molecular sieve used in this invention has a one-dimensional ten-membered ring mesoporous channel and a unique side-bag structure, allowing the long-branched alkyl groups of cashew nut shell oil to penetrate deep into the channel and achieve molecular adsorption. Due to the steric hindrance effect, the phenolic groups of cashew nut shell oil are only exposed on the surface of the molecular sieve. The Pt hydrogenation component on the surface of the molecular sieve can be activated and release a large number of active H atoms, which can quickly react with the phenolic groups to convert them into cyclohexane. The modifier MO2 located on the surface of the molecular sieve can not only improve the dispersibility of Pt, but also coordinate with the hydroxyl groups of the phenolic groups through the oxygen vacancies on its surface, further activating the groups and making the hydrogenation conversion smoother. By combining the unique pore structure of EU-1 molecular sieve with the synergistic effect between different metals, the catalyst of this invention achieves efficient hydrogenation conversion of cashew nut shell oil and has a long service life.

[0023] (2) Compared with traditional and more complex chemical synthesis routes, this invention obtains the target product pentadecylcyclohexane in one step through chemical catalysis. The production process produces fewer by-products and less waste, and the target product has high selectivity and high industrial applicability. Compared with the hydrogen fluoride catalyst used in traditional synthesis routes, the MO2 / EU-1 catalyst selected in this invention is safer and more environmentally friendly.

[0024] (3) By using the supported hydrogenation active component Pt and the modified EU-1 zeolite molecular sieve catalyst, its catalytic performance can be significantly improved. The feed conversion rate can reach more than 95%, the selectivity for pentadecylcyclohexane is high (more than 75%), and it has good isomerization activity in the high temperature range. The yield of pentadecylcyclohexane isomer products can reach more than 41.6%. Attached Figure Description

[0025] Figure 1 XRD patterns of catalysts 1-5 for the hydrodeoxygenation and isomerization of cashew nut shell oil.

[0026] Figure 2 Stability test of catalyst 2 for hydrodeoxygenation and isomerization of cashew shell oil at 280℃. Detailed Implementation

[0027] To enable those skilled in the art to better understand the technical solution of the present invention, the present invention will be further described in detail below with reference to the accompanying drawings and preferred embodiments.

[0028] Example 1

[0029] (1) Place 0.0027 g H2PtCl6·6H2O, 0.13 g ZrOCl2·8H2O and 1 g EU-1 zeolite molecular sieve (SiO2 / Al2O3=20) into a beaker, add 10 g deionized water, place on a magnetic stirrer and stir for 12 h at a stirring speed of 500 r / min, then place in a constant temperature water bath and slowly evaporate the distilled water at 50 °C;

[0030] (2) The sample obtained in step (1) was placed in an oven and dried at 80°C to obtain the catalyst precursor;

[0031] (3) The catalyst precursor obtained in step (2) was calcined at 450℃ for 3h and cooled to room temperature to finally obtain a PtO2-ZrO2 / EU-1 catalyst with a Pt loading of 0.1wt% (the mass ratio of elemental Pt to support EU-1) and a ZrO2 loading of 5wt% (the mass ratio of ZrO2 to support EU-1), which is denoted as Cat.-1.

[0032] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 2 h under a hydrogen atmosphere, and the reduction activation temperature was 450 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 500 h⁻¹. -1 The reaction pressure was 2 MPa, the raw material was cashew phenol (10% by mass, solvent was decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 1 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0033] Example 2

[0034] (1) Place 0.008 g H2PtCl6·6H2O, 0.26 g ZrOCl2·8H2O and 1 g EU-1 zeolite molecular sieve (SiO2 / Al2O3=30) into a beaker, add 10 g deionized water, place it on a magnetic stirrer and stir for 16 h at a stirring speed of 600 r / min, and then place it in a constant temperature water bath and slowly evaporate it at 60 °C.

[0035] (2) The sample obtained in step (1) was placed in an oven and dried at 100°C to obtain the catalyst precursor;

[0036] (3) The catalyst precursor obtained in step (2) was calcined at 500℃ for 4h and cooled to room temperature to finally obtain a PtO2-ZrO2 / EU-1 catalyst with a Pt loading of 0.3wt% and a ZrO2 loading of 10wt%, which was denoted as Cat.-2.

[0037] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 3 h under a hydrogen atmosphere, and the reduction activation temperature was 500 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 1000 h⁻¹. -1 The reaction pressure was 4 MPa, the raw material was cashew phenol (20% by mass, solvent: decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 2 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0038] Example 3

[0039] (1) Place 0.013g H2PtCl6·6H2O, 0.24g TiCl4 and 1g EU-1 zeolite molecular sieve (SiO2 / Al2O3=50) into a beaker, add 10g of deionized water, place it on a magnetic stirrer and stir for 20h at a stirring speed of 700r / min, and then place it in a constant temperature water bath and slowly evaporate it at 70℃;

[0040] (2) The sample obtained in step (1) was placed in an oven and dried at 120°C to obtain the catalyst precursor;

[0041] (3) The catalyst precursor obtained in step (2) was calcined at 550°C for 5 hours and cooled to room temperature to finally obtain a PtO2-TiO2 / EU-1 catalyst with a Pt loading of 0.5 wt% and a TiO2 loading of 10 wt%, which was denoted as Cat.-3.

[0042] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out under a hydrogen atmosphere for 4 h, and the reduction activation temperature was 550 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere, with a gas hourly space velocity (HSV) of 1500 h⁻¹. -1 The reaction pressure was 6 MPa, the raw material was cashew phenol (30% by mass, solvent was decahydronaphthalene), and the mass hourly space velocity (H₂S) of the liquid phase was 3 h₀. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0043] Example 4

[0044] (1) Place 0.027g H2PtCl6·6H2O, 0.26g Ce(NO3)3·6H2O and 1g EU-1 zeolite molecular sieve (SiO2 / Al2O3=100) into a beaker, add 10g of deionized water, place it on a magnetic stirrer and stir for 24h at a stirring speed of 800r / min, and then place it in a constant temperature water bath and slowly evaporate it at 80℃;

[0045] (2) The sample obtained in step (1) was placed in an oven and dried at 140°C to obtain the catalyst precursor;

[0046] (3) The catalyst precursor obtained in step (2) was calcined at 600℃ for 6h and cooled to room temperature to finally obtain a PtO2-CeO2 / EU-1 catalyst with a Pt loading of 1wt% and a CeO2 loading of 10wt%, which is denoted as Cat.-4.

[0047] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 5 h in a hydrogen atmosphere, and the reduction activation temperature was 600 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 2000 h⁻¹. -1 The reaction pressure was 8 MPa, the raw material was cashew phenol (40% by mass, solvent was decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 4 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0048] Comparative Example 1

[0049] (1) Place 0.008 g H2PtCl6·6H2O and 1 g EU-1 zeolite molecular sieve (SiO2 / Al2O3=30) into a beaker, add 10 g of deionized water, place it on a magnetic stirrer and stir for 16 h at a stirring speed of 600 r / min, and then place it in a constant temperature water bath and slowly evaporate it at 60 °C.

[0050] (2) The sample obtained in step (1) was placed in an oven and dried at 100°C to obtain the catalyst precursor;

[0051] (3) The catalyst precursor obtained in step (2) was calcined at 500°C for 4 hours and cooled to room temperature to finally obtain a PtO2 / EU-1 catalyst with a Pt loading of 0.3wt%, which is denoted as Cat.-5.

[0052] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 3 h under a hydrogen atmosphere, and the reduction activation temperature was 500 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 1000 h⁻¹. -1 The reaction pressure was 4 MPa, the raw material was cashew phenol (20% by mass, solvent: decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 2 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0053] Comparative Example 2

[0054] (1) Place 0.008 g H2PtCl6·6H2O, 0.26 g ZrOCl2·8H2O and 1 g USY zeolite molecular sieve (SiO2 / Al2O3=5) into a beaker, add 10 g of deionized water, place it on a magnetic stirrer and stir for 16 h at a stirring speed of 600 r / min, and then place it in a constant temperature water bath and slowly evaporate it at 60 °C.

[0055] (2) The sample obtained in step (1) was placed in an oven and dried at 100°C to obtain the catalyst precursor;

[0056] (3) The catalyst precursor obtained in step (2) was calcined at 500°C for 4 hours and cooled to room temperature to finally obtain a PtO2-ZrO2 / USY catalyst with a Pt loading of 0.3wt% and a ZrO2 loading of 10wt%, which was denoted as Cat.-6.

[0057] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 3 h under a hydrogen atmosphere, and the reduction activation temperature was 500 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 1000 h⁻¹. -1 The reaction pressure was 4 MPa, the raw material was cashew phenol (20% by mass, solvent: decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 2 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0058] Comparative Example 3

[0059] (1) Place 0.008 g H2PtCl6·6H2O, 0.26 g ZrOCl2·8H2O and 1 g Al2O3 into a beaker, add 10 g of deionized water, place it on a magnetic stirrer and stir for 16 h at a stirring speed of 600 r / min, and then place it in a constant temperature water bath and slowly evaporate it at 60 °C.

[0060] (2) The sample obtained in step (1) was placed in an oven and dried at 100°C to obtain the catalyst precursor;

[0061] (3) The catalyst precursor obtained in step (2) was calcined at 500°C for 4 hours and cooled to room temperature to finally obtain a PtO2-ZrO2 / Al2O3 catalyst with a Pt loading of 0.3wt% and a ZrO2 loading of 10wt%, which was denoted as Cat.-7.

[0062] The hydrogenation performance of the catalyst was evaluated in a stainless steel fixed-bed tubular reactor with an inner diameter of 10 mm and a length of 400 mm. The catalyst loading was 1.2 g. After fixed-bed packing, reduction was carried out for 3 h under a hydrogen atmosphere, and the reduction activation temperature was 500 °C. The temperature in the isothermal zone in the middle of the reactor was 553 K during the reaction, under a hydrogen atmosphere and a gas hourly space velocity (VHSV) of 1000 h⁻¹. -1 The reaction pressure was 4 MPa, the raw material was cashew phenol (20% by mass, solvent: decahydronaphthalene), and the mass hourly space velocity (HHSV) of the liquid phase was 2 h⁻¹. -1 The liquid phase products were analyzed by GC-MS, and the results were calculated using the area normalization method. The test results are shown in Table 1.

[0063] Table 1. Texture parameters and activity test results at 280°C for the catalysts of the examples and comparative examples.

[0064]

[0065] The results show that the zeolite molecular sieve catalyst EU-1, based on the hydrogenation active component Pt prepared in Example 2 of this invention and modified with a modifier, exhibits significantly higher cashew nut shell oil conversion and pentadecylcyclohexane selectivity at a reaction temperature of 280℃ compared to the catalyst in the comparative example. The increased oxygen vacancies through modification enhance the catalyst's adsorption and activation capacity for oxygen atoms, facilitating oxygen atom removal. Furthermore, the introduction of the noble metal Pt significantly enhances the catalyst's hydrogenation activity. Due to the unique pore structure of the EU-1 molecular sieve, compared to USY and Al2O3 (Comparative Examples 2 and 3), the long-branched alkyl groups of cashew nut shell oil can penetrate deeper into its pores, achieving molecular adsorption. This facilitates the hydrogenation reaction of phenolic groups by the hydrogenation active component Pt on the molecular sieve surface, resulting in a significant improvement in cashew nut shell oil conversion and target product selectivity. Therefore, the catalyst described in this invention for the hydrogenation conversion of cashew nut shell oil exhibits superior activity compared to the catalyst in the comparative example and shows promising prospects for industrial application.

[0066] To further investigate the heterogeneous activity of the catalysts prepared in this invention, the catalysts in the examples and comparative examples were tested at 380°C in the above-mentioned stainless steel fixed-bed tubular reactor. The test results are shown in Table 2.

[0067] Table 2. Results of isomerization activity tests of catalysts in the examples and comparative examples at 380°C.

[0068]

[0069] As shown in Tables 1 and 2, the conversion rates of cashew phenol in both the examples and the comparative example increased with increasing temperature. The yield of the pentadecylcyclohexane isomer in the examples was significantly higher than that in the comparative example. Therefore, the catalyst prepared by this invention has good isomerization activity, and its isomerization ability is mainly enhanced in the low-temperature range (260℃-320℃) and at higher temperatures (320℃-400℃).

[0070] Figure 1 The XRD pattern of the catalyst in this embodiment of the invention shows that the main characteristic peaks of EU-1 are located around 7.93°, 8.75°, 19.08°, 20.54°, 22.19°, 23.32°, 23.98°, 26.01°, 26.58°, and 27.27°, which is basically consistent with relevant literature reports. Furthermore, there are no obvious characteristic peaks of supported metal ions, indicating that it is well dispersed on the support. Figure 2It can be seen that the catalyst Cat.-2 of this patent invention can maintain good catalytic activity for a relatively long time (280℃), the conversion rate of cashew phenol is maintained above 95%, and the selectivity of pentadecylcyclohexane is basically maintained above 85%. This data well illustrates that the catalyst of this patent has good hydrogenation reaction activity and stability.

[0071] The above description is only a preferred embodiment of the present invention. All equivalent changes and modifications made within the scope of the claims of the present invention should be included in the scope of the present invention.

Claims

1. The application of a PtO2-MO2 / EU-1 catalyst in the hydroconversion of cashew nut shell oil, characterized in that: The PtO2-MO2 / EU-1 catalyst comprises a hydrogenation active component Pt, a catalyst support EU-1 type zeolite molecular sieve, and a catalyst modifier MO2; M in the catalyst modifier MO2 is one of Zr, Ti, and Ce; the average pore size of the PtO2-MO2 / EU-1 catalyst is 1.5 to 2.0 nm.

2. The application according to claim 1, characterized in that: The loading of the hydrogenation active component Pt on the catalyst support EU-1 type zeolite molecular sieve is 0.1wt%~1wt%; the hydrogenation active component Pt is derived from one of chloroplatinic acid hexahydrate, tetraammineplatinum nitrate, and tetraammineplatinum chloride.

3. The application according to claim 1, characterized in that: The catalyst modifier MO2 is loaded at a rate of 5wt% to 20wt% on the catalyst support EU-1 type zeolite molecular sieve; the catalyst modifier MO2 is derived from one of zirconium oxychloride octahydrate, zirconium nitrate, titanium tetrachloride, tetrabutyl titanate, titanium isopropoxide, cerium nitrate, and cerium acetate.

4. The application according to claim 1, characterized in that: The silica-alumina ratio of the catalyst support EU-1 type zeolite molecular sieve is 20~100.

5. The application according to claim 1, characterized in that: The preparation method of the PtO2-MO2 / EU-1 catalyst includes the following steps: (1) Add deionized water to the hydrogenation active component Pt, catalyst modifier MO2 and catalyst support EU-1 type zeolite molecular sieve, place it on a magnetic stirrer and stir and soak for 12~24h at a stirring speed of 500~800r / min, and then slowly evaporate the deionized water in a constant temperature water bath at 50~80℃. (2) The sample obtained in step (1) is dried at 80~140℃ to obtain the catalyst precursor; (3) The catalyst precursor obtained in step (2) is calcined and then cooled to room temperature to obtain PtO2-MO2 / EU-1 catalyst; the calcination temperature is 450~600℃ and the calcination time is 3~6h.

6. The application according to claim 1, characterized in that: The pore volume of the PtO2-MO2 / EU-1 catalyst is 0.14–0.20 cm³. 3 / g, specific surface area 150m² 2 / g~200m 2 / g.

7. The application according to claim 1, characterized in that: The PtO2-MO2 / EU-1 catalyst was reacted in a fixed-bed tubular reactor under the following conditions: reduction time 2–5 h, reduction temperature 450–600 °C, reaction pressure 2–8 MPa, reaction temperature 200–400 °C, and a mass hourly space velocity (MSV) of 1–4 h⁻¹ for the cashew phenol feedstock. -1 The gas space velocity of hydrogen is 500-2000 h⁻¹. -1 .

8. The application according to claim 7, characterized in that: The cashew phenol raw material has a mass percentage concentration of 0-40 wt%.

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