Process for the preparation of a catalyst for the hydrogenation of epoxy tetralin to beta-phenethyl alcohol and its use

Abstract

The present application relates to a catalyst for preparing beta-phenethyl alcohol by hydrogenation of styrene, in particular to a preparation method and application of a catalyst for preparing beta-phenethyl alcohol by hydrogenation of epoxyphenyl ethane, comprising the following steps: preparing a solution of nickel acetate, ammonium molybdate, ZrOCl2.8H2O and niobium oxalate; adding a titanium-aluminum oxide carrier into the solution, stirring, and impregnating; adding potassium hydroxide to generate a precipitate, washing with deionized water, drying, and calcining to obtain the catalyst product; the titanium-aluminum oxide carrier is prepared by stirring tetrabutyl titanate, triethylamine, mesoporous aluminum oxide and low-carbon alcohol, suction filtering, air-drying at room temperature, and calcining in an air atmosphere; the application of the catalyst mixes epoxyphenyl ethane, solvent, hydrogen and hydrogen dissolving agent through a fixed bed reactor containing the catalyst, adjusts the reaction conditions of the fixed bed reactor, makes the epoxyphenyl ethane completely react, generates beta-phenethyl alcohol, has high reaction conversion rate, good reaction selectivity, low energy consumption, and saves device investment.

Description

Technical Field

[0001] This invention relates to catalysts for the hydrogenation of styrene to β-phenylethanol, and more specifically to a method for preparing catalysts for the hydrogenation of epoxide to β-phenylethanol and their applications. Background Technology

[0002] β-Phenylacetyl alcohol is a colorless, transparent liquid at room temperature with a soft, delicate, and pleasant rose scent. Its pure aroma makes it an important fragrance and fine chemical intermediate. Due to its unique physical and chemical properties, it is widely used in the pharmaceutical, fragrance, cosmetic, and food industries. β-Phenylacetyl alcohol is also a key raw material for the antipyretic and analgesic drug ibuprofen.

[0003] Currently, the main methods for synthesizing β-phenylethanol are as follows: one is the preparation method using benzene and ethylene oxide as raw materials in the presence of a catalyst; the other is the chlorination process using toluene as raw material. These two processes are the classic methods for industrial production of β-phenylethanol.

[0004] However, existing technologies suffer from problems such as severe pollution, high energy consumption, low conversion rate, and poor reaction selectivity to varying degrees. Summary of the Invention

[0005] To address the aforementioned problems, this invention proposes a method for preparing a catalyst for the hydrogenation of epoxide to β-phenylethanol, comprising the following steps:

[0006] (1) Prepare a solution by mixing nickel acetate, ammonium molybdate, ZrOCl2·8H2O and niobium oxalate;

[0007] (2) Add titanium aluminum oxide carrier to the solution, stir, and impregnate;

[0008] (3) Add potassium hydroxide to the solution to form a precipitate, then wash with water, dry, and calcine to obtain the catalyst product;

[0009] The titanium aluminate carrier is prepared by stirring tetrabutyl titanate, triethylamine, mesoporous alumina, and low carbon alcohol for 16-24 hours, filtering, air drying at room temperature, and calcining in an air atmosphere.

[0010] The main active component in the catalyst is Ni. 2+ Mo 6+ Zr 4+ 、Nb 5+ The active ingredient is Al. 3+ Ti 4+ .

[0011] The soaking time in step (2) is 12 hours or more.

[0012] Based on tetrabutyl titanate, the molar ratio of tetrabutyl titanate, triethylamine, mesoporous alumina, and low-carbon alcohol is 1:4-6:11-17:130-200.

[0013] Furthermore, the calcination temperature is 450–600°C, and the time is 2–6 hours; the calcination temperature in the air atmosphere is 520–620°C, and the time is 3–6 hours.

[0014] Furthermore, the mesoporous alumina is prepared by dissolving lauric acid and aluminum sec-butoxide separately in sec-butanol, then adding the sec-butanol solution containing lauric acid dropwise to the solution containing aluminum sec-butoxide, stirring, adding water dropwise, filtering and washing with water until neutral after 16-24 hours, drying in an oven at 80-110°C for 10-15 hours, and calcining at 550-650°C for 4-8 hours.

[0015] Furthermore, the proportions of each component in the catalyst for the hydrogenation of epoxide to β-phenylethanol are as follows: NiO: 15.3–24%, MoO3: 12.65–17.46%, Al2O3: 55.0–69.3%, TiO2: 3.2–4.11%, K2O: 0.12–0.8%, Nb2O5: 0.2–0.5%, ZrO2: 1.0–2.0%, with C as the balance.

[0016] The application of the catalyst for the hydrogenation of epoxide to β-phenylethanol prepared by the method described above involves mixing epoxide, solvent, hydrogen, and a hydrogen dissolving agent and reacting them in a fixed-bed reactor packed with the catalyst to produce the product.

[0017] Furthermore, the molar ratio of phenylene oxide to hydrogen is 1:2 to 1:6, and the molar ratio of phenylene oxide to solvent is 1:1 to 1:4.

[0018] Furthermore, the molar ratio of the epoxide to the hydrogen is 1:4 to 1:5, and the molar ratio of the epoxide to the solvent is 1:2 to 1:3.

[0019] Furthermore, the reaction temperature of the fixed-bed reactor is 60–110°C; the reaction pressure of the fixed-bed reactor is 1–2 MPa.

[0020] Furthermore, the reaction temperature of the fixed-bed reactor is 75–95°C; the reaction pressure of the fixed-bed reactor is 1.2–1.6 MPa.

[0021] Furthermore, the space velocity of the epoxide and the solvent is 0.1–3 h⁻¹. -1 .

[0022] Furthermore, the space velocity of the epoxide and the solvent is 0.5–1.5 h⁻¹. -1 .

[0023] Furthermore, the solvent is diethylene glycol butyl ether.

[0024] Furthermore, the hydrogen dissolving agent is tetrahydronaphthalene, and the mass content of the tetrahydronaphthalene is 0.001 to 0.015 of the mass content of the epoxy phenylene oxide.

[0025] The present invention can bring the following beneficial effects:

[0026] 1. This invention uses a solid catalyst containing nickel-molybdenum-niobium-titanium-aluminum metal oxides obtained by impregnation, and by adjusting the reaction conditions of the fixed-bed reactor, epoxide phenyl ethane is completely reacted to generate the target product β-phenylethanol. The reaction has a high conversion rate, good selectivity, simple process flow, low energy consumption, and saves on equipment investment.

[0027] 2. The catalyst of the present invention does not contain precious metals, and the preparation process is simple, requires no precision instruments, and is low in cost.

[0028] 3. In this invention, thorough mixing and double calcination ensure uniform distribution of the various substances in the catalyst, enhancing the stability and reactivity of the catalytic reaction and improving production efficiency.

[0029] 4. The mesoporous alumina in this invention has a high specific surface area, suitable pore structure, narrow pore size distribution and good surface acidity. Using mesoporous alumina to prepare titanium aluminum oxide support and loading the active components in the catalyst further improves the catalytic effect of the catalyst.

[0030] 5. This invention uses a fixed-bed hydrogenation reactor and a hydrogen dissolving agent to regulate the reaction rate. Combined with the catalyst used in this invention, epoxide phenylene oxide can be completely reacted at a suitable molar ratio to produce the target product β-phenylethanol.

[0031] 6. By adjusting the temperature, pressure, and molar ratio of phenylene oxide and hydrogen in the fixed-bed reactor, this invention can regulate and control the reaction in real time, and improve the conversion rate and selectivity of the reaction. Attached Figure Description

[0032] The accompanying drawings, which are included to provide a further understanding of the invention and form part of this invention, illustrate exemplary embodiments of the invention and are used to explain the invention, but do not constitute an undue limitation of the invention. In the drawings:

[0033] Figure 1 This is a flowchart of the preparation process of β-phenylethanol in this invention. Detailed Implementation

[0034] The present invention will be further described below with reference to the embodiments. However, the content of the present invention is not limited to these embodiments.

[0035] The aluminum sec-butoxide, sec-butanol, lauric acid, tetrabutyl titanate, triethylamine, ethanol, nickel nitrate, ammonium molybdate, niobium oxalate, ZrOCl2·8H2O, and potassium hydroxide mentioned below are all chemically pure substances.

[0036] Example 1

[0037] 500g of lauric acid was prepared into a 10% sec-butanol solution, and 3000g of aluminum sec-butoxide was also prepared into a 10% sec-butanol solution. The sec-butanol solution containing lauric acid was then slowly added dropwise to the solution containing aluminum sec-butoxide, and the mixture was stirred for 1 hour. Deionized water was then added dropwise, and the mixture was stirred continuously for 18 hours. The mixture was then filtered, washed with water until neutral, dried in a 90℃ oven for 12 hours, and calcined in a muffle furnace at 580℃ for 6 hours to obtain the porous alumina material. The prepared porous alumina was mixed in a molar ratio of tetrabutyl titanate:triethylamine:porous alumina:anhydrous ethanol = 1:6:14:150, stirred thoroughly for 18 hours, filtered, air-dried at room temperature, and then calcined for the first time in air at 550℃ for 5 hours to prepare the desired titanium-aluminum oxide support.

[0038] Mix 300g of 40% nickel nitrate solution, 302g of 25% ammonium molybdate solution, and 60g of 10% ZrOCl2 solution evenly. Then add 200.0g of titanium aluminum oxide support to the prepared solution, stir, and add 2g of niobium oxalate. After impregnation for 12h, adjust the pH value with potassium hydroxide to 9.5. Dry at 95℃ for 16h and calcine a second time at 520℃ for 4h to obtain catalyst product A (mass content: nickel monoxide 16.85%, molybdenum trioxide 12.67%, aluminum trioxide 64.69%, titanium dioxide 3.6%, zirconium dioxide 1.43%, niobium pentoxide 0.35%, potassium oxide 0.15%, carbon 0.26%).

[0039] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.2 MPa, a reaction temperature of 90 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.012 of the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1 Under the action of catalyst A, the hydrogenation reaction of epoxide phenyl ethane occurs to produce the target product β-phenylethanol. The conversion rate of epoxide phenyl ethane is 99.21%, and the selectivity of β-phenylethanol is 99.16%. After the catalyst has been running for 1000 hours, the conversion rate of epoxide phenyl ethane decreases slightly, while the selectivity of β-phenylethanol remains basically unchanged.

[0040] Example 2

[0041] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0042] 480g of 40% nickel nitrate solution, 360g of 25% ammonium molybdate solution, and 60g of 10% ZrOCl2 solution were mixed evenly. Then, 200.0g of titanium aluminum oxide support was added to the prepared solution, stirred, and 2g of niobium oxalate was added. After impregnation for 12h, the pH value was adjusted with potassium hydroxide to 9.5. The solution was dried at 95℃ for 16h and then calcined for a second time at 520℃ for 4h to obtain catalyst product B (mass content: nickel monoxide 23.92%, molybdenum trioxide 13.43%, aluminum trioxide 57.59%, titanium dioxide 3.21%, zirconium dioxide 1.27%, niobium pentoxide 0.31%, potassium oxide 0.17%, carbon 0.01%).

[0043] See Figure 1 The process flow shown is as follows: fixed-bed reactor pressure 1.5 MPa, reaction temperature 90 °C, diethylene glycol butyl ether as solvent, solvent to phenylene oxide molar ratio 2:1, tetrahydronaphthalene added 0.012 of the mass of phenylene oxide, hydrogen to phenylene oxide molar ratio 5:1, and phenylene oxide to solvent space velocity 1.50 h⁻¹. -1 Under the action of catalyst B, the hydrogenation reaction of epoxide phenyl ethane occurs to produce the target product β-phenylethanol. The conversion rate of epoxide phenyl ethane is 99.84%, and the selectivity of β-phenylethanol is 99.05%. After 700 hours of catalyst operation, the conversion rate of epoxide phenyl ethane and the selectivity of β-phenylethanol remain basically unchanged.

[0044] Example 3

[0045] The preparation process of catalyst A is shown in Example 1.

[0046] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.5 MPa, a reaction temperature of 90 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.015 times the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 2.50 h⁻¹. -1 Under the action of catalyst A, the hydrogenation reaction of epoxide-phenylene oxide occurs to produce the target product β-phenylethanol. The conversion rate of epoxide-phenylene oxide is 99.27%, and the selectivity of β-phenylethanol is 99.19%.

[0047] Example 4

[0048] The preparation process of catalyst B is shown in Example 2.

[0049] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.5 MPa, a reaction temperature of 85 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.014 times the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 2.5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1 Under the action of catalyst B, the hydrogenation reaction of epoxide phenylene oxide occurs to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.78%, and the selectivity of β-phenylethanol is 99.15%.

[0050] Comparative Example 5

[0051] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0052] Mix 300g of 40% nickel nitrate solution, 300g of 25% ammonium molybdate solution, and 60g of 10% ZrOCl2 solution evenly. Then add 200.0g of titanium aluminum oxide support to the prepared solution, stir, and impregnate for 12 hours. Adjust the pH value with potassium hydroxide to 9.5. Dry at 95℃ for 18 hours and calcine a second time at 520℃ for 4 hours to obtain catalyst product C (mass content: nickel monoxide 16.91%, molybdenum trioxide 12.66%, aluminum oxide 64.92%, titanium dioxide 3.61%, zirconium dioxide 1.44%, potassium oxide 0.15%, carbon 0.31%).

[0053] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.5 MPa, a reaction temperature of 85 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.011 times the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1 Under the action of catalyst C, the hydrogenation reaction of epoxide phenylene oxide occurs to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.78%, and the selectivity of β-phenylethanol is 97.15%.

[0054] Comparative Example 6

[0055] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0056] 300g of a 40% nickel nitrate solution and 300g of a 25% ammonium molybdate solution were mixed thoroughly. Then, 200.0g of titanium aluminum oxide support was added to the prepared solution, stirred, and 2g of niobium oxalate was added. After impregnation for 12 hours, the pH value was adjusted with potassium hydroxide to 9.5. The solution was dried at 95℃ for 18 hours and then calcined a second time at 520℃ for 4 hours to obtain catalyst product D (mass content: nickel monoxide 17.09%, molybdenum trioxide 12.80%, aluminum trioxide 65.63%, titanium dioxide 3.65%, niobium pentoxide 0.36%, potassium oxide 0.15%, carbon 0.32%).

[0057] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.2 MPa, a reaction temperature of 90 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.015 times the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1 Under the action of catalyst D, epoxide phenylene oxide undergoes a hydrogenation reaction to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.73%, and the selectivity of β-phenylethanol is 95.18%.

[0058] Comparative Example 7

[0059] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0060] 300g of a 40% nickel nitrate solution, 302g of a 25% ammonium molybdate solution, and 100g of a 10% ZrOCl2 solution were mixed thoroughly. Then, 200.0g of titanium aluminum oxide support was added to the prepared solution, stirred, and 2g of niobium oxalate was added. After impregnation for 12 hours, the pH was adjusted to 9.5 with potassium hydroxide. The solution was dried at 95℃ for 16 hours and then calcined a second time at 520℃ for 4 hours to obtain catalyst product E (mass content: nickel monoxide 16.64%, molybdenum trioxide 12.65%, aluminum trioxide 64.20%, titanium dioxide 3.57%, zirconium dioxide 2.35%, niobium pentoxide 0.35%, potassium oxide 0.14%, carbon 0.10%).

[0061] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.2 MPa, a reaction temperature of 90 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.012 of the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1Under the action of catalyst E, epoxide phenylene oxide undergoes a hydrogenation reaction to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.34%, and the selectivity of β-phenylethanol is 98.13%.

[0062] Comparative Example 8

[0063] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0064] Mix 300g of 40% nickel nitrate solution, 302g of 25% ammonium molybdate solution, and 60g of 10% ZrOCl2 solution evenly. Then add 200.0g of titanium aluminum oxide support to the prepared solution, stir, and add 4g of niobium oxalate. After impregnation for 12h, adjust the pH value with potassium hydroxide to 9.5. Dry at 95℃ for 16h, and calcine a second time at 520℃ for 4h to obtain catalyst product F (mass content: nickel monoxide 16.77%, molybdenum trioxide 12.67%, aluminum trioxide 64.08%, titanium dioxide 3.59%, zirconium dioxide 1.41%, niobium pentoxide 0.71%, potassium oxide 0.15%, carbon 0.62%).

[0065] See Figure 1 The process flow shown features a fixed-bed reactor at a pressure of 1.2 MPa, a reaction temperature of 90 °C, diethylene glycol butyl ether as the solvent, a solvent-to-epoxyphenyl ethane molar ratio of 2:1, tetrahydronaphthalene added at 0.014 times the mass of epoxyphenyl ethane, a hydrogen-to-epoxyphenyl ethane molar ratio of 5:1, and an epoxyphenyl ethane-solvent space velocity of 1.50 h⁻¹. -1 Under the action of catalyst F, epoxide phenylene oxide undergoes a hydrogenation reaction to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.07%, and the selectivity of β-phenylethanol is 97.55%.

[0066] Comparative Example 9

[0067] The preparation process of the titanium aluminum oxide support is shown in Example 1.

[0068] Mix 520g of 40% nickel nitrate solution, 380g of 25% ammonium molybdate solution, and 60g of 10% ZrOCl2 solution evenly. Then add 200.0g of titanium aluminum oxide support to the prepared solution, stir, and add 2g of niobium oxalate. After impregnation for 12h, adjust the pH value with potassium hydroxide to 9.5. Dry at 95℃ for 19h and calcine a second time at 520℃ for 4h to obtain catalyst product G (mass content: nickel monoxide 25.24%, molybdenum trioxide 13.81%, aluminum trioxide 56.04%, titanium dioxide 3.15%, zirconium dioxide 1.23%, niobium pentoxide 0.31%, potassium oxide 0.16%, carbon 0.06%).

[0069] See Figure 1 The process flow shown is as follows: fixed-bed reactor pressure 1.2 MPa, reaction temperature 90 °C, diethylene glycol butyl ether as solvent, solvent to phenylene oxide molar ratio 2:1, tetrahydronaphthalene added 0.012 of the mass of phenylene oxide, hydrogen to phenylene oxide molar ratio 4:1, and phenylene oxide to solvent space velocity 1.50 h⁻¹. -1 Under the action of catalyst G, epoxide phenylene oxide undergoes a hydrogenation reaction to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 99.88%, and the selectivity of β-phenylethanol is 93.05%.

[0070] Comparative Example 10

[0071] The preparation process of catalyst A is shown in Example 1.

[0072] See Figure 1 The process flow shown is as follows: fixed-bed reactor pressure 1.2 MPa, reaction temperature 90 °C, diethylene glycol butyl ether as solvent, solvent to phenylene oxide molar ratio 2:1, no tetrahydronaphthalene added, hydrogen to phenylene oxide molar ratio 5:1, and phenylene oxide to solvent space velocity 1.50 h⁻¹. -1 Under the action of catalyst A, the hydrogenation reaction of epoxide phenylene oxide occurs to produce the target product β-phenylethanol. The conversion rate of epoxide phenylene oxide is 98.07%, and the selectivity of β-phenylethanol is 94.55%.

[0073] Table 1 Catalytic performance of the catalysts prepared in the examples

[0074] Conversion rate of epoxide Selectivity of β-phenylethanol Example 1 99.21％ 99.16％ Example 2 99.84％ 99.05％ Example 3 99.27％ 99.19％ Example 4 99.78％ 99.15％ Comparative Example 5 99.78％ 97.15％ Comparative Example 6 99.73％ 95.18％ Comparative Example 7 99.34％ 98.13％ Comparative Example 8 99.07％ 97.55％ Comparative Example 9 99.88％ 93.05％ Comparative Example 10 98.07％ 94.55％

[0075] As can be seen from the above examples and comparative examples, catalysts made with different proportions of raw materials have different conversion rates of epoxide and different selectivity of β-phenylethanol. Furthermore, in comparative examples 7-9, excessive zirconium, niobium, and nickel elements also cause a decrease in the final selectivity of β-phenylethanol.

[0076] The various embodiments in this specification are described in a progressive manner. Similar or identical parts between embodiments can be referred to interchangeably. Each embodiment focuses on describing the differences from other embodiments. In particular, the system embodiments are basically similar to the method embodiments, so the description is relatively simple; relevant parts can be referred to the descriptions in the method embodiments.

[0077] The above description is merely an embodiment of the present invention and is not intended to limit the invention. Various modifications and variations can be made to the present invention by those skilled in the art. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principle of the present invention should be included within the scope of the claims of the present invention.

Claims

1. A method for preparing a catalyst for the hydrogenation of epoxide to β-phenylethanol, characterized in that, Includes the following steps: (1) Prepare a solution of nickel acetate, ammonium molybdate, ZrOCl2·8H2O and niobium oxalate; (2) Add titanium aluminum oxide carrier to the solution, stir, and impregnate; (3) Add potassium hydroxide to the solution to form a precipitate, then wash with water, dry, and calcine to obtain the catalyst product for the hydrogenation of epoxide to β-phenylethanol; The titanium aluminate carrier is prepared by stirring tetrabutyl titanate, triethylamine, mesoporous alumina, and low carbon alcohol for 16-24 hours, filtering, air drying at room temperature, and calcining in an air atmosphere. The main active component in the catalyst for the hydrogenation of epoxide to β-phenylethanol is Ni. 2+ Mo 6+ Zr 4+ 、Nb 5+ The active ingredient is Al. 3+ Ti 4+ .

2. The method for preparing the catalyst for the hydrogenation of epoxide to β-phenylethanol according to claim 1, characterized in that, The roasting temperature is 450–600℃ and the time is 2–6 hours; the roasting temperature in the air atmosphere is 520–620℃ and the time is 3–6 hours.

3. The method for preparing the catalyst for the hydrogenation of epoxide to β-phenylethanol according to claim 1, characterized in that, The mesoporous alumina is prepared by dissolving lauric acid and aluminum sec-butoxide separately in sec-butanol, then adding the sec-butanol solution containing lauric acid dropwise to the solution containing aluminum sec-butoxide, stirring, then adding water dropwise, stirring continuously for 16-24 hours, filtering and washing with water until neutral, drying in an oven at 80-110℃ for 10-15 hours, and calcining at 550-650℃ for 4-8 hours.

4. The method for preparing the catalyst for the hydrogenation of epoxide to β-phenylethanol according to claim 1, characterized in that, The mass content of each component in the catalyst for the hydrogenation of epoxide to β-phenylethanol is as follows: NiO: 15.3-24%, MoO3: 12.65-17.46%, Al2O3: 55.0-69.3%, TiO2: 3.2-4.11%, K2O: 0.12-0.8%, Nb2O5: 0.2-0.5%, ZrO2: 1.0-2.0%, with C as the balance.

5. The application of the catalyst for the hydrogenation of epoxide to β-phenylethanol prepared by any one of the preparation methods according to claims 1-4, characterized in that, Epoxy phenylene oxide, solvent, hydrogen, and hydrogen dissolving agent are mixed and reacted in a fixed-bed reactor containing a catalyst for the hydrogenation of epoxy phenylene oxide to β-phenylethanol to produce the product.

6. The application according to claim 5, characterized in that, The molar ratio of phenylene oxide to hydrogen is 1:2 to 1:6, and the molar ratio of phenylene oxide to solvent is 1:1 to 1:

4.

7. The application according to claim 5, characterized in that, The reaction temperature of the fixed-bed reactor is 60–110°C; the reaction pressure of the fixed-bed reactor is 1–2 MPa.

8. The application according to claim 5, characterized in that, The space velocity of the epoxide and the solvent is 0.1–3 h⁻¹. -1 .

9. The application according to claim 5, characterized in that, The solvent is diethylene glycol butyl ether.

10. The application according to claim 5, characterized in that, The hydrogen dissolving agent is tetrahydronaphthalene, and the mass content of the tetrahydronaphthalene is 0.001 to 0.015 of the mass content of the epoxy phenylene oxide.

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