Liquid-phase hydrogenation catalyst as well as preparation method and application method thereof

Abstract

The invention discloses a liquid-phase hydrogenation catalyst as well as a preparation method and an application method thereof, and belongs to the technical field of catalysts. The preparation method comprises the following steps: (1) mixing aluminum hydroxide dry glue with pseudo-boehmite, adding an auxiliary agent and water, kneading, carrying out extrusion molding, naturally airing, and roasting at 860-910 DEG C for 2-3 hours to obtain a carrier; (2) mixing platinum salt, palladium salt and water according to the molar ratio of platinum to palladium of 1: 1.83, and dissolving to prepare a platinum-palladium salt aqueous solution; and (3) dipping the carrier in a platinum-palladium salt aqueous solution for 30-45 minutes, drying for 1.5-2 hours at 110-125 DEG C, and roasting for 2-3 hours at 420-450 DEG C. The catalyst is prepared from the following active components: 0.2-0.3 wt% of platinum and 0.1-0.25 wt% of palladium. The liquid-phase hydrogenation catalyst disclosed by the invention has the hydrogenation conversion rate of a raw material isooctenal as high as 99% or above and the selectivity of a product isooctenal as high as 98% or above, and can be applied to preparation of isooctenal by liquid-phase hydrogenation of isooctenal.

Description

Technical Field

[0001] The invention discloses a liquid phase hydrogenation catalyst and a preparation method and an application method thereof, belonging to the technical field of catalysts. Background Art

[0002] Isooctyl aldehyde is an important chemical intermediate product, which can be used to produce isooctyl acid or isooctyl alcohol, and is also a flavor additive for soaps and detergents. At present, the industrial preparation of isooctyl aldehyde mainly includes propylene carbonyl synthesis method and acetaldehyde aldol condensation method.

[0003] The key to the selective hydrogenation of isooctyl aldehyde to isooctyl aldehyde lies in the catalyst. From the perspective of economy, the reaction conversion rate is high and the selectivity is good, and the hydrogenation reaction occurs at the carbon-carbon double bond instead of the carbonyl group. Precious metals are common active components of selective hydrogenation.

[0004] For example, US Pat. No. 3,903,171A uses palladium, platinum or ruthenium catalysts, aluminum oxide, SiO2 or silica gel carriers, and has harsh process conditions, high pressure and low isooctene aldehyde liquid space velocity.

[0005] US5756856 uses a catalyst with a palladium content of 0.5% and the remainder being alumina, and adopts a method of large-scale circulation of materials after hydrogenation to dilute the raw materials that need hydrogenation. su1728217A1 uses a catalyst with 0.1-2.0wt.% palladium loaded on alumina. In order to improve the stability of the catalyst and the quality of the target product, butyl isobutyrate or isobutyl butyrate is used as a diluent. Li Zheng (2-ethylhexenal liquid phase hydrogenation to 2-ethylhexenal [J]. Jilin Chemical Technology, 1993 (04): 38-41) The research results are: Pd / γ-Al2O3 catalyst, hydrogen-aldehyde ratio 2.6:1-5.2:1, temperature 85-95℃, pressure 2450kPa, octenal liquid space velocity 0.15-0.30h -1 , using the hydrogenation product as solvent, the circulation ratio is 3.40:1-3.80:1, and the isooctylaldehyde production capacity is 0.2g isooctylaldehyde / (gcat·h). The research results of Diaoxiang (Research on the Synthesis Process of 2-Ethylhexanal [J]. Journal of Shandong University of Technology: Natural Science Edition, 2008, 22(1):4) are: QSH-01 catalyst (palladium-alumina catalyst), hydrogen ratio 4-6, temperature 130-150℃, pressure 1.5-2.0MPa, octenal liquid space velocity 0.4-0.8h -1 , using crude isooctylaldehyde circulation, the circulation ratio is 1: 1-3: 1. The process methods of the above two patents and two documents all adopt the method of partial product circulation, which increases the equipment investment and operation cost to varying degrees.

[0006] In summary, the current technical issues that need to be addressed are developing a process for producing isooctyl aldehyde by liquid-phase hydrogenation of octenal with low operating costs and developing a high-activity and high-selectivity catalyst to match it. Summary of the invention

[0007] The technical problem to be solved by the present invention is to overcome the deficiencies of the prior art and provide a liquid phase hydrogenation catalyst and a preparation method and an application method thereof. The prepared liquid phase hydrogenation catalyst has a high hydrogenation conversion rate for the raw material isooctyl aldehyde, which can reach more than 99%, and a high selectivity for the product isooctyl aldehyde, which can reach more than 98%, and can be applied to the preparation of isooctyl aldehyde by liquid phase selective hydrogenation of isooctyl aldehyde.

[0008] The technical solution of the method adopted by the present invention to solve the technical problem is: the preparation method of the liquid phase hydrogenation catalyst comprises the following steps: 1) Mix aluminum hydroxide dry glue and pseudo-boehmite, add additives and water, knead, extrude into strips, dry naturally, and roast at 860-910℃ for 2-3 hours to obtain a carrier; 2) using platinum salt, palladium salt and water, mixing and dissolving in a molar ratio of platinum to palladium of 1:1.8-2.0 to prepare a platinum-palladium salt aqueous solution; 3) Weigh the carrier, impregnate it with a platinum-palladium salt aqueous solution for 30-45 minutes, dry it at 110-125°C for 1.5-2 hours, and calcine it at 420-450°C for 2-3 hours to obtain the catalyst.

[0009] Step 1) The weight ratio of the aluminum hydroxide dry gel to the pseudo-boehmite is 65-80:20-35.

[0010] The specific operation of adding the auxiliary agent and water in step 1) is as follows: based on the sum of the weight of the aluminum hydroxide dry gel and the pseudo-boehmite as 100%, 8-15 wt% of the auxiliary agent and 80 wt% of water are added.

[0011] Step 1) The auxiliary agent is at least two of sesbania powder, citric acid, nitric acid and cellulose.

[0012] In step 2), the platinum salt is platinum nitrate, and the palladium salt is palladium nitrate; in step 2), the platinum content in the platinum nitrate is 58 wt%, and the palladium content in the palladium nitrate is 39.5 wt%.

[0013] The active components of the liquid phase hydrogenation catalyst are as follows: the content of platinum is 0.2 wt%-0.3 wt% calculated as elemental platinum, and the content of palladium is 0.1 wt%-0.25 wt% calculated as elemental palladium.

[0014] The carrier of the liquid phase hydrogenation catalyst comprises a γ-Al2O3 phase and a θ-Al2O3 phase, wherein the γ-Al2O3 is ≥ 80wt%; the pore volume of the catalyst is 0.42-0.46cm 3 / g, specific surface area 150-160m 2 / g, average pore radius 9.50-10.95nm, bulk density 0.60-0.65kg / L.

[0015] The invention discloses an application method of the liquid phase hydrogenation catalyst and a method for preparing isooctyl aldehyde by liquid phase hydrogenation using isooctyl aldehyde as a raw material under the catalysis of the liquid phase hydrogenation catalyst.

[0016] The application method of the liquid phase hydrogenation catalyst comprises the following steps: First, isooctenal is preheated to 50-150°C; then, isooctenal and hydrogen are used as raw materials, and isooctenal is subjected to liquid phase hydrogenation reaction and gas-liquid separation under the catalysis of the liquid phase hydrogenation catalyst to obtain isooctenal; the reaction temperature of the liquid phase hydrogenation reaction is 70-180°C, the reaction pressure is 1.5-2.6MPa, and the isooctenal liquid space velocity is 0.3-6.0h -1 , the molar ratio of hydrogen to isooctene aldehyde is 1.8-5.0:1.

[0017] The application method of the liquid phase hydrogenation catalyst also includes the following steps: subjecting the obtained isooctyl aldehyde to heat exchange, cooling and separation to improve the purity and obtain refined isooctyl aldehyde. The refined isooctyl aldehyde can be directly sold as a product.

[0018] The liquid phase hydrogenation reaction is carried out in a reactor, which is a cylindrical reactor; the height-to-diameter ratio of the catalyst bed in the reactor is 2-6, and the spacing between the distributors of each layer is 25-35 cm.

[0019] Step 1) The aluminum hydroxide dry glue is a carbonized aluminum hydroxide dry glue. Preferably, the aluminum hydroxide dry glue is a carbonized aluminum hydroxide dry glue produced by Shandong Hengyi Chemical Technology Co., Ltd.; and the pseudo-boehmite is produced by Shandong Hengyi Chemical Technology Co., Ltd.

[0020] Step 2) The platinum nitrate and palladium nitrate are both products of Sinopharm Group Shanghai Co., Ltd.

[0021] Step 3) The impregnation is carried out by volume impregnation method, which is a well-known impregnation method. The required amount of impregnation liquid is calculated according to the water absorption rate of the carrier and the platinum content and palladium content of the prepared catalyst.

[0022] The catalyst is a sphere with a particle size of 1-2 mm, or a column-shaped catalyst with a diameter of 1-2 mm and a length of 0.5-2 cm.

[0023] Preferably, the columnar strip catalyst is in the shape of a columnar strip with a circular, clover-shaped or four-leaf-clover cross section.

[0024] The present invention is described as follows: 1. The reaction of octenal hydrogenation to produce isooctyl aldehyde is a highly exothermic reaction. The experimental phenomenon is: the impurity content caused by side reactions will increase with the increase of catalyst bed temperature. Excess hydrogen will cause over-hydrogenation to produce isooctyl alcohol and fusel alcohols. Insufficient hydrogen will cause low octenal hydrogenation rate, affecting reaction efficiency and economy.

[0025] 2. With the help of a cylindrical reactor, 1) a smaller height-to-diameter ratio is used to allow the material to pass through the catalyst bed quickly to prevent the catalyst bed temperature from being too high; 2) the raw materials and hydrogen pass through the multi-layered distributor, and the temperature of the material entering later is significantly lower than the material that has already reacted, which can reduce the temperature of the material in the reactor, thereby controlling the reaction to an appropriate degree and obtaining the target product mainly composed of isooctylaldehyde. When the reaction temperature is greater than 138°C, the side reactions are more active and the selectivity of isooctylaldehyde tends to decrease.

[0026] 3. Through a series of experiments, it is believed that "high activity" should not be pursued in this reaction. The purpose can be achieved as long as the catalyst has appropriate activity. The role of the catalyst in this reaction process is important. The present invention adopts a newly developed platinum-palladium catalyst. By adjusting the catalyst activity, appropriate activity and high selectivity are achieved, avoiding the dilution and circulation of aldehyde materials in the prior art, which helps to reduce operating costs.

[0027] Compared with the prior art, the present invention has the following beneficial effects: 1. The liquid phase hydrogenation catalyst of the present invention adopts a newly developed platinum-palladium catalyst, and achieves suitable activity and high selectivity by adjusting the catalyst activity, avoiding the dilution and circulation of aldehyde materials in the prior art, which helps to reduce operating costs.

[0028] 2. Application of the liquid phase hydrogenation catalyst of the present invention. The present invention replaces the existing gas phase hydrogenation reactor with liquid phase hydrogenation. The energy consumption of the liquid phase hydrogenation process is lower than that of the gas phase hydrogenation. The process flow is reasonably designed and the process operation is simple. It can effectively reduce the energy consumption of the reaction process and ensure that the isooctylaldehyde product that meets the control index is obtained. When it is used for the liquid phase hydrogenation of octenal to produce isooctylaldehyde, the octenal hydrogenation conversion rate is ≥99.0%, and the isooctylaldehyde selectivity is ≥98%. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] Figure 1 It is a cross-sectional view of the reactor for liquid phase hydrogenation of the present invention.

[0030] Figure 2 yes Figure 1 Top view of the middle AA surface.

[0031] Among them: 1. Reactor; 2. Distributor; 3. Inert porcelain ball; 4. Isooctylaldehyde inlet pipe; 5. Programmable regulating valve. DETAILED DESCRIPTION

[0032] Reference Figure 1 The liquid phase hydrogenation reactor of the present invention comprises a reactor 1, the bottom of which is filled with inert porcelain balls 3; a multi-layer distributor 2 is arranged in the middle of the reactor 1, and the multi-layer distributor 2 is horizontally and parallelly distributed in the reactor 1; the interval between adjacent distributors 2 is 35 cm.

[0033] The liquid phase hydrogenation catalyst of the present invention is loaded in each layer of the distributor 2. The specific structure of the distributor 2 is conventional and commercially available.

[0034] Each layer of distributor 2 is connected to an isooctene aldehyde inlet pipe 4, and multiple isooctene aldehyde inlet pipes 4 are connected in parallel. Each isooctene aldehyde inlet pipe 4 is provided with a programmable regulating valve 5. This design can facilitate the individual control of the isooctene aldehyde added to each layer of distributor according to the liquid phase hydrogenation, and flexibly adjust the liquid phase hydrogenation reaction.

[0035] The present invention is further described below in conjunction with specific examples, wherein Example 1 is the best example. The comparative examples are designed to compare the effects of the examples.

[0036] Step 1) The aluminum hydroxide dry glue is produced by the carbonization process of Shandong Hengyi Chemical Technology Co., Ltd.; the pseudo-boehmite is produced by Shandong Hengyi Chemical Technology Co., Ltd.

[0037] Step 2) Platinum nitrate and palladium nitrate are both products of Sinopharm Group Shanghai Co., Ltd.

[0038] Example 1 The preparation method of the liquid phase hydrogenation catalyst of this embodiment comprises the following steps: 1) 75 parts of aluminum hydroxide dry glue obtained by carbonization method were mixed with 25 parts of pseudo-boehmite, and the mixture was measured as 100%, and 3 wt% of sesbania powder, 3 wt% of citric acid, 3 wt% of nitric acid, and 80 wt% of water were added, and the mixture was kneaded and extruded to obtain cylindrical bars with a diameter of 1.5 mm and a length of 0.5 cm. The cylindrical bars were naturally dried and calcined at 910°C for 2 hours to obtain a carrier, and the water absorption rate of the carrier was measured to be 46%; 2) platinum nitrate (platinum content 58%) and palladium nitrate (palladium content 39.5%) are mixed and dissolved in a molar ratio of platinum to palladium of 1:1.83 to prepare a platinum-palladium nitrate aqueous solution; 3) Weigh the carrier, impregnate it with platinum palladium nitrate aqueous solution for 30-45 minutes, dry it at 125°C for 2 hours, and calcine it at 450°C for 2 hours to obtain the catalyst. The catalyst is numbered PtPd-1.

[0039] Catalyst quality inspection results: platinum content is 0.201 wt%, palladium content is 0.202 wt%, the phase is mainly γ-Al2O3 phase (more than 80%), containing a small amount of θ-Al2O3 phase, pore volume is 0.43cm 3 / g, specific surface area 158.9m 2 / g, average pore radius is 9.57nm, and bulk density is 0.61kg / L.

[0040] In the application method of the catalyst in this embodiment, the reactor used is a cylindrical reactor, the height-to-diameter ratio of the catalyst bed is 4, the spacing between the distributors of each layer is 35 cm, and the catalyst PtPd-1 is loaded.

[0041] The application method of the catalyst in this embodiment comprises the following steps: After the temperature of the octenal raw material is raised to 90°C, it is mixed with hydrogen and enters from the distributor. By controlling the material flow of each distributor, the reactor outlet temperature is controlled at 125°C. The reaction pressure is controlled at 1.5MPa by back pressure, and the liquid space velocity of the raw material octenal is 6.0h -1 , the molar ratio of hydrogen:octenal is 4.0; The product composition was analyzed by chromatography, and the 2-ethylhexanal hydrogenation conversion rate was 99.39%, and the 2-ethylhexanal selectivity was 98.65%.

[0042] Example 2 The preparation method of the liquid phase hydrogenation catalyst of this embodiment comprises the following steps: 1) 65 parts of aluminum hydroxide dry glue obtained by carbonization method were mixed with 35 parts of pseudo-boehmite, and the mixture was measured as 100%, and 3 wt% of sesbania powder, 3 wt% of citric acid, 3 wt% of nitric acid, and 65 wt% of water were added, and the mixture was kneaded and extruded to obtain φ1.5 mm spheres, which were naturally dried and calcined at 860°C for 3 hours to obtain a carrier, and the water absorption rate of the carrier was measured to be 51%; 2) platinum nitrate (platinum content 58%) and palladium nitrate (palladium content 39.5%) are mixed and dissolved in a molar ratio of platinum to palladium of 1:1.83 to prepare a platinum-palladium nitrate aqueous solution; 3) Weigh the carrier, impregnate it with platinum palladium nitrate aqueous solution for 45 minutes, dry it at 110°C for 2 hours, and calcine it at 420°C for 3 hours to obtain the catalyst. The catalyst is numbered PtPd-2.

[0043] Catalyst quality inspection results: platinum content is 0.297 wt%, palladium content is 0.104 wt%, the phase is mainly γ-Al2O3 phase (more than 90%), containing a small amount of θ-Al2O3 phase, pore volume is 0.46cm 3 / g, specific surface area 151.3m 2 / g, average pore radius 10.91nm, bulk density 0.65kg / L.

[0044] The application method of the catalyst in this embodiment uses a cylindrical reactor with a catalyst bed having a height-to-diameter ratio of 1, a spacing of 25 cm between distributors at each layer, and is loaded with the catalyst PtPd-2.

[0045] The application method of the catalyst in this embodiment comprises the following steps: After the temperature of the octenal raw material is raised to 100°C, it is mixed with hydrogen and enters from the distributor. By controlling the material flow of each distributor, the reactor outlet temperature is controlled at 130°C. The reaction pressure is controlled at 2.5MPa by back pressure, and the liquid space velocity of the raw material octenal is 6.0h -1 , the molar ratio of hydrogen:octenal is 3.0; The product composition was analyzed by chromatography, and the 2-ethylhexanal hydrogenation conversion rate was 99.20%, and the 2-ethylhexanal selectivity was 98.82%.

[0046] Example 3 The preparation method of the liquid phase hydrogenation catalyst of this embodiment comprises the following steps: 1) 80 parts of aluminum hydroxide dry glue obtained by carbonization method and 20 parts of pseudo-boehmite (both produced by Shandong Hengyi Chemical Technology Co., Ltd.) were mixed, and the mixture was measured as 100%, and 3 wt% of sesbania powder, 3 wt% of citric acid, 3 wt% of nitric acid, and 65 wt% of water were added, kneaded, extruded, and φ1.5 mm spheres were obtained, naturally dried, and calcined at 910°C for 2 hours to obtain a carrier, and the water absorption rate of the carrier was measured to be 52%; 2) platinum nitrate (platinum content 58%) and palladium nitrate (palladium content 39.5%) are mixed and dissolved in a molar ratio of platinum to palladium of 1:1.83 to prepare a platinum-palladium nitrate aqueous solution; 3) Weigh the carrier, impregnate it with platinum palladium nitrate aqueous solution for 40 minutes, dry it at 120°C for 2 hours, and calcine it at 430°C for 3 hours to obtain the catalyst. The catalyst is numbered PtPd-3.

[0047] Catalyst quality inspection results: platinum content is 0.253 wt%, palladium content is 0.246 wt%, the phase is mainly γ-Al2O3 phase (more than 85%), containing a small amount of θ-Al2O3 phase, pore volume is 0.44cm 3 / g, specific surface area 155.7m 2 / g, average pore radius 10.11nm, bulk density 0.63kg / L.

[0048] The application method of the catalyst in this embodiment uses a cylindrical reactor with a catalyst bed having a height-to-diameter ratio of 1, a spacing of 30 cm between distributors of each layer, and is loaded with the catalyst PtPd-3.

[0049] The application method of the catalyst in this embodiment comprises the following steps: After the temperature of the octenal raw material is raised to 120°C, it is mixed with hydrogen and enters from the distributor. By controlling the material flow of each distributor, the reactor outlet temperature is controlled at 180°C. The reaction pressure is controlled at 2.5MPa by back pressure, and the liquid space velocity of the raw material octenal is 6.0h -1 , the molar ratio of hydrogen to octenal is 5.0:1; The product composition was analyzed by chromatography, and the 2-ethylhexanal hydrogenation conversion rate was 99.48, and the 2-ethylhexanal selectivity was 98.67%.

[0050] Comparative Example 1 The aluminum hydroxide dry gel in Example 1 was replaced with a product produced by the Shandong Branch of Aluminum Corporation of China using a sulfuric acid method, while other formula proportions and preparation process remained unchanged, to obtain a sample.

[0051] Comparative Example 2 The aluminum hydroxide dry gel in Example 2 was replaced with a product produced by the Shandong Branch of Aluminum Corporation of China using a sulfuric acid process, and other formula proportions and preparation processes remained unchanged to obtain a sample.

[0052] Comparative Example 3 According to the conditions of Example 3, the sample evaluations of Comparative Example 1 and Comparative Example 2 were completed respectively.

[0053] The evaluation results of the sample of Comparative Example 1: the hydrogenation rate of isooctyl aldehyde is 98.71%, and the selectivity of isooctyl aldehyde is 97.37%.

[0054] The evaluation results of the sample of Comparative Example 2: the hydrogenation rate of isooctyl aldehyde is 98.93%, and the selectivity of isooctyl aldehyde is 98.33%.

[0055] Comparative Example 3 The information about the catalyst used in US5756856 (0.5% Pd / Al2O3, Engelhard) is incomplete.

[0056] The carrier of Example 1 was used and loaded with 0.5 wt% Pd. The catalyst was evaluated under the conditions of Example 3. The evaluation results showed that the isooctyl aldehyde hydrogenation rate was 94.87% and the isooctyl aldehyde selectivity was 94.62%.

[0057] Comparative Example 4 The catalyst QSH-01 used by the author Diao Xiang in the published article is the result of research and development by our unit. It corresponds to patent CN1084222C and belongs to the field of selective hydrogenation of C4 alkylation raw materials. It is used for selective hydrogenation of butadiene in C4 raw materials into C4 olefins and has been industrially applied in dozens of equipment at home and abroad.

[0058] The evaluation was carried out using QSH-01 according to the conditions of Example 3. The evaluation results showed that the isooctyl aldehyde hydrogenation rate was 94.11% and the isooctyl aldehyde selectivity was 95.45%.

[0059] The above is only a preferred embodiment of the present invention, and does not limit the present invention in other forms. Any technician familiar with the profession may use the above disclosed technical content to change or modify it into an equivalent embodiment with equivalent changes. However, any simple modification, equivalent change and modification made to the above embodiment according to the technical essence of the present invention without departing from the technical solution of the present invention still belongs to the protection scope of the technical solution of the present invention.

Claims

1. A method for preparing a liquid phase hydrogenation catalyst, characterized in that: The steps include: 1) Mix aluminum hydroxide dry glue and pseudo-boehmite, add additives and water, knead, extrude into strips, dry naturally, and roast at 860-910℃ for 2-3 hours to obtain a carrier; 2) using platinum salt, palladium salt and water, mixing and dissolving in a molar ratio of platinum to palladium of 1:1.8-2.0 to prepare a platinum-palladium salt aqueous solution; 3) Weigh the carrier, impregnate it with a platinum-palladium salt aqueous solution for 30-45 minutes, dry it at 110-125°C for 1.5-2 hours, and calcine it at 420-450°C for 2-3 hours to obtain the catalyst.

2. The method for preparing a liquid phase hydrogenation catalyst according to claim 1, characterized in that: Step 1) The weight ratio of the aluminum hydroxide dry gel to the pseudo-boehmite is 65-80:20-35.

3. The method for preparing a liquid phase hydrogenation catalyst according to claim 1, characterized in that: The specific operation of adding the auxiliary agent and water in step 1) is as follows: based on the sum of the weight of the aluminum hydroxide dry gel and the pseudo-boehmite as 100%, 8-15 wt% of the auxiliary agent and 80 wt% of water are added.

4. The method for preparing a liquid phase hydrogenation catalyst according to claim 1, characterized in that: Step 1) The auxiliary agent is at least two of sesbania powder, citric acid, nitric acid and cellulose.

5. The method for preparing a liquid phase hydrogenation catalyst according to claim 1, characterized in that: In step 2), the platinum salt is platinum nitrate, and the palladium salt is palladium nitrate; in step 2), the platinum content in the platinum nitrate is 58 wt %, and the palladium content in the palladium nitrate is 39.5 wt %.

6. The liquid phase hydrogenation catalyst prepared by the preparation method according to any one of claims 1 to 5, characterized in that: The active components of the catalyst are: the platinum content is 0.2 wt%-0.3 wt% calculated as elemental platinum, and the palladium content is 0.1 wt%-0.25 wt% calculated as elemental palladium.

7. The liquid phase hydrogenation catalyst according to claim 6, characterized in that: The catalyst carrier comprises a γ-Al2O3 phase and a θ-Al2O3 phase, wherein the γ-Al2O3 is ≥ 80 wt%; the catalyst has a pore volume of 0.42-0.46 cm 3 / g, specific surface area 150-160m 2 / g, average pore radius 9.50-10.95nm, bulk density 0.60-0.65kg / L.

8. A method for applying a liquid phase hydrogenation catalyst, characterized in that: A method for preparing isooctyl aldehyde by liquid phase hydrogenation using isooctyl aldehyde as a raw material under the catalysis of the catalyst described in any one of claims 1 to 6.

9. The method for using a liquid phase hydrogenation catalyst according to claim 8, characterized in that: The steps include: First, isooctenal is preheated to 50-150° C.; then, isooctenal and hydrogen are used as raw materials, and the isooctenal is subjected to liquid phase hydrogenation reaction and gas-liquid separation under the catalysis of the catalyst described in any one of claims 1 to 6 to obtain isooctenal; the reaction temperature of the liquid phase hydrogenation reaction is 70-180° C., the reaction pressure is 1.5-2.6 MPa, and the isooctenal liquid space velocity is 0.3-6.0 h -1 , the molar ratio of hydrogen to isooctene aldehyde is 1.8-5.0:

1.

10. The method for using a liquid phase hydrogenation catalyst according to claim 9, characterized in that: The liquid phase hydrogenation reaction is carried out in a reactor, which is a cylindrical reactor; the height-to-diameter ratio of the catalyst bed in the reactor is 2-6, and the spacing between the distributors of each layer is 25-35 cm.

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