A catalyst for preparing hexafluoroisopropanol, a preparation method thereof and application thereof

Abstract

This invention discloses a catalyst for the gas-phase catalytic hydrogenation of hexafluoroisopropanol, its preparation method, and its application. The catalyst comprises: an activated carbon support, which is pretreated by two steps: alkali washing with an inorganic alkali solution and adsorption with an organic alkali gas; an active component and an auxiliary agent supported on the activated carbon support, wherein the active component is Pd, and the auxiliary agent is selected from at least one of Ce, Mo, Co, Zr, and B, and the particle size of both the active component and the auxiliary agent is 1-10 nm. When the catalyst of this invention is used for the catalytic hydrogenation of hexafluoroacetone trihydrate, the fluoride ion content in the product can be controlled below 10 ppm, and it also exhibits high reactivity and reaction stability.

Description

Technical Field

[0001] This invention relates to the field of catalysis, and in particular to a catalyst for the gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate to prepare hexafluoroisopropanol, its preparation method, and its application. Background Technology

[0002] Hexafluoroisopropanol is an important fluorinated fine chemical that can be used to prepare high-end fluorinated fine chemicals such as the anesthetic sevoflurane, refrigerants, and lithium battery additives. It is also widely used in the organic synthesis of pharmaceuticals and pesticides. Furthermore, hexafluoroisopropanol is highly polar, readily miscible with water and many organic reagents, heat-resistant, and allows ultraviolet light to pass through, making it an ideal solvent for many polymers.

[0003] The process of catalytic hydrogenation to produce hexafluoroisopropanol using hexafluoroacetone as a raw material has advantages such as atom economy and high yield, and has become the main industrial method for producing hexafluoroisopropanol. Based on the different forms of hexafluoroacetone, it can be divided into catalytic hydrogenation processes using gaseous hexafluoroacetone as a raw material and catalytic hydrogenation processes using hexafluoroacetone hydrate as a raw material.

[0004] The catalytic hydrogenation process using gaseous hexafluoroacetone as a raw material involves reacting gaseous hexafluoroacetone with hydrogen in the presence of a catalyst to obtain hexafluoroisopropanol. However, this process presents challenges due to the low boiling point and extremely high toxicity of gaseous hexafluoroacetone, making it difficult to transport and store.

[0005] The catalytic hydrogenation process using hexafluoroacetone hydrate as a raw material can overcome the above-mentioned defects. The catalytic hydrogenation process using hexafluoroacetone hydrate as a raw material includes liquid-phase hydrogenation and gas-phase hydrogenation processes. Among them, the liquid-phase hydrogenation process has the disadvantages of long reaction time and high reaction pressure, and it is a batch reaction, which is not conducive to continuous industrial production.

[0006] The gas-phase catalytic hydrogenation process using hexafluoroacetone hydrate as a raw material refers to the method of preparing hexafluoroisopropanol by vaporizing hexafluoroacetone hydrate and then using a fixed-bed gas-phase catalytic hydrogenation process. It has the advantages of mild reaction conditions, high product yield, and suitability for continuous industrial production, and has good development prospects.

[0007] Patent CN102274734A discloses a catalyst that uses palladium and copper as the first catalyst, K, La or Bi as the second catalyst, and activated carbon as the support for the gas-phase hydrogenation of hexafluoroacetone hydrate to prepare hexafluoroisopropanol. It has the advantages of good catalytic activity and good product selectivity, but it does not disclose the fluoride ion content in the product.

[0008] Patent CN111790401A discloses the application of a catalyst using palladium metal as the active component, Ni, Cr or Cu as an auxiliary agent, and carbon material as a support in the synthesis of hexafluoroisopropanol. It can solve the problems of large amount of precious metal, low activity and short life in palladium carbon catalysts, but it also does not disclose the content of fluoride ions in the product.

[0009] In fact, our research has revealed that existing gas-phase catalytic hydrogenation processes using hexafluoroacetone hydrate as a raw material, employing noble metal catalytic systems, all suffer from high fluoride ion content in the products. For example, when using commercially available Pd / AC, Pd-Cu / AC, and Pd-Ni / AC catalysts, the fluoride ion content in the products can reach over 1000 ppm. High fluoride ion content readily combines with free water in the products to form hydrofluoric acid, which is corrosive, not only damaging equipment but also causing the loss of precious metals from the catalyst and catalyst poisoning.

[0010] Therefore, developing a catalyst with high activity and high stability that can suppress the fluoride ion content in the product is of great significance for the industrial production of hexafluoroisopropanol by gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate as a raw material. Summary of the Invention

[0011] To address the aforementioned technical problems, this invention proposes a catalyst capable of controlling the fluoride ion content in the product to below 10 ppm, while simultaneously possessing high reactivity and reaction stability, for the gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate as a raw material to prepare hexafluoroisopropanol.

[0012] The objective of this invention is achieved through the following technical solution:

[0013] A catalyst for the gas-phase catalytic hydrogenation to prepare hexafluoroisopropanol, the catalyst comprising:

[0014] The activated carbon carrier is pretreated in two steps: inorganic alkaline washing and organic alkaline gas adsorption.

[0015] An active component and an auxiliary agent loaded on an activated carbon support, wherein the active component is Pd and the auxiliary agent is selected from at least one of Ce, Mo, Co, Zr and B, and the particle size of the active component and the auxiliary agent is 1-10 nm.

[0016] The particle size of the active component and auxiliary agent in this invention is 1-10 nm, preferably 1-6 nm. If the particle size of the active component and auxiliary agent is less than 1 nm, the catalyst activity is high, but the fluoride ion content in the product is higher than 10,000 ppm; if the particle size of the active component and auxiliary agent is greater than 10 nm, the catalyst activity is low, and the conversion rate of the raw material hexafluoroacetone trihydrate is less than 80%.

[0017] The active component and the auxiliary agent of this invention are located in adjacent positions in the periodic table, and electrons can easily shift between the metal structures of the active component and the auxiliary agent. This can modulate the carbonyl activation performance and the dissociation ability of the carbon-fluorine bond (CF), resulting in a catalyst with high activity and high stability, while inhibiting the breaking of the carbon-fluorine bond (CF).

[0018] Furthermore, the active component is Pd, and the auxiliary agent is preferably at least one of Ce, Co, and Zr.

[0019] In the catalyst, the active component accounts for 0.1-5.0% of the total mass of the catalyst, preferably 0.5-3.0%; the auxiliary agent accounts for 0.1-3.0% of the total mass of the catalyst, preferably 0.5-2.0%, and the remainder is an activated carbon support. The activated carbon support of this invention can be a conventional activated carbon support, preferably coconut shell activated carbon, with a preferred specific surface area of ​​80-1300 m². 2 The pore volume is preferably between 0.6-1.0 cm³ / g. 3 The apparent density is preferably 0.4-0.6 g / cm³. 3 between.

[0020] This invention also provides a method for preparing any of the catalysts described above, the method comprising the following steps:

[0021] (1) Alkali washing: The activated carbon carrier is treated with inorganic alkali solution, then washed with water until the washing solution is neutral and dried.

[0022] (2) Adsorption: Organic base gas is introduced and adsorbed on the surface of activated carbon carrier to obtain pretreated activated carbon carrier.

[0023] (3) Impregnation and deposition: Prepare active component salt solution and auxiliary agent salt solution, add active component salt solution and / or auxiliary agent salt solution to reaction vessel, then add citric acid or glycerol to impregnate the activated carbon carrier. The impregnation temperature is 50-100℃. After impregnation for 1-5 hours, add ammonia water dropwise until the pH of the solution is 7-9; preferably, the pH is controlled to be about 8.

[0024] (4) Remove the impregnated activated carbon support, dry it, and obtain the catalyst.

[0025] In step (1), the alkaline washing treatment temperature is 40-100°C and the time is 1-5h; the preferred temperature is 60-80°C and the time is 2-3h.

[0026] In step (1), the drying temperature is 100-120°C and the drying time is 2-5h; preferably, the temperature is 100-110°C and the time is 3-4h.

[0027] In step (2), the amount of organic base gas introduced is 2-5 times the mass of the activated carbon carrier, preferably 3-4 times, and more preferably about 3 times; the adsorption time is 3-4 hours.

[0028] In step (3), the active component salt solution is selected from palladium chloroacetate and / or palladium acetate of the active component; the auxiliary agent salt solution is selected from at least one of the chloride, nitrate, and acid salt of the auxiliary agent. Preferably, the auxiliary agent salt solution is selected from at least one of cerium chloride, cerium nitrate, ammonium molybdate, sodium tetraborate, cobalt chloride, and zirconium nitrate.

[0029] In step (4), the drying temperature is 80-120℃ and the drying time is 5-10h; preferably, the drying temperature is 100-120℃ and the drying time is 6-8h.

[0030] The special feature of this invention is that the activated carbon carrier needs to be subjected to an inorganic alkaline washing treatment and an organic alkaline gas adsorption treatment in sequence. The inorganic alkaline solution is selected from at least one of sodium hydroxide solution, potassium hydroxide solution or ammonia water; the organic alkaline gas is selected from at least one of triethylamine, pyridine or piperidine.

[0031] This invention first alters the functional group types on the surface of activated carbon through alkaline washing, then adsorbs and pre-treats the carrier using a nitrogen-containing organic base. This allows the nitrogen-containing organic base gas to be immobilized on the activated carbon carrier surface. The lone pair electrons in the nitrogen-containing organic base can coordinate with holes in the metal, facilitating the anchoring of active component metal ions and auxiliary metal ions on the activated carbon carrier. Simultaneously, during the loading of active components and auxiliary agents using an impregnation deposition method, the addition of a hydroxyl-containing organic dispersant (citric acid or glycerol) aids in the dispersion of the metal on the carrier surface. After impregnation for a period of time, the particle size of the active components and auxiliary agents can be controlled by adjusting the pH.

[0032] The catalyst described in this invention employs an impregnation deposition method, which can be either a stepwise impregnation deposition method or a co-impregnation deposition method. When using stepwise impregnation deposition, the active component can be impregnated first, followed by the additives, or the additives can be impregnated first, followed by the active component. When using co-impregnation deposition, the active component and the additives can be impregnated simultaneously.

[0033] The catalyst prepared by the impregnation deposition method of this invention has an active component and auxiliary agent with a particle size of 1-10 nm, and the active component and auxiliary agent are uniformly dispersed, with an auxiliary metal near each active site. The interaction force between the bimetallic surface formed by the active metal and the auxiliary agent and hydrogen atoms is weaker than that of the pure active metal (Pd) surface, which allows hydrogen to desorb at a lower temperature during the gas-phase hydrodechlorination reaction to prepare hexafluoroisopropanol; at the same time, the bimetal also weakens the activation of CF and reduces the fluoride ion content in the reaction product.

[0034] The present invention also provides a method for preparing hexafluoroisopropanol, the method comprising: using hexafluoroacetone trihydrate as raw material, and preparing it by gas-phase catalytic hydrogenation under the action of any of the catalysts described above or the catalysts prepared by any of the preparation methods described above, at a reaction temperature of 110-200℃ and a reaction pressure of atmospheric pressure.

[0035] Preferably, the catalyst is subjected to reduction treatment before the reaction. The reduction treatment step includes: loading the catalyst into the reactor, introducing a hydrogen-nitrogen mixture for heating and reduction, wherein hydrogen accounts for 10%-60% of the volume of the hydrogen-nitrogen mixture, the reduction temperature is 200-300℃, and the reduction time is 1-3h.

[0036] The gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate to prepare hexafluoroisopropanol described in this invention is carried out in a fixed-bed reactor, preferably made of 316L stainless steel.

[0037] The preparation method of hexafluoroisopropanol according to the present invention specifically includes the following steps:

[0038] The raw material, hexafluoroacetone trihydrate, is injected using a micro-pump, with a preferred liquid hourly space velocity (LHSV) of 0.05-10 h⁻¹. -1 The mixture is then vaporized in a vaporizer after being mixed with hydrogen. The preferred vaporization temperature is 110-180℃, the preferred molar ratio of hydrogen to hexafluorolactone trihydrate is (1-4):1, the preferred reaction temperature is 110-200℃, and the preferred reaction pressure is atmospheric pressure. After the reaction is complete, the reaction products are condensed and separated, the hydrogen is vented, and the liquid phase material is collected and analyzed by gas chromatography for conversion and selectivity. The fluoride ion content in the product is analyzed using a fluoride ion electrode.

[0039] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0040] When the catalyst of this invention is used for the gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate to prepare hexafluoroisopropanol, the conversion rate of hexafluoroacetone trihydrate is ≥99%, the selectivity of the product hexafluoroisopropanol is ≥99%, and the fluoride ion content in the product is <10ppm. Attached Figure Description

[0041] Appendix Figure 1 This is a TEM characterization image of the catalyst prepared in Example 1 of the present invention. Detailed Implementation

[0042] The present invention will be further described below with reference to specific embodiments, but the invention is not limited to these specific embodiments. Those skilled in the art should recognize that the present invention covers all alternatives, improvements, and equivalents that may be included within the scope of the claims.

[0043] Example 1

[0044] This embodiment provides a method for preparing a catalyst for preparing hexafluoroisopropanol, comprising the following steps:

[0045] (1) Carrier pretreatment: Prepare 500 mL of 10 wt% sodium hydroxide solution, weigh 100 g of coconut shell activated carbon and add it to the sodium hydroxide solution, heat to 80 °C, stir and reflux for 2 h, then cool to room temperature; wash with deionized water until the pH of the washing solution is neutral; dry at 100 °C for 5 h. Pass triethylamine vapor into the activated carbon for adsorption treatment for 2 h, and set aside for later use.

[0046] (2) Impregnation: Prepare an aqueous solution of chloropalladic acid and an aqueous solution of cerium nitrate and add them to the reaction vessel. Then add citric acid. The palladium content is 1.0% of the activated carbon support, the cerium content is 0.5% of the activated carbon support, and the citric acid content is 10% of the activated carbon support. The total volume of the impregnation solution is 3:1 to the volume of the activated carbon support. The impregnation temperature is 60℃. After impregnation for 1 hour, stir and add 10% ammonia water precipitation solution dropwise. Stop the dropwise addition when the pH is about 8. Take out the impregnated activated carbon support and dry it in an oven at 110℃ for 6 hours to obtain the catalyst precursor.

[0047] (3) Reduction: The obtained catalyst precursor was placed in a hydrogen-nitrogen mixed atmosphere, with hydrogen occupying 50% of the volume of the hydrogen-nitrogen mixture and a space velocity of 100 h⁻¹. -1 The temperature was increased from room temperature to 300°C at a rate of 1°C / min and held at that temperature for 3 hours to obtain the catalyst, denoted as cat1.

[0048] Figure 1 TEM characterization images of the catalyst prepared in this embodiment are given. It can be seen from the images that Pd and Ce are uniformly dispersed in the catalyst, and the particle size of Pd and Ce is 1 nm.

[0049] Example 2

[0050] The operation in this embodiment is the same as in embodiment 1, except that step (2) adopts stepwise impregnation deposition, and the specific steps are as follows:

[0051] (2) Prepare an aqueous solution of cerium nitrate and add it to the reaction vessel. Then add citric acid. The cerium content is 0.5% of the activated carbon support and the citric acid content is 10% of the activated carbon support. The total volume of the impregnation solution and the volume ratio of the activated carbon support are 3:1. The impregnation temperature is 60℃. After impregnation for 1 hour, stir and add 10% ammonia water precipitation solution dropwise. Stop the dropwise addition when the pH is about 8. Take out the impregnated activated carbon support and place it in an oven at 110℃ to dry for 6 hours to obtain the stage catalyst.

[0052] Continue preparing the chloropalladium acid aqueous solution and adding it to the reaction vessel, then add citric acid. The palladium content is 1.0% of the activated carbon support, and the citric acid content is 10% of the activated carbon support. The total volume ratio of the impregnation solution to the activated carbon support is 3:1. Pour the stage catalyst into the solution, and the impregnation temperature is 60℃. After impregnation for 1 hour, stir, and add 10% ammonia water precipitation solution dropwise. Stop the dropwise addition when the pH is about 8. Take out the impregnated activated carbon support and place it in a 110℃ oven to dry for 6 hours to obtain the catalyst precursor.

[0053] With all other operations unchanged, the catalyst prepared was denoted as cat2. TEM characterization showed that the particle size of both Pd and Ce was 4 nm.

[0054] Example 3

[0055] The operation of this embodiment is the same as that of embodiment 2, except that: in step (2) step-by-step impregnation deposition, the active component is impregnated first, and then the deposition aid is impregnated. The catalyst obtained is denoted as cat3. According to TEM characterization, the particle size of Pd and Ce is 3nm.

[0056] Example 4

[0057] The operation in this embodiment is the same as in Example 1, except that the auxiliary salt solution is zirconium nitrate, and everything else remains the same. The catalyst obtained is denoted as cat4. TEM characterization shows that the particle size of Pd and Zr is 2 nm.

[0058] Example 5

[0059] The operation in this embodiment is the same as in embodiment 1, except that the auxiliary salt solution is cobalt nitrate, and everything else remains the same. The catalyst obtained is denoted as cat5. TEM characterization shows that the particle size of Pd and Co is 4 nm.

[0060] Example 6

[0061] The operation in this embodiment is the same as in embodiment 1, except that: the auxiliary salt solution is ammonium molybdate, and everything else remains the same. The catalyst obtained is denoted as cat6. TEM characterization shows that the particle size of Pd and Mo is 2 nm.

[0062] Example 7

[0063] The operation in this embodiment is the same as in Example 1, except that the auxiliary salt solution is sodium tetraborate, and everything else remains the same. The catalyst obtained is denoted as cat7. TEM characterization shows that the particle size of Pd and B is 3 nm.

[0064] Example 8

[0065] The operation of this embodiment is the same as that of embodiment 1, except that the activated carbon support material is coal-based carbon instead of coconut shell carbon, and everything else remains the same. The catalyst obtained is denoted as cat8. TEM characterization shows that the particle size of Pd and Ce is 6 nm.

[0066] Example 9

[0067] The operation in this embodiment is the same as in Example 1, except that the content of the active component Pd is increased to 2% and the content of the auxiliary agent Ce is increased to 2%, while other aspects remain unchanged. The catalyst obtained is denoted as cat9. TEM characterization shows that the particle size of both Pd and Ce is 4 nm.

[0068] Example 10

[0069] The operation in this embodiment is the same as in Example 5, except that the content of the active component Pd is increased to 4% and the content of the auxiliary agent Co is increased to 3%, while other aspects remain unchanged. The catalyst obtained is denoted as cat10. TEM characterization shows that the particle size of both Pd and Co is 6 nm.

[0070] Example 11

[0071] The operation of this embodiment is the same as that of embodiment 1, except that in step (1), pyridine vapor is used instead of triethylamine vapor for adsorption, and everything else remains the same. The catalyst obtained is denoted as cat11. By TEM characterization, the particle size of Pd and Ce is 5 nm.

[0072] Comparative Example 1

[0073] A commercial Pd / C catalyst with a Pd loading of 1.5% was used, and the reduction method was the same as in Example 1, denoted as catB1.

[0074] Comparative Example 2

[0075] The operation of this comparative example is the same as that of Example 1, except that: step (1) carrier pretreatment adopts acid washing treatment, the specific steps of which are as follows:

[0076] Using a 30% nitric acid solution, weigh 100g of coconut shell activated carbon and add it to the nitric acid solution. Heat to 90℃, stir and reflux for 2 hours, cool to room temperature, wash with deionized water until the pH of the washing solution is neutral, and dry at 100℃ for 5 hours for later use.

[0077] With all other operations remaining unchanged, the catalyst obtained is denoted as catB2.

[0078] Comparative Example 3

[0079] The operation of this comparative example is the same as that of Example 1, except that in step (1) the carrier pretreatment process, only sodium hydroxide solution is used for washing, and triethylamine adsorption treatment is not used. Other operations remain unchanged, and the catalyst obtained is denoted as catB3.

[0080] Comparative Example 4

[0081] The operation of this comparative example is the same as that of Example 1, except that: the active component is Pd, and the auxiliary agent is nickel nitrate, wherein the Pd content is 1% and the nickel content is 0.5%, and other operations remain unchanged. The catalyst obtained is denoted as catB4.

[0082] Comparative Example 5

[0083] The operation of this comparative example is the same as that of Example 1, except that: the active component is Pd, and the auxiliary agents are copper chloride and potassium chloride, wherein the Pd content is 2.55%, the copper content is 0.5%, and the potassium content is 0.1%, and other operations remain unchanged. The catalyst obtained is denoted as catB5.

[0084] Application Example 1

[0085] The prepared cat1-cat11 and catB1-catB5 catalysts were used as reaction catalysts in the gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate to prepare hexafluoroisopropanol. The specific operation is as follows:

[0086] Catalyst evaluation: A micro-injection pump was used for feeding hexafluoroacetone trihydrate at a rate of 10 g / h, with a liquid hourly space velocity (LHSV) of 5 h⁻¹. -1 After being mixed with hydrogen, it enters the vaporizer for vaporization at a temperature of 150°C. The molar ratio of hydrogen to hexafluorolactone trihydrate is 3:1. The reaction temperature is 140°C, and the reaction pressure is atmospheric pressure.

[0087] After the reaction was completed, the reaction products were condensed and separated, hydrogen gas was released into the atmosphere, and the liquid phase was collected and analyzed for conversion and selectivity using an Agilent 7890A gas chromatograph. The fluoride ion content in the products was analyzed using a fluoride ion electrode. The analytical results are shown in Table 1 below:

[0088] Table 1 Reaction Results

[0089]

[0090]

[0091] Application Example 2

[0092] Using Cat1 and commercial Pd / C catalysts as the subjects of investigation, the reaction stability of the hydrogenation of hexafluoroacetone trihydrate to hexafluoroisopropanol at different reaction times was evaluated using the catalyst evaluation method in Application Example 1. The results are shown in Table 2 below:

[0093] Table 2 Stability evaluation results

[0094]

Claims

1. A catalyst for the gas-phase catalytic hydrogenation to prepare hexafluoroisopropanol, characterized in that: The catalyst includes: The activated carbon carrier is pretreated in two steps: inorganic alkaline washing and organic alkaline gas adsorption. An active component and an auxiliary agent loaded on an activated carbon support, wherein the active component is Pd and the auxiliary agent is selected from at least one of Ce, Mo, Co, Zr and B, and the particle size of the active component and the auxiliary agent is 1-10 nm. The inorganic alkaline solution is selected from at least one of sodium hydroxide solution, potassium hydroxide solution, or ammonia water; the organic alkaline gas is selected from at least one of triethylamine, pyridine, or piperidine.

2. The catalyst for the gas-phase catalytic hydrogenation to prepare hexafluoroisopropanol according to claim 1, characterized in that: The active component accounts for 0.1-5.0% of the total mass of the catalyst, the auxiliary agent accounts for 0.1-3.0% of the total mass of the catalyst, and the remainder is activated carbon support.

3. The method for preparing the catalyst according to any one of claims 1-2, characterized in that: The preparation method includes the following steps: (1) Alkali washing: The activated carbon carrier is treated with an inorganic alkaline solution, followed by water washing until the washing solution is neutral and then dried; the inorganic alkaline solution is selected from at least one of sodium hydroxide solution, potassium hydroxide solution or ammonia water. (2) Adsorption: An organic base gas is introduced and adsorbed on the surface of the activated carbon support to obtain a pretreated activated carbon support; the organic base gas is selected from at least one of triethylamine, pyridine or piperidine. (3) Impregnation and deposition: Prepare active component salt solution and auxiliary agent salt solution, add active component salt solution and / or auxiliary agent salt solution to reaction vessel, then add citric acid or glycerol to impregnate the activated carbon carrier. The impregnation temperature is 50-100℃. After impregnation for 1-5 hours, add ammonia water dropwise until the pH of the solution is 7-9. (4) Remove the impregnated activated carbon support, dry it, and obtain the catalyst.

4. The method for preparing the catalyst according to claim 3, characterized in that: In step (1), the alkaline washing treatment temperature is 40-100℃ and the time is 1-5h.

5. The method for preparing the catalyst according to claim 3, characterized in that: In step (1), the drying temperature is 100-120℃ and the drying time is 2-5h.

6. The method for preparing the catalyst according to claim 3, characterized in that: In step (4), the drying temperature is 80-120℃ and the drying time is 5-10h.

7. The method for preparing the catalyst according to claim 3, characterized in that: The active component salt solution is selected from chloropalladium acid and / or palladium acetate of the active component; the auxiliary agent salt solution is selected from at least one of the chloride, nitrate, and acid salt of the auxiliary agent.

8. A method for preparing hexafluoroisopropanol, comprising preparing it by gas-phase catalytic hydrogenation of hexafluoroacetone trihydrate, characterized in that: The catalyst described in any one of claims 1-2, or the catalyst prepared by any one of the preparation methods in claims 4-7, is used as the reaction catalyst. The reaction temperature is 110-200℃ and the reaction pressure is atmospheric pressure.

9. The method for preparing hexafluoroisopropanol according to claim 8, characterized in that: Before the reaction, the catalyst is subjected to reduction treatment. The reduction treatment steps include: loading the catalyst into the reactor, introducing a hydrogen-nitrogen mixture for heating and reduction, wherein hydrogen accounts for 10%-60% of the volume of the hydrogen-nitrogen mixture, the reduction temperature is 200-300℃, and the reduction time is 1-3h.

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