A 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst and its preparation method and application

Abstract

The present invention provides a kind of 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst and its preparation method and application, relating to the field of catalysts; The catalyst obtained is with ZnO / SiO2 as carrier, and the Zn / Si molar ratio in the carrier is 1: 2-5, with Cu and Ni as active ingredients, and by mass percentage, the carrier content is 70-80%, the active component CuO content is 15-20%, and the NiO content is 5-10%. During preparation, silica sol and zinc nitrate are mixed and added to the reactor with stirring, alkali liquor is quickly added, and then the nitrate solution of active component is mixed and added thereto, and after neutralization, it is washed, filtered, dried, granulated, roasted, and finally sheeted into a ring type to obtain a catalyst. The catalyst obtained by the present invention, the isononanal conversion rate reaches more than 99%, and the isononanol selectivity reaches more than 99%, with excellent activity, selectivity and stability, which is conducive to industrial application promotion.

Description

Technical Field

[0001] The present invention relates to the technical field of catalysts, and in particular to a 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst, a preparation method and an application thereof. Background Art

[0002] 3,5,5-trimethyl-1-hexanol, molecular formula is C9H 20 O, with a relative molecular mass of 144.25, is primarily used in reaction with phthalic anhydride to produce diisononyl phthalate (DINP), a plasticizer for PVC. As the market gradually recognizes the safety of DINP, demand for DINP, an environmentally friendly alternative to DOP, is expected to grow rapidly, effectively meeting consumer demand and driving a rapid increase in isononanol consumption.

[0003] Currently, 3,5,5-trimethyl-1-hexanol is primarily produced through aldehyde hydrogenation, which involves both gas-phase and liquid-phase processes. Compared to gas-phase aldehyde hydrogenation, liquid-phase processes offer advantages such as higher product quality, smaller reactor size, and lower energy consumption. Existing liquid-phase aldehyde hydrogenation catalysts often use alumina, silica, zirconium oxide, magnesium oxide, zinc oxide, activated carbon, and other supports. However, the acidity or alkalinity of the support significantly influences the selectivity of the reaction, creating a trade-off between the activity and selectivity of liquid-phase hydrogenation catalysts. Patent 201911220649.3 discloses an aldehyde hydrogenation catalyst used to prepare 3,5,5-trimethyl-1-hexanol, wherein the main components are Ni, Mg, and Na as active components, with one or more of Co, Ca, Sr, and Ba metal elements as auxiliary agents, and one or more of alumina, silica, and diatomaceous earth treated with ammonia as carriers; Patent 202010481547.3 discloses a method for preparing isononanol, wherein the catalyst includes one or a mixture of nickel, copper, platinum, or palladium.

[0004] Although the prior art has proposed catalysts for preparing 3,5,5-trimethyl-1-hexanol, these catalysts are all conventional aldehyde hydrogenation catalysts. When used, the conversion rate of 3,5,5-trimethyl-1-hexanal and the selectivity for 3,5,5-trimethyl-1-hexanol are both relatively low, making them unsuitable for industrial promotion. Summary of the Invention

[0005] The present invention aims to provide a 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst, a preparation method, and an application thereof. The main features of the prepared catalyst are the use of a composite ZnO / SiO2 carrier and Cu and Ni as active ingredients. The catalyst can fully utilize the large specific surface area and suitable pore structure of the ZnO / SiO2 carrier, promote the dispersion of the active ingredients, and improve the shape selectivity of the product. It also anchors the active component Cu to prevent its migration during use, resulting in the growth of copper grains, thereby improving the activity, selectivity, and stability of the catalyst.

[0006] To achieve the above objectives, the present invention proposes the following technical solutions:

[0007] In a first aspect, the present invention discloses a method for preparing a 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst, comprising the following preparation steps:

[0008] 1) preparing a silicon-zinc mixed solution;

[0009] 2) adding alkali to the silicon-zinc mixture to prepare a ZnO / SiO2 carrier, wherein the Zn / Si molar ratio in the ZnO / SiO2 carrier is 1:2-5;

[0010] 3) mixing the ZnO / SiO2 carrier and the Cu-Ni mixed solution under stirring, and aging after the reaction to achieve the loading of active components of metal Ni and metal Cu on the ZnO / SiO2 carrier; wherein the Cu-Ni mixed solution is prepared by mixing a Cu salt and a Ni salt;

[0011] 4) filtering, washing, drying, granulating, and calcining the aged product, and finally adding water and a binder to form a ring-shaped sheet to obtain the liquid-phase hydrogenation catalyst;

[0012] The active components of metal Ni and metal Cu are attached to the ZnO / SiO2 carrier in the form of active component oxides, and the content of the ZnO / SiO2 carrier in the prepared liquid-phase hydrogenation catalyst is 70-80% by mass, the content of the active component CuO is 15-20%, and the content of NiO is 5-10%.

[0013] Furthermore, the specific process of preparing the silicon-zinc mixed solution in step 1) is: uniformly mixing the silica sol solution and the zinc nitrate solution under stirring conditions.

[0014] Furthermore, the base in step 2) is one of NaOH, KOH, Na2CO3, and K2CO3.

[0015] Furthermore, the time for adding the silicon-zinc mixed solution after the alkali is prepared into a solution is 10-30 minutes.

[0016] Furthermore, in step 3), the Cu salt and the Ni salt are both nitrates, the mixing reaction temperature of the ZnO / SiO2 carrier and the Cu-Ni mixed solution is 55-75°C, the reaction time is 20-40 min, and the aging time is 30-60 min.

[0017] Furthermore, in step 4), the calcination temperature of the aged product is 350-450° C., and the calcination time is 2-6 hours.

[0018] In a second aspect, the present invention discloses a liquid phase hydrogenation catalyst prepared by the above-mentioned preparation method of 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst; the specific surface area of ​​the liquid phase hydrogenation catalyst is 215-400m 2 / g, average pore diameter 25-45nm, pore volume 0.3-0.5cm 3 / g.

[0019] In a third aspect, the present invention discloses an application of the above-mentioned 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst in the aldehyde hydrogenation to alcohol reaction.

[0020] Furthermore, when the liquid phase hydrogenation catalyst is used in the liquid phase hydrogenation of 3,5,5-trimethyl-1-hexanal to 3,5,5-trimethyl-1-hexanol, the reaction conditions are: reaction temperature 160-240°C, reaction pressure 4-6 MPa, hydrogen-to-oil ratio 300-800:1, 3,5,5-trimethyl-1-hexanal liquid hourly space velocity 0.4-1.2h -1 .

[0021] It can be seen from the above technical solutions that the technical solutions of the present invention have the following beneficial effects:

[0022] The present invention provides a 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst, its preparation method, and application, relating to the field of catalysts. During preparation, a silicon-zinc mixed solution is prepared by mixing silica sol with a zinc nitrate solution. This mixed solution is reacted with an alkali to form a carrier oxide, while the carrier surface is etched to produce a ZnO / SiO2 carrier. The ZnO / SiO2 carrier is then impregnated with a salt corresponding to the active ingredient and calcined to obtain a liquid-phase hydrogenation catalyst. The present invention's design allows the catalyst to have a large specific surface area and a suitable pore structure while fully utilizing the positioning function of ZnO to anchor the active component Cu, thereby ensuring the catalyst's activity, selectivity, and stability. Specific advantages include the following:

[0023] (1) The present invention uses a ZnO / SiO2 composite carrier, which has a large specific surface area and a suitable pore structure. It promotes the dispersion of the active components and is conducive to improving the shape selectivity of the product. It also anchors the active component Cu, preventing its migration during use and causing the growth of copper grains.

[0024] (2) The present invention uses Cu and Ni bimetallics as active components to compensate for the low conversion rate of Cu-based hydrogenation catalysts and balance the catalyst conversion rate and selectivity;

[0025] (3) The technical method adopted by the present invention is simple, conducive to industrial application and promotion, and has important social and economic significance.

[0026] It should be appreciated that all combinations of the foregoing concepts, as well as additional concepts described in greater detail below, to the extent such concepts are not mutually inconsistent, can be considered to be part of the inventive subject matter of this disclosure.

[0027] The foregoing and other aspects, embodiments, and features of the present invention will be more fully understood from the following description in conjunction with the accompanying drawings. Other additional aspects of the present invention, such as features and / or beneficial effects of the exemplary embodiments, will become apparent from the following description or through practice of specific embodiments according to the present invention. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] The accompanying drawings are not drawn to scale. In the accompanying drawings, each identical or nearly identical component shown in various figures may be represented by the same reference numeral. For clarity, not every component is labeled in every figure. Embodiments of various aspects of the present invention will now be described by way of example with reference to the accompanying drawings, in which:

[0029] Figure 1 The present invention is a flow chart for preparing the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst. DETAILED DESCRIPTION

[0030] In order to make the purpose, technical solutions and advantages of the embodiments of the present invention clearer, the technical solutions of the embodiments of the present invention will be clearly and completely described below in conjunction with the drawings of the embodiments of the present invention. Obviously, the described embodiments are part of the embodiments of the present invention, not all of the embodiments. Based on the described embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention. Unless otherwise defined, the technical terms or scientific terms used herein should be the common meanings understood by people with ordinary skills in the field to which the present invention belongs.

[0031] The words “first”, “second” and similar words used in the patent application specification and claims of the present invention do not indicate any order, quantity or importance, but are only used to distinguish different components. Similarly, unless the context clearly indicates otherwise, the singular forms of “a”, “an” or “the” and similar words do not indicate a quantity limitation, but rather indicate the presence of at least one. Words such as “include” or “comprise” mean that the elements or objects appearing before “include” or “comprises” cover the features, wholes, steps, operations, elements and / or components listed after “include” or “comprises”, and do not exclude the existence or addition of one or more other features, wholes, steps, operations, elements, components and / or their collections. “Up”, “down”, “left”, “right” and the like are only used to indicate relative positional relationships. When the absolute position of the described object changes, the relative positional relationship may also change accordingly.

[0032] The consumption of isononanol is increasing, while domestic isononanol plasticizers currently rely mainly on imports, with extremely low domestic production, and the key technologies for producing isononanol are also from foreign countries. Prior art reports show that the catalyst for preparing 3,5,5-trimethyl-1-hexanol is a conventional aldehyde hydrogenation catalyst. When used, the conversion rate of 3,5,5-trimethyl-1-hexanal and the selectivity for 3,5,5-trimethyl-1-hexanal are both low, making them unsuitable for industrial promotion. The present invention aims to address the shortcomings of existing catalysts and propose a 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst for use in aldehyde hydrogenation to alcohol reactions and a preparation method thereof. The catalyst not only has excellent activity and stability when used, but also has high selectivity for isononanol.

[0033] Specifically, the preparation method of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst disclosed in the present invention is as follows: Figure 1As shown, the method comprises the following preparation steps: S1, preparing a silicon-zinc mixed solution; specifically, uniformly mixing a silica sol solution and a zinc nitrate solution under stirring conditions to obtain a mixed solution; S2, adding an alkali to the silicon-zinc mixed solution to obtain a ZnO / SiO2 carrier, wherein the Zn / Si molar ratio in the ZnO / SiO2 carrier is 1:2-5; wherein the alkali is selected from one of NaOH, KOH, Na2CO3, and K2CO3, and the concentration can be selected from 1-2 mol / L, and the time for adding the silicon-zinc mixed solution is controlled to be 10-30 min; S3, mixing the ZnO / SiO2 carrier and the Cu-Ni mixed solution under stirring, and after the reaction is completed Aging is performed to achieve the loading of active ingredients of metal Ni and metal Cu on the ZnO / SiO2 carrier; wherein, the Cu-Ni mixed solution is prepared by mixing Cu salt and Ni salt, both of which are nitrates, and the mixing reaction temperature of the ZnO / SiO2 carrier and the Cu-Ni mixed solution is 55-75°C, the reaction time is 20-40min, and the aging time is 30-60min; S4, the aged product is filtered, washed, dried, granulated, and calcined, and finally water and a binder are added to form sheets into rings to obtain the liquid phase hydrogenation catalyst; optionally, the calcination temperature is 350-450°C, and the calcination time is 2-6h.

[0034] In step S3, the active components of metal Ni and metal Cu are attached to the ZnO / SiO2 carrier in the form of active component oxides, and the content of the ZnO / SiO2 carrier in the prepared liquid phase hydrogenation catalyst is 70-80%, the content of the active component CuO is 15-20%, and the content of NiO is 5-10%. Finally, the specific surface area of ​​the liquid phase hydrogenation catalyst is 215-400m 2 / g, average pore diameter 25-45nm, pore volume 0.3-0.5cm 3 / g, that is, from the perspective of the catalyst microstructure, it has rich specific surface area and suitable pore structure.

[0035] The 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst disclosed in the present invention, as well as its preparation method and application, are further specifically introduced below in conjunction with specific examples.

[0036] Example 1

[0037] The molar ratio of SiO2:ZnO is 3:1. Weigh 240g of 40% silica sol and 102.7g of zinc nitrate, add them to a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 200g of NaOH in 3L of deionized water to form a solution; weigh 294g of Cu(NO3) and 248.8g of Ni(NO3), dissolve them in 1L of deionized water to form a copper-nickel mixed solution; add alkali solution to the silicon-zinc mixed solution, control the addition time to 20min, to obtain a ZnO / SiO2 carrier; continue to add the copper-nickel mixed solution to the reactor, control the reaction time to 30min, and the reaction temperature to 60°C; after neutralization, raise the reaction temperature to 65°C and age for 40min; pour out the product, wash, filter, dry, granulate, and calcine at 360°C for 4h, finally add water and graphite to press into a ring shape to obtain catalyst C1.

[0038] Example 2

[0039] The molar ratio of SiO2:ZnO is 4:1. Weigh 261.7g of 40% silica sol and 82.4g of zinc nitrate, add them to a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 280g of KOH in 3L of deionized water to form a solution; weigh 294g of Cu(NO3) and 248.8g of Ni(NO3), dissolve them in 1L of deionized water to form a copper-nickel mixed solution; add alkali solution to the silicon-zinc mixed solution, control the addition time to 10min, and obtain a ZnO / SiO2 carrier; continue to add the copper-nickel mixed solution to the reactor, control the reaction time to 20min, and the reaction temperature to 65°C; after neutralization, raise the reaction temperature to 70°C and age for 60min; pour out the product, wash, filter, dry, granulate, and calcine at 400°C for 3h, and finally add water and graphite to press into a ring shape to obtain catalyst C2.

[0040] Example 3

[0041] The molar ratio of SiO2:ZnO is 2:1. Weigh 223.8g of 40% silica sol and 141.2g of zinc nitrate, add them to a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 265g of Na2CO3 in 3L of deionized water to form a solution; weigh 294g of Cu(NO3) and 224.4g of Ni(NO3), dissolve them in 1L of deionized water to form a copper-nickel mixed solution; add alkali solution to the silicon-zinc mixed solution, control the addition time to 10min, and obtain a ZnO / SiO2 carrier; continue to add the copper-nickel mixed solution to the reactor, control the reaction time to 40min, and the reaction temperature to 55°C; after neutralization, raise the reaction temperature to 60°C and age for 30min; pour out the product, wash, filter, dry, granulate, and calcine at 450°C for 2h, finally add water and graphite to press into a ring shape to obtain catalyst C3.

[0042] Example 4

[0043] The molar ratio of SiO2:ZnO is 5:1. 315g of 40% silica sol and 79.3g of zinc nitrate are weighed and added to a stirred reactor, and the mixture is evenly mixed to form a silicon-zinc mixed solution; 345g of K2CO3 is dissolved in 3L of deionized water to form a solution; 70.5g of Cu(NO3)2 and 24.4g of Ni(NO3)2 are weighed and dissolved in 1L of deionized water to form a copper-nickel mixed solution; alkali solution is added to the silicon-zinc mixed solution, and the addition time is controlled to 15min to obtain a ZnO / SiO2 carrier; the copper-nickel mixed solution is continued to be added to the reactor, and the reaction time is controlled to 20min and the reaction temperature is 75°C; after neutralization, the reaction temperature is raised to 80°C and aged for 45min; the product is poured out, washed, filtered, dried, granulated, and calcined at 350°C for 6h, and finally water and graphite are added to press into a ring shape to obtain catalyst C4.

[0044] Example 5

[0045] The molar ratio of SiO2:ZnO is 3:1. Weigh 257.5g of 40% silica sol and 110g of zinc nitrate, add them to a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 200g of NaOH in 3L of deionized water to form a solution; weigh 270.5g of Cu(NO3) and 248.8g of Ni(NO3), dissolve them in 1L of deionized water to form a copper-nickel mixed solution; add alkali solution to the silicon-zinc mixed solution, control the addition time to 18min, and obtain a ZnO / SiO2 carrier; continue to add the copper-nickel mixed solution to the reactor, control the reaction time to 25min, and the reaction temperature to 60℃; after neutralization, raise the reaction temperature to 65℃ and age for 30min; pour out the product, wash, filter, dry, granulate, and calcine at 380℃ for 4h, finally add water and graphite to press into a ring shape to obtain catalyst C5.

[0046] Example 6

[0047] The molar ratio of SiO2:ZnO is 3:1. Weigh 257.5g of 40% silica sol and 110g of zinc nitrate, add them to a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 280g of KOH in 3L of deionized water to form a solution; weigh 284.6g of Cu(NO3) and 234.2g of Ni(NO3), dissolve them in 1L of deionized water to form a copper-nickel mixed solution; add alkali solution to the silicon-zinc mixed solution, control the addition time to 25min, and obtain a ZnO / SiO2 carrier; continue to add the copper-nickel mixed solution to the reactor, control the reaction time to 40min, and the reaction temperature to 70℃; after neutralization, raise the reaction temperature to 75℃ and age for 40min; pour out the product, wash, filter, dry, granulate, and calcine at 400℃ for 4h, finally add water and graphite to press into a ring shape to obtain catalyst C6.

[0048] The only difference between Comparative Examples 1 and 2 and Example 1 is the addition time of the alkali solution to the silicon-zinc mixture for reaction; in Comparative Example 1, the alkali solution addition time is controlled to 5 minutes to obtain catalyst D1; in Comparative Example 2, the alkali solution addition time is controlled to 45 minutes to obtain catalyst D2.

[0049] Example 7

[0050] The catalyst was applied to the hydrogenation of 3,5,5,-trimethyl-1-hexanal to 3,5,5-trimethyl-1-hexanol.

[0051] Take 50ml of C1-C6 and D1-D2 catalysts and load them into a fixed bed reactor. Before the reaction, reduce the catalysts at 180℃, 0.2MPa, and 5% hydrogen concentration in nitrogen and hydrogen atmosphere for 12h. Then, heat to 200℃, reaction pressure 5MPa, 3,5,5,-trimethyl-1-hexanal, feed rate 0.6h -1 , H2 flow rate 250ml / min, the results are shown in Table 1.

[0052] Table 1 Activity evaluation results

[0053] Serial number <![CDATA[Specific surface area m 2 / g]]> Average pore size nm Isononanal conversion rate / % Isononanol selectivity / % C1 387 35 100 99.7 C2 210 25 100 99.5 C3 230 27 100 99.2 C4 354 31 100 99.1 C5 375 32 99.7 99.4 C6 400 45 99.8 99.7 D1 158 19 98.5 94.5 D2 185 54 97.4 93.2

[0054] From the data in Table 1, it can be seen that when the catalyst designed by the technical solution of the present invention is applied to the reaction of hydrogenating 3,5,5,-trimethyl-1-hexanal to 3,5,5,-trimethyl-1-hexanol, the conversion rate of isononanal reaches more than 99%, and the selectivity of isononanol reaches more than 99%, and the catalyst performance is good. The reasons for the poor catalytic performance of Comparative Examples 1 and 2 are: in Comparative Example 1, the alkali solution fails to fully contact and etch the ZnO / SiO2 support on the support surface, so that the support surface fails to fully form a suitable pore structure, the specific surface area is small, the active ingredient is unevenly dispersed on the support surface, and copper agglomerates, thereby reducing the conversion rate of isononanal and the selectivity of isononanol; in Comparative Example 2, when the alkali solution excessively contacts and etches the ZnO / SiO2 support, a larger pore structure is formed on the support surface, the specific surface area is significantly reduced, the pore size is increased, and the active ingredient is poorly dispersed on the support surface, thereby reducing the conversion rate of isononanal and the selectivity of isononanol.

[0055] The present invention further studies the effect of liquid-phase aldehyde hydrogenation reaction conditions on catalyst activity, that is, whether the catalyst has excellent stability, as shown in the following Examples 8-10 and Table 2.

[0056] Example 8

[0057] Take 50ml of C1 catalyst and load it into a fixed bed reactor. Before the reaction, reduce the catalyst at 180℃, 0.2MPa, 5% hydrogen concentration nitrogen and hydrogen atmosphere for 12h, then raise the temperature to 240℃, reaction pressure to 4MPa, feed 3,5,5,-trimethyl-1-hexanal for 0.8h. -1 , H2 flow rate 400ml / min, the results are shown in Table 2.

[0058] Example 9

[0059] Take 50ml of C1 catalyst and load it into a fixed bed reactor. Before the reaction, reduce the catalyst at 180℃, 0.2MPa, 5% hydrogen concentration nitrogen and hydrogen atmosphere for 12h, cool it to 160℃, reaction pressure 6MPa, 3,5,5,-trimethyl-1-hexanal feed rate 1.2h -1 , H2 flow rate 150ml / min, the results are shown in Table 2.

[0060] Example 10

[0061] Take 50ml of C1 catalyst and load it into a fixed bed reactor. Before the reaction, reduce the catalyst at 180℃, 0.2MPa, and 5% hydrogen concentration in nitrogen and hydrogen atmosphere for 12h. Maintain 180℃, reaction pressure 6MPa, and feed 3,5,5,-trimethyl-1-hexanal for 0.4h. -1 , H2 flow rate 150ml / min, the results are shown in Table 2.

[0062] Table 2 Effect of reaction conditions on activity evaluation results

[0063]

[0064]

[0065] As can be seen from Table 2, at a reaction temperature of 160°C-240°C and a reaction pressure of 4-6 MPa, the feed amount of 3,5,5,-trimethyl-1-hexanal is 0.4-1.2 h -1 The catalysts all showed excellent catalytic effects, had excellent stability, were suitable for industrial reaction conditions, and were conducive to industrial promotion.

[0066] While the present invention has been disclosed above with reference to preferred embodiments, this is not intended to limit the present invention. Persons skilled in the art will readily appreciate that various modifications and variations can be made without departing from the spirit and scope of the present invention. Therefore, the scope of protection of the present invention shall be determined by the claims.

Claims

1. A method for preparing a 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst, characterized in that: The liquid phase hydrogenation catalyst comprises the following preparation steps: 1) Prepare a silicon-zinc mixed solution; 2) adding an alkali to a silicon-zinc mixture to prepare a ZnO / SiO2 carrier, wherein the Zn / Si molar ratio in the ZnO / SiO2 carrier is 1:2-5; wherein the alkali is added to the silicon-zinc mixture after being prepared into a solution for 10-30 minutes; 3) mixing the ZnO / SiO2 support and the Cu-Ni mixed solution under stirring, and aging the mixture after the reaction to achieve loading of the active components, metallic Ni and metallic Cu, on the ZnO / SiO2 support; wherein the Cu-Ni mixed solution is prepared by mixing a Cu salt and a Ni salt; 4) The aged product is filtered, washed, dried, granulated, and calcined, and finally water and a binder are added to form a ring-shaped sheet to obtain the liquid-phase hydrogenation catalyst; The active components of metal Ni and metal Cu are attached to the ZnO / SiO2 carrier in the form of active component oxides, and the content of the ZnO / SiO2 carrier in the prepared liquid-phase hydrogenation catalyst is 70-80% by mass, the content of the active component CuO is 15-20%, and the content of NiO is 5-10%.

2. The preparation method of 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 1, characterized in that, The specific process of step 1) preparing the silicon-zinc mixed solution is: uniformly mixing the silica sol solution and the zinc nitrate solution under stirring conditions.

3. The preparation method of 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 1, characterized in that, The base in step 2) is one of NaOH, KOH, Na2CO3, and K2CO3.

4. The preparation method of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 1, wherein In the step 3), the Cu salt and the Ni salt are both nitrates, the mixing reaction temperature of the ZnO / SiO2 carrier and the Cu-Ni mixed solution is 55-75°C, the reaction time is 20-40 minutes, and the aging time is 30-60 minutes.

5. The preparation method of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 1, wherein The calcination temperature of the aged product in step 4) is 350-450° C., and the calcination time is 2-6 hours.

6. A liquid-phase hydrogenation catalyst prepared by the preparation method of the 3,5,5-trimethyl-1-hexanal liquid-phase hydrogenation catalyst according to any one of claims 1 to 5.

7. The 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 6, characterized in that The specific surface area of ​​the liquid phase hydrogenation catalyst is 215-400m 2 / g, average pore diameter 25-45nm, pore volume 0.3-0.5cm 3 / g.

8. Use of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 6 in an aldehyde hydrogenation to alcohol reaction.

9. Use of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 8 in an aldehyde hydrogenation to alcohol reaction, characterized in that: When the liquid phase hydrogenation catalyst is used in the liquid phase hydrogenation of 3,5,5-trimethyl-1-hexanal to 3,5,5-trimethyl-1-hexanol, the reaction conditions are: reaction temperature 160-240° C., reaction pressure 4-6 MPa, hydrogen-to-oil ratio 300-800:1, and 3,5,5-trimethyl-1-hexanal liquid hourly space velocity 0.4-1.2 h -1 .

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