A catalyst for preparing 1-phenylethanol by hydrogenating acetophenone, a preparation method and application thereof

Abstract

The application relates to a CuZn / Silicalite-1 catalyst for directly hydrogenating acetophenone into 1-phenylethanol as well as a preparation method and application of the catalyst. The catalyst comprises copper oxide, zinc oxide and a molecular sieve Silicalite-1, and the preparation method comprises the following steps: precipitating, aging, filtering, washing and drying a mixed solution of a copper salt and a zinc salt and an alkali solution to obtain an oxide precursor; uniformly mixing an aqueous template agent tetrapropylammonium hydroxide solution, tetraethyl orthosilicate and deionized water, and crystallizing, centrifuging, washing and drying to obtain a molecular sieve raw powder; ball-milling and calcining the oxide precursor and the molecular sieve raw powder; uniformly mixing the calcined catalyst and an additive, and tabletting to form a shaped catalyst. The catalyst prepared by the method has the advantages of high dispersion degree of the active component Cu and difficulty in sintering, and the catalyst has high activity and selectivity.

Description

TECHNICAL FIELD

[0001] The application belongs to the technical field of catalytic hydrogenation, and particularly relates to a catalyst for preparing 1-phenylethanol by liquid-phase hydrogenation of acetophenone as well as a preparation method and application thereof. BACKGROUND

[0002] 1-phenylethanol is an important chemical product and is widely used in the pharmaceutical industry and the perfume manufacturing industry. Among various routes for synthesizing 1-phenylethanol, the preparation of 1-phenylethanol by catalytic hydrogenation of acetophenone is widely concerned because it is most consistent with atomic economy.

[0003] The reaction of preparing 1-phenylethanol by hydrogenation of acetophenone has multiple side reactions, and the development of a high-activity and high-selectivity catalyst for hydrogenation of acetophenone is a research focus. The catalysts used for hydrogenation of acetophenone mainly include noble metal catalysts such as Pt, Pd and Rh, and non-noble metal catalysts such as Ni-based and Cu-based catalysts. Among them, the noble metal catalysts are high in price, and the 1-phenylethanol selectivity of the Ni-based catalyst is low. Compared with the above catalysts, the Cu-based catalyst has the advantages of high activity, high selectivity and low price in the reaction of hydrogenation of acetophenone.

[0004] The Cu-based catalyst for hydrogenation of acetophenone has been reported in the literature and patents, and researchers have done a lot of work to optimize the catalyst performance. Lv et al. prepared a SiO2-supported nano-Cu catalyst by optimizing the preparation method and using a urea homogeneous precipitation method, so that the acetophenone conversion rate and reaction stability were improved (Applied Organometallic Chemistry. 2019, 33(8), e5000; Catalysis Letters. 2020, 150(1), 56-64).

[0005] Patent CN 112221508A discloses a heterogeneous shaped SiO2-supported CuZn@C catalyst, which reduces the use amount of Cu and the use of a promoter.

[0006] Patents CN 115445629 A, CN 111346638 A and CN 108043414 A respectively disclose Cu-based catalysts for hydrogenation of acetophenone with different combinations and structures, which improve the catalyst performance by adding additives, adjusting the catalyst structure and the like.

[0007] The hydrogenolysis / dehydration side reaction of 1-phenylethanol is prone to occur in the process of hydrogenation of acetophenone, and ethylbenzene / phenylethylene is generated. In order to obtain a high-efficiency catalyst for hydrogenation of acetophenone, it is necessary to not only promote the acetophenone conversion rate by using a Cu active component with high dispersity, but also to promote the selectivity of by-products by using a catalyst with few strong acid sites, and to promote the stability of the catalyst by using a Cu active component with strong anti-sintering ability.

[0008] Therefore, in view of the problems of the Cu-based catalyst for preparing 1-phenylethanol by hydrogenation of acetophenone, such as low dispersion of active component Cu, strong acidity of the catalyst, and weak interaction between the carrier and the active component, how to improve the dispersion and stability of the active component Cu and control the acidity of the catalyst by using a simple preparation method and by regulating the additives and the carrier is of great significance for preparing a high-performance catalyst for hydrogenation of acetophenone. SUMMARY

[0009] According to a first aspect of the present application, a catalyst for preparing 1-phenylethanol by hydrogenation of acetophenone is provided, which has high dispersion of active component Cu and is not prone to sintering, and has high activity and good selectivity.

[0010] The CuZn / Silicalite-1 catalyst for preparing 1-phenylethanol by hydrogenation of acetophenone provided in the present application contains, based on the weight of the catalyst, 16-35 wt% of copper oxide, 24%-45 wt% of zinc oxide, and 25-60 wt% of Silicalite-1 molecular sieve.

[0011] According to a second aspect of the present application, a preparation method of the catalyst for preparing 1-phenylethanol by hydrogenation of acetophenone is provided, and the method comprises the following steps:

[0012] (1) mixing a mixed solution in which copper salt and zinc salt are dissolved with an alkali solution to perform precipitation, aging, filtration, washing, and drying, to obtain an oxide precursor;

[0013] (2) uniformly mixing an aqueous template agent tetrapropylammonium hydroxide solution, tetraethyl orthosilicate, and deionized water, and sequentially performing crystallization, centrifugation, washing, and drying on the mixture to obtain a molecular sieve raw powder;

[0014] (3) mixing the oxide precursor and the molecular sieve raw powder to perform ball milling treatment, and performing calcination on the sample after the ball milling treatment to obtain a catalyst;

[0015] (4) uniformly mixing the catalyst after the calcination with an additive, and tabletting to form a shaped catalyst.

[0016] The copper salt is selected from one or both of copper nitrate and copper acetate, and the zinc salt is selected from one or both of zinc nitrate and zinc acetate. The total molar concentration of metal ions in the copper-zinc mixed salt solution is 0.5-2 mol / L, and preferably 0.8-1.2 mol / L.

[0017] The alkali solution is selected from an aqueous solution of at least one of sodium carbonate or sodium bicarbonate, and the molar concentration of alkali molecules in the alkali solution is 0.5-2 mol / L, and preferably 0.8-1.2 mol / L.

[0018] The total molar concentration of metal ions in the mixed solution and the molar concentration of base molecules in the base solution can be the same or different, preferably the same or substantially the same.

[0019] The mixing and precipitation in step (1) specifically includes the following conditions:

[0020] The mixing and precipitation mode is parallel flow precipitation.

[0021] The precipitation temperature is 50-70℃;

[0022] The precipitation pH value is 6.0-9.0; preferably 6.5-8.2;

[0023] The aging temperature is 55-75℃;

[0024] The aging time is 20-50min; preferably 25-35min.

[0025] The crystallization process in step (2) specifically includes the following conditions:

[0026] The molar ratio of the amount of template agent tetrapropylammonium hydroxide to the amount of tetraethyl orthosilicate is 4:1;

[0027] The molar ratio of the amount of deionized water to the amount of tetraethyl orthosilicate is (8.5-100):1; preferably (8.5-50):1;

[0028] The crystallization temperature is 130-180℃; preferably 150-180℃;

[0029] The crystallization time is 24-72h.

[0030] The ball milling process in step (3) is specifically as follows: carried out in a ball mill, the diameter of the grinding balls in the ball mill is 5-20mm, the rotation speed of the grinding balls is 400-500r / min, and the ball milling time is 12-24h.

[0031] The drying temperatures in step (1) and step (2) can be the same or different, and the drying times can be the same or different, wherein the drying temperatures are both in the range of 100-120℃, and the drying times are both 12-24h;

[0032] The calcination temperature in step (3) is in the range of 350-550℃, and the calcination time is 2-6h.

[0033] In a specific embodiment, the preparation method of the catalyst includes the following steps:

[0034] (1) A certain amount of soluble copper salt and zinc salt are dissolved in deionized water to prepare a mixed salt solution, and a certain amount of base is dissolved in deionized water to prepare a base solution;

[0035] (2) After the two aqueous solutions are precipitated under the condition of a certain temperature and a certain pH value, the oxide precursor is obtained by aging, filtering and drying;

[0036] (3) A certain amount of tetrapropylammonium hydroxide, tetraethyl orthosilicate and deionized water are weighed and mixed to prepare a mixed solution, which is then added into a high-pressure reaction kettle, and the molecular sieve raw powder is obtained by centrifuging, washing and drying after crystallization under a certain temperature for a certain time;

[0037] (4) A certain amount of the oxide precursor and the molecular sieve raw powder are mixed and subjected to ball milling treatment, and the catalyst is obtained by calcining the sample after the ball milling treatment;

[0038] (5) The calcined catalyst is mixed with an additive, and the shaped catalyst is obtained by tabletting.

[0039] Optionally, the soluble copper salt and zinc salt are selected from one or both of the nitrate and acetate of the metal; and the alkali solution is selected from an aqueous solution of at least one of sodium carbonate or sodium bicarbonate.

[0040] Optionally, the total molar concentration of metal ions in the salt solution and the molar concentration of the alkali solution are substantially the same during the preparation of the salt solution and the alkali solution, and are in the range of 0.5-2 mol / L, preferably 0.8-1.2 mol / L.

[0041] Optionally, the precipitation process is carried out under water bath conditions, and the pH value in the precipitation process is controlled by adjusting the flow rates of the salt solution and the alkali solution under the stirring condition of a stirring paddle. Specifically, the water bath temperature is 50-70℃; the pH value is 6.0-9.0, preferably the pH value is 6.5-8.2; the aging temperature is 55-75℃; and the aging time is 20-50 min, preferably 25-35 min.

[0042] Optionally, the drying process refers to drying the obtained solid under the condition of 100-120℃ for 12-24 h.

[0043] Optionally, the crystallization process is carried out in a high-pressure reaction kettle, and the prepared mixed solution is added into the high-pressure reaction kettle and placed in an oven. Specifically, the crystallization temperature is 130-180℃, preferably 150-180℃; and the crystallization time is 24-72 h.

[0044] Optionally, the ball milling process is carried out in a ball mill, and the oxide precursor and the molecular sieve raw powder are mixed and then added into a ball mill tank for ball milling with milling balls. Specifically, the milling ball rotation speed is 400-500 r / min, and the ball milling time is 12-24 h.

[0045] Optionally, the calcination process refers to calcination of the dried solid at 350-550℃; specifically, first, heat to 150℃ at a heating rate of 2℃ / min, keep for 2h, then continue to heat to 350-550℃ at a heating rate of 2℃ / min, keep for 2-6h.

[0046] Optionally, the tabletting process is carried out on a tablet press, and the specification of the shaped catalyst is selected as needed.

[0047] According to a third aspect of the present application, a method for preparing 1-phenylethanol by hydrogenation of acetophenone is provided, which comprises mixing a solution containing acetophenone and hydrogen gas through a reactor, and contacting the solution with at least one of the catalysts according to any one of the above-mentioned catalysts or the catalysts prepared by the method according to any one of the above-mentioned methods, to generate 1-phenylethanol.

[0048] In a specific embodiment, a method for preparing 1-phenylethanol by hydrogenation of acetophenone comprises:

[0049] The catalyst is reduced and activated by first increasing the temperature of the reactor to 170℃ under a nitrogen atmosphere, keeping the nitrogen gas volumetric space velocity at 300-600h -1 -1, and keeping the temperature constant for 1-2h to remove the physical water adsorbed by the catalyst. The catalyst is reduced by passing a mixed gas of hydrogen and nitrogen, keeping the mixed gas volumetric space velocity at 300-600h -1 -1, and the hydrogen volume fraction is not more than 10%; after reduction for at least 1h, the hydrogen concentration is gradually increased to a volume fraction of 10%, 20%, 30%, 50%, and 100%, and the hot spot temperature of the catalyst bed during the reduction process is controlled to be not more than 230℃; the temperature is increased to 200-230℃, and the catalyst is reduced under a full hydrogen atmosphere for 2-4h to obtain the activated catalyst.

[0050] Optionally, the specific conditions of the contacting reaction include:

[0051] The reaction temperature is 80-130℃;

[0052] The reaction pressure is 1.5-2.6MPa;

[0053] The molar ratio of H2 / acetophenone is (3-20):1;

[0054] The liquid hourly space velocity of acetophenone is 0.4-0.6g·g cat -1 ·h -1 .

[0055] The beneficial effects of the present application include but are not limited to:

[0056] (1) The present application provides a catalyst for preparing 1-phenylethanol by hydrogenation of acetophenone, which has the characteristics of high dispersion of active component Cu and low sintering of active component, and has the advantages of high reaction activity and high stability of the catalyst.

[0057] (2) The application provides a catalyst for preparing 1-phenylethanol by hydrogenating acetophenone. In the preparation process, the isomorphism replacement phenomenon of Zn and Cu in the oxide precursor can effectively promote the dispersion of the Cu component of the active component and make the final shaped catalyst have rich copper-zinc oxide interfaces.

[0058] (3) The application provides a catalyst for preparing 1-phenylethanol by hydrogenating acetophenone. The addition of the carrier Silicalite-1 enables the active component to be highly dispersed and to be stably present in the reaction process through the anchoring of the active component by the interaction between the carrier hydroxyl pits and metal species.

[0059] (4) The application provides a catalyst for preparing 1-phenylethanol by hydrogenating acetophenone. The oxide precursor and the molecular sieve raw powder are first ball milled and then calcined, so that the metal component can be uniformly dispersed in the molecular sieve and can be fully contacted with the carrier hydroxyl pits.

[0060] (5) The catalyst of the application is applied to the reaction of preparing 1-phenylethanol by hydrogenating acetophenone, can ensure high product yield, and has a wide adjustable range of reaction process conditions, so that the application has universality and has a very wide industrial application range. Embodiment

[0061] The application will be described in detail below with reference to the embodiments, but the application is not limited to the embodiments.

[0062] In the embodiments of the application, the raw materials are purchased through commercial channels unless otherwise specified.

[0063] The raw material acetophenone and the hydrogenation reaction product are detected by using an Agilent 7890A gas chromatograph and a DB-Waxer capillary column of Agilent.

[0064] In the embodiments of the application, the conversion rate and the selectivity are calculated as follows:

[0065] Acetophenone conversion rate = (moles of acetophenone in the feed - moles of acetophenone in the discharge) ÷ moles of acetophenone in the feed × 100%

[0066] 1-phenylethanol selectivity = moles of 1-phenylethanol in the discharge / (moles of acetophenone in the feed - moles of acetophenone in the discharge) × 100% Example 1

[0067] Take 198.9 g of zinc nitrate, 131.3 g of copper nitrate, and dissolve them in 1750 mL of deionized water to obtain an aqueous solution I; take 185.5 g of ammonium carbonate and dissolve them in 1750 mL of deionized water to obtain an aqueous solution II; under the condition of a 70℃ water bath and stirring paddle stirring, co-precipitate the aqueous solution I and the aqueous solution II in parallel flow, and control the pH in the precipitate to be 6.2-6.4. After co-precipitation, age at 75℃ for 30 min, wash, and dry at 100℃ for 12 h to obtain an oxide precursor.

[0068] Take 203.4 g of a tetrapropylammonium hydroxide aqueous solution (25 wt%), 208.3 g of tetraethyl orthosilicate, and 747.5 g of deionized water, mix and stir for 4 h to obtain a solution III. Add the solution III into a high-pressure reaction kettle, crystallize at 180℃ for 72 h, centrifuge and wash, and then dry at 100℃ for 12 h to obtain a molecular sieve raw powder.

[0069] Take 194.4 g of the oxide precursor and 70.6 g of the molecular sieve raw powder, place them in a ball mill tank of a ball mill, add mill balls, adjust the rotation speed of the mill balls to be 500 r / min, and ball mill for 12 h. After ball milling, the sample is calcined at 500℃ for 3 h to obtain a catalyst. Mix the calcined catalyst with an additive, uniformly tablet, and form to obtain a formed catalyst. Example 2

[0070] Take 198.9 g of zinc nitrate, 131.3 g of copper nitrate, and dissolve them in 1750 mL of deionized water to obtain an aqueous solution I; take 222.6 g of ammonium carbonate and dissolve them in 2100 mL of deionized water to obtain an aqueous solution II; under the condition of a 65℃ water bath and stirring paddle stirring, co-precipitate the aqueous solution I and the aqueous solution II in parallel flow, and control the pH in the precipitate to be 6.9-7.1. After co-precipitation, age at 70℃ for 30 min, wash, and dry at 100℃ for 12 h to obtain an oxide precursor.

[0071] Take 203.4 g of a tetrapropylammonium hydroxide aqueous solution (25 wt%), 208.3 g of tetraethyl orthosilicate, and mix and stir for 4 h to obtain a solution III. Add the solution III into a high-pressure reaction kettle, crystallize at 170℃ for 24 h, centrifuge and wash, and then dry at 100℃ for 12 h to obtain a molecular sieve raw powder.

[0072] The subsequent preparation procedure is consistent with Example 1. Example 3

[0073] Take 181.8 g of zinc nitrate, 150.1 g of copper nitrate, and dissolve them in 1750 mL of deionized water to obtain an aqueous solution I; take 264.6 g of ammonium carbonate and dissolve them in 2650 mL of deionized water to obtain an aqueous solution II; under the condition of a 60℃ water bath and stirring paddle stirring, co-precipitate the aqueous solution I and the aqueous solution II in parallel flow, and control the pH in the precipitate to be 7.6-7.8. After co-precipitation, age at 65℃ for 30 min, wash, and dry at 100℃ for 12 h to obtain an oxide precursor.

[0074] The subsequent preparation procedure remains the same as that in Example 2, except that the calcination temperature is changed to 400℃. Example 4

[0075] Take 181.8 g of zinc nitrate, 150.1 g of copper nitrate, and dissolve them in 1750 mL of deionized water to obtain an aqueous solution I; take 264.6 g of ammonium carbonate and dissolve them in 2650 mL of deionized water to obtain an aqueous solution II; under the condition of a 60℃ water bath and stirring paddle stirring, co-precipitate the aqueous solution I and the aqueous solution II in parallel flow, and control the pH in the precipitate to be 7.6-7.8. After co-precipitation, age at 65℃ for 30 min, wash, and dry at 100℃ for 12 h to obtain an oxide precursor.

[0076] Take 244.0 g of a tetrapropylammonium hydroxide aqueous solution (25 wt%), 250.0 g of tetraethyl orthosilicate, and 465.0 g of deionized water, mix and stir for 4 h to obtain solution III. Add the solution III into a high-pressure reaction kettle, crystallize at 170℃ for 72 h, centrifuge and wash, and then dry at 100℃ for 12 h to obtain a molecular sieve raw powder.

[0077] Take 92.1 g of the oxide precursor and 86.0 g of the molecular sieve raw powder, place them in a ball mill jar, add grinding balls, adjust the rotation speed of the grinding balls to 400 r / min, and ball mill for 16 h. Calcine the ball-milled sample at 550℃ for 4 h to obtain a catalyst. Mix the calcined catalyst with an additive, uniformly tablet, and form to obtain a shaped catalyst. Example 5

[0078] Take 181.8 g of zinc nitrate, 150.1 g of copper nitrate, and dissolve them in 1750 mL of deionized water to obtain an aqueous solution I; take 264.6 g of ammonium carbonate and dissolve them in 2650 mL of deionized water to obtain an aqueous solution II; under the condition of a 60℃ water bath and stirring paddle stirring, co-precipitate the aqueous solution I and the aqueous solution II in parallel flow, and control the pH in the precipitate to be 7.6-7.8. After co-precipitation, age at 65℃ for 30 min, wash, and dry at 100℃ for 12 h to obtain an oxide precursor.

[0079] Take 269.5 g of tetrapropylammonium hydroxide aqueous solution (25 wt%), 173.6 g of tetraethyl orthosilicate, mix and stir for 4 h to obtain solution III. Add solution III into a high-pressure reaction kettle, crystallize at 170℃ for 48 h, centrifuge and wash, and then dry at 100℃ for 12 h to obtain the molecular sieve crude powder.

[0080] Take 192.9 g of oxide precursor and 60.0 g of molecular sieve crude powder, place them in the ball mill jar of a ball mill, add the grinding balls, and adjust the rotation speed of the grinding balls to 450 r / min, and ball mill for 12 h. The milled sample is calcined at 350℃ for 4 h to obtain the catalyst. The calcined catalyst is mixed with the additives, and then sheeted and formed to obtain the shaped catalyst. Example 6

[0081] Take 84.4 g of zinc nitrate and 85.2 g of copper nitrate, and dissolve them in 900 mL of deionized water to obtain aqueous solution I; take 115.0 g of ammonium carbonate and dissolve it in 1200 mL of deionized water to obtain aqueous solution II; under the conditions of a 60℃ water bath and stirring paddle stirring, co-precipitate aqueous solution I and aqueous solution II in a parallel flow, and control the pH in the precipitate to be 7.4-7.5. After co-precipitation, age at 65℃ for 30 min, wash, and then dry at 100℃ for 12 h to obtain the oxide precursor.

[0082] Take 292.8 g of tetrapropylammonium hydroxide aqueous solution (25 wt%), 300.0 g of tetraethyl orthosilicate, and 298.9 g of deionized water, mix and stir for 4 h to obtain solution III. Add solution III into a high-pressure reaction kettle, crystallize at 170℃ for 72 h, centrifuge and wash, and then dry at 100℃ for 12 h to obtain the molecular sieve crude powder.

[0083] Take 72.9 g of oxide precursor and 102.0 g of molecular sieve crude powder, place them in the ball mill jar of a ball mill, add the grinding balls, and adjust the rotation speed of the grinding balls to 500 r / min, and ball mill for 12 h. The milled sample is calcined at 450℃ for 4 h to obtain the catalyst. The calcined catalyst is mixed with the additives, and then sheeted and formed to obtain the shaped catalyst. Example 7

[0084] The catalysts in the above Examples 1-6 are investigated for reaction performance under the following conditions.

[0085] Catalyst reduction and activation: the shaped catalyst is loaded into a fixed bed reactor, and the catalyst loading amount is 50 mL. First, the temperature of the reactor is raised to 170℃ under a nitrogen atmosphere, and the nitrogen volume space velocity is 480 h-1 -1, and the physical water adsorbed by the catalyst is removed at constant temperature for 2 hours. Then, the catalyst is reduced by passing a mixed gas of hydrogen and nitrogen, the volume fraction of hydrogen is 2%, and the reduction is performed for at least 1 hour, and then the hydrogen concentration is gradually increased to 5%, 10%, 20%, 50% and 100%, and the hot spot temperature of the catalyst bed in the reduction process is controlled to be not more than 230 DEG C; finally, the temperature is increased to 230 DEG C, and the catalyst is reduced in a full hydrogen atmosphere for 2 hours to obtain the activated catalyst.

[0086] Reaction evaluation: after the catalyst is reduced and activated, under the conditions of a reaction temperature of 90 DEG C and a reaction pressure of 2.3 MPa, a solution of ethylbenzene with a mass fraction of 15% of acetophenone is used as a reaction raw material, the liquid mass space velocity of acetophenone is controlled to be 0.4 g·g cat -1 ·h -1 , and the molar ratio of H2 / acetophenone is 15:1. Under the above conditions, the reaction product is obtained by performing the hydrogenation reaction of acetophenone, and the reaction results are shown in the following table.

[0087]

[0088] The above is only a few embodiments of the present application, and does not limit the present application in any form. Any skilled person in the art can make some changes or modifications to the above disclosed technical contents without departing from the scope of the technical scheme of the present application, and the equivalent embodiments are equivalent to the equivalent embodiments, which are all within the scope of the technical scheme.

Claims

1. A catalyst for the hydrogenation of acetophenone to 1-phenylethanol, characterized in that, Based on the weight of the catalyst, the catalyst comprises: 16-35 wt% copper oxide, 24%-45 wt% zinc oxide, and 25-60 wt% Silicalite-1 molecular sieve; The method for preparing the catalyst includes the following steps: (1) Mix the solution containing copper and zinc salts with an alkaline solution to precipitate, age, filter, wash and dry to obtain the oxide precursor; (2) Mix the template agent tetrapropylammonium hydroxide aqueous solution, tetraethyl orthosilicate and deionized water evenly, and then crystallize, centrifuge, wash and dry the mixture in sequence to obtain molecular sieve raw powder; (3) The oxide precursor and molecular sieve powder are mixed and ball-milled. The ball-milled sample is then calcined to obtain the catalyst. The specific process of the ball milling is as follows: it is carried out in a ball mill with a diameter of 5-20 mm, a rotation speed of 400-500 r / min, and a milling time of 12-24 h. (4) The calcined catalyst and the additive are mixed evenly and then formed into a sheet to obtain the shaped CuZn / Silicalite-1 catalyst.

2. The catalyst according to claim 1, characterized in that, The copper and zinc salts are selected from one or both of the nitrates or acetates of the corresponding metals.

3. The catalyst according to claim 1, characterized in that, The alkaline solution is an aqueous solution selected from at least one of sodium carbonate or sodium bicarbonate.

4. The catalyst according to claim 1, characterized in that, The mixed precipitation mentioned in step (1) specifically includes the following conditions: the mixed precipitation method is co-current precipitation; the precipitation temperature is 50-70℃; the precipitation pH value is 6.0-9.0; the aging temperature is 55-75℃; and the aging time is 20-50min.

5. The catalyst according to claim 1, characterized in that, In the crystallization process described in step (2), the raw material composition conditions include: the molar ratio of the template agent tetrapropylammonium hydroxide to tetraethyl orthosilicate is 4:1; the molar ratio of the deionized water to tetraethyl orthosilicate is (8.5-100):

1.

6. The catalyst according to claim 1, characterized in that, In the crystallization process described in step (2), the crystallization conditions include: a crystallization temperature of 130-180℃ and a crystallization time of 24-72h.

7. The catalyst according to claim 1, characterized in that, The drying temperature in steps (1) and (2) is 100-120℃ and the drying time is 12-24h; the calcination temperature in step (3) is 350-550℃ and the calcination time is 2-6h.

8. A method for hydrogenating acetophenone to 1-phenylethanol, characterized in that, A solution containing acetophenone and hydrogen are mixed and passed through a reactor, where they react with the catalyst described in any one of claims 1-7 to produce 1-phenylethanol.

9. The method according to claim 8, characterized in that, The specific conditions for the contact reaction include: a reaction temperature of 80-130℃; a reaction pressure of 1.5-2.6 MPa; an H2 / acetophenone molar ratio of (3-20):1; and an acetophenone liquid hourly space velocity of 0.4-0.6 g·g⁻¹. cat -1 ·h -1 .

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