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

Abstract

The invention discloses a 3, 5, 5-trimethyl-1-hexanal liquid phase hydrogenation catalyst as well as a preparation method and application thereof, and relates to the field of catalysts. The prepared catalyst takes ZnO / SiO2 as a carrier, the molar ratio of Zn / Si in the carrier is 1: (2-5), Cu and Ni are taken as active components, and the catalyst comprises the following components in percentage by mass: 70-80% of the carrier, 15-20% of the active component CuO and 5-10% of NiO. The preparation method comprises the following steps: uniformly mixing silica sol and zinc nitrate, adding the mixture into a reaction kettle with a stirring function, quickly adding alkali liquor, then mixing and adding a nitrate solution of the active component into the reaction kettle, after neutralization is finished, washing, filtering, drying, granulating, roasting, and finally flaking into a ring shape to obtain the catalyst. According to the prepared catalyst, the conversion rate of isononyl aldehyde reaches 99% or above, the selectivity of isononyl alcohol reaches 99% or above, and the catalyst has excellent activity, selectivity and stability and is beneficial to industrial application and popularization.

Description

Technical Field

[0001] The invention relates to the technical field of catalysts, and in particular to a 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst and a preparation method and 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 mainly used to react with phthalic anhydride to produce diisononyl phthalate (DINP), a plasticizer for PVC. As the market gradually recognizes the safety of DINP, the demand for DINP as an environmentally friendly substitute for DOP will grow rapidly, effectively meeting consumer demand while driving the rapid increase in the consumption of isononanol.

[0003] Currently, 3,5,5-trimethyl-1-hexanol is mainly obtained through aldehyde hydrogenation reaction, and the aldehyde hydrogenation reaction process includes two methods: gas phase method and liquid phase method. Compared with the gas phase aldehyde hydrogenation process, the liquid phase aldehyde hydrogenation process has the advantages of good product quality, small reactor volume and low energy consumption. In the existing technology, liquid phase aldehyde hydrogenation catalysts mostly use aluminum oxide, silicon oxide, zirconium oxide, magnesium oxide, zinc oxide, activated carbon, etc. as carriers, but the acidity and alkalinity of the carrier have a great influence on the selectivity of the reaction, and there is a contradiction between the activity and selectivity of the liquid phase hydrogenation catalyst. Patent 201911220649.3 discloses that the aldehyde hydrogenation catalyst used in the preparation of 3,5,5-trimethyl-1-hexanol mainly comprises Ni, Mg and Na as active components, 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 that the catalyst used in the method for preparing isononanol comprises 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, such catalysts are all conventional aldehyde hydrogenation catalysts. When used, the conversion rate of 3,5,5-trimethyl-1-hexanal and the selectivity of 3,5,5-trimethyl-1-hexanol are both low, and thus they are not suitable for industrial promotion. Summary of the invention

[0005] The purpose of the present invention is to provide a 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst and a preparation method and application thereof. The main characteristics of the prepared catalyst are that a composite ZnO / SiO2 carrier is used, and Cu and Ni are used as active components. The large specific surface area and suitable pore structure of the ZnO / SiO2 carrier can be fully utilized, and the dispersion of the active components is promoted while improving the shape selectivity of the product, and the active component Cu is anchored to avoid 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 object, 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 is completed, so as to load the active components 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;

[0011] 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;

[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 configured into a solution is 10-30 minutes.

[0016] Furthermore, in step 3), both the Cu salt and the Ni salt are nitrates, the mixed 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.

[0017] Furthermore, in the 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 liquid phase hydrogenation catalyst has a specific surface area of ​​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 reaction of aldehyde hydrogenation to produce alcohol.

[0020] Further, 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 4-6MPa, 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 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst provided by the present invention and its preparation method and application relate to the field of catalysts; during the preparation, a silicon-zinc mixed solution is prepared by mixing silica sol and zinc nitrate solution, and the carrier surface is etched to obtain a ZnO / SiO2 carrier while reacting with an alkali to generate a carrier oxide; then the ZnO / SiO2 carrier is impregnated with a salt corresponding to the active ingredient and calcined to obtain a liquid phase hydrogenation catalyst. The design scheme of the present invention enables the catalyst to obtain a large specific surface area and a suitable pore structure, while giving full play to the positioning effect of ZnO and anchoring the active component Cu, thereby ensuring the activity, selectivity and stability of the catalyst. The advantages include the following:

[0023] (1) The present invention adopts a ZnO / SiO2 composite carrier, which has a large specific surface area and a suitable pore structure, which promotes the dispersion of active components and is beneficial to improving the shape selectivity of the product, and anchors the active component Cu to prevent its migration during use and cause 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, may be considered to be part of the inventive subject matter of the present disclosure, provided such concepts are not mutually inconsistent.

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

[0028] The accompanying drawings are not drawn to scale according to actual reference objects. In the accompanying drawings, each identical or nearly identical component shown in various figures may be represented by the same reference numeral. For the sake of clarity, not every component is labeled in each figure. Now, embodiments of various aspects of the present invention will be described by way of example and 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 solution and advantages of the embodiment of the present invention clearer, the technical solution of the embodiment of the present invention will be clearly and completely described below in conjunction with the drawings of the embodiment of the present invention. Obviously, the described embodiment is a part of the embodiment of the present invention, not all of the embodiments. Based on the described embodiment 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 meaning understood by people with general 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 other similar words do not indicate a quantitative limitation, but indicate the existence of at least one. Words such as "include" or "comprise" mean that the elements or objects appearing before "include" or "comprise" cover the features, wholes, steps, operations, elements and / or components listed after "include" or "comprise", 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 isononyl alcohol is increasing day by day, and currently domestic isononyl alcohol plasticizers mainly rely on imports, with extremely low self-production, and the key technology for producing isononyl alcohol is also from foreign countries. The prior art reports that the catalyst for preparing 3,5,5-trimethyl-1-hexanol is a conventional aldehyde hydrogenation catalyst. When used, the conversion rate of catalyzing 3,5,5-trimethyl-1-hexanal and the selectivity of 3,5,5-trimethyl-1-hexanal are both low, which is not suitable 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 reaction and a preparation method thereof. The catalyst not only has excellent activity and stability when used, but also has high selectivity for isononyl alcohol.

[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 preparation steps include: S1, preparing a silicon-zinc mixed solution; specifically, under stirring conditions, uniformly mixing a silica sol solution and a zinc nitrate solution to obtain a mixed solution; S2, adding an alkali to the silicon-zinc mixed solution to obtain a ZnO / SiO2 carrier, and 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, under stirring, mixing the ZnO / SiO2 carrier and the Cu-Ni mixed solution, 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% by mass percentage; 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 abundant specific surface area and suitable pore structure.

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

[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 into 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, and 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℃; after neutralization, raise the reaction temperature to 65℃ and age for 40min; pour out the product, wash, filter, dry, granulate, and roast at 360℃ 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 into 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℃; after neutralization, raise the reaction temperature to 70℃ and age for 60min; pour out the product, wash, filter, dry, granulate, and roast at 400℃ for 3h, 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 into 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. Weigh 315g of 40% silica sol and 79.3g of zinc nitrate, add them into a stirred reactor, mix well to form a silicon-zinc mixed solution; dissolve 345g of K2CO3 in 3L of deionized water to form a solution; weigh 70.5g of Cu(NO3)2 and 24.4g of Ni(NO3)2, 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 15min, 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 75℃; after neutralization, raise the reaction temperature to 80℃ and age for 45min; pour out the product, wash, filter, dry, granulate, and roast at 350℃ for 6h, finally add water and graphite 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 into 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 roast 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 into 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 roast 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 that the addition time of the alkali solution to the silicon-zinc mixed solution for reaction is different; in Comparative Example 1, the alkali solution addition time is controlled to be 5 minutes to obtain catalyst D1; in Comparative Example 2, the alkali solution addition time is controlled to be 45 minutes to obtain catalyst D2.

[0049] Example 7

[0050] The catalyst was applied to the hydrogenation reaction 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 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%, the selectivity of isononanol reaches more than 99%, and the catalyst performance is good. The reason why the catalytic performance of Comparative Example 1 and Comparative Example 2 is poor is that: the alkali solution of Comparative Example 1 fails to fully contact with the ZnO / SiO2 carrier and etch on the carrier surface, so that the carrier surface fails to fully form a suitable pore structure, the specific surface area is small, the active ingredients are unevenly dispersed on the carrier surface, and copper agglomerates, which leads to a decrease in the conversion rate of isononanal and the selectivity of isononanol; when the alkali solution of Comparative Example 2 excessively contacts and etches the ZnO / SiO2 carrier, a larger pore structure is formed on the carrier surface, the specific surface area is significantly reduced, the pore size is increased, and the active ingredients are poorly dispersed on the carrier surface, which leads to a decrease in the conversion rate of isononanal and the selectivity of isononanol.

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

[0056] Example 8

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

[0058] Example 9

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

[0060] Example 10

[0061] Take 50 ml of C1 catalyst and load it into a fixed bed reactor. Before the reaction, reduce the catalyst at 180°C, 0.2 MPa, and 5% hydrogen concentration in nitrogen and hydrogen atmosphere for 12 h. Maintain 180°C, reaction pressure 6 MPa, and feed 3,5,5-trimethyl-1-hexanal for 0.4 h. -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] From Table 2, we can see that 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] Although the present invention has been disclosed as above with preferred embodiments, it is not intended to limit the present invention. A person with ordinary knowledge in the technical field to which the present invention belongs may make various changes and modifications without departing from the spirit and scope of the present invention. Therefore, the protection scope of the present invention shall be determined by the definition of 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) preparing a silicon-zinc mixed solution; 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; 3) Mixing the ZnO / SiO2 carrier and the Cu-Ni mixed solution under stirring, and aging after the reaction is completed, so as to load the active components 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; 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 method for preparing the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 1, characterized in that: 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.

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 2, characterized in that, The time for adding the silicon-zinc mixed solution after the alkali is configured into a solution is 10-30 minutes.

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

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

7. 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 6.

8. The 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 7, 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.

9. Use of the 3,5,5-trimethyl-1-hexanal liquid phase hydrogenation catalyst according to claim 7 in the reaction of aldehyde hydrogenation to alcohol.

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

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