A transition metal supported catalytic hydroisomerization catalyst, its preparation method and application

Abstract

This invention discloses a transition metal-supported catalytic hydroisomerization catalyst, its preparation method, and its application, belonging to the field of catalysis technology. The technical solution includes preparing solution A by mixing nickel nitrate hexahydrate, cobalt nitrate hexahydrate, ferric nitrate nonahydrate, aluminum nitrate nonahydrate, phosphoric acid, and citric acid; preparing solution B by adding tetraethyl orthosilicate to anhydrous ethanol; transferring solutions A and B to a high-pressure reactor and reacting them fully at 150-250°C to obtain a catalyst precursor; calcining the catalyst precursor at 550-650°C; and then reducing the calcined catalyst with hydrogen to obtain the transition metal-supported catalytic hydroisomerization catalyst. This invention is applied to the catalytic preparation of bio-jet fuel, solving the technical problems of complex preparation processes and poor activity and selectivity of existing hydroisomerization catalysts, and features a simple preparation process and high catalyst activity and selectivity.

Description

Technical Field

[0001] This invention belongs to the field of catalysis technology, and particularly relates to a transition metal supported catalytic hydrogenation isomer catalyst, its preparation method and application. Background Technology

[0002] Currently, the main production processes for bio-jet kerosene include oil hydrogenation, Fischer-Tropsch synthesis, hydrothermal treatment of oils, and bio-ethanol production. Among these, oil hydrogenation is the most competitive and commercially mature method due to its simpler process and higher product quality compared to other methods. The process steps of oil hydrogenation are as follows: using waste oils as raw materials, pretreatment (including acid washing and adsorption) removes impurities. Then, hydrogenation deoxygenation removes oxygen, nitrogen, and sulfur from the oils to prepare hydrogenated vegetable oil (HVO). Next, hydroisomerization adjusts the molecular structure by isomerizing the long-chain n-isomers to meet the low-temperature fluidity requirements of jet kerosene (e.g., freezing point ≤ -40℃). Finally, purification through distillation yields the bio-jet kerosene product. In existing technologies, precious metal catalysts (such as Pt and Pd) are expensive and suffer from low isomerization selectivity and numerous cracking side reactions, resulting in insufficient product yield. While non-precious metal catalysts are cheaper, they suffer from insufficient active sites and difficulties in acidity control.

[0003] Chinese patent CN119237005A discloses a hydrocarbon skeletal isomer catalyst, its preparation method, and its application, and specifically discloses the following steps: 1) contacting an active metal source solution with mesoporous silica or anionic polymer to obtain a metal source; 2) mixing the metal source with a SAPO-11 synthesis system, and sequentially subjecting the resulting mixture to crystallization, drying, and calcination treatments to obtain the catalyst; the SAPO-11 synthesis system includes deionized water, a phosphorus source, an aluminum source, a silicon source, and a structure directing agent.

[0004] However, the above-mentioned catalyst preparation process is complicated. It requires the preparation of a precursor first, then mixing the precursor with the silicon source. Furthermore, the precursor uses a pre-formed support before participating in the synthesis system of the support, resulting in uneven distribution. At the same time, the active component is a single component, leading to poor catalyst selectivity and stability. Summary of the Invention

[0005] To address the shortcomings of existing technologies, this invention solves the technical problems of complex preparation processes and poor activity and selectivity of existing hydroisomerization catalysts. It proposes a transition metal supported hydroisomerization catalyst with simple preparation process, high activity and selectivity, its preparation method and application.

[0006] To solve the aforementioned technical problem, the technical solution adopted by the present invention is as follows:

[0007] This invention provides a method for preparing a transition metal-supported catalytic hydroisomerization catalyst, comprising:

[0008] Prepare solution A by mixing nickel nitrate hexahydrate, cobalt nitrate hexahydrate, ferric nitrate nonahydrate, aluminum nitrate nonahydrate, phosphoric acid, and citric acid.

[0009] Tetraethyl orthosilicate was added to anhydrous ethanol to prepare solution B;

[0010] Solution A and solution B were transferred to a high-pressure reactor and reacted at 150-250℃ to obtain the catalyst precursor.

[0011] The catalyst precursor was calcined at 550-650℃, and the calcined catalyst was reduced with hydrogen to obtain a transition metal supported catalytic hydroisomerization catalyst.

[0012] By weight, the amount of nickel nitrate hexahydrate is any value of 8-20 parts, the amount of cobalt nitrate hexahydrate is any value of 3-10 parts, the amount of ferric nitrate nonahydrate is any value of 5-16 parts, the amount of aluminum nitrate nonahydrate is any value of 40-100 parts, the amount of phosphoric acid is any value of 5-20 parts, the amount of citric acid is any value of 5-20 parts, and the amount of tetraethyl orthosilicate is any value of 10-40 parts.

[0013] Preferably, solutions A and B are subjected to ultrasonic treatment before being transferred to a high-pressure reactor.

[0014] Preferably, solutions A and B are transferred to a high-pressure reactor and reacted at 150-250°C for 6-24 hours to obtain a catalyst precursor, which is then extruded into shape.

[0015] The extruded catalyst precursor was calcined at 550-650℃ for 2-8 hours, and the calcined catalyst was reduced with hydrogen to obtain a transition metal supported catalytic hydroisomerization catalyst.

[0016] In another aspect, the present invention provides a transition metal supported catalytic hydroisomerization catalyst prepared by the preparation method of any of the above technical solutions.

[0017] Preferably, the ICP content of nickel in the transition metal supported catalytic hydroisomerization catalyst is 7-15%, the ICP content of cobalt is 2-8%, the ICP content of iron is 3-9%, the ICP content of aluminum is 12-30%, and the ICP content of silicon is 4-25%.

[0018] The specific surface area of ​​the transition metal supported catalytic hydroisomerization catalyst is 211-235 m². 2 / g.

[0019] This invention also provides the application of the above-mentioned transition metal supported catalytic hydroisomerization catalyst in hydroisomerization catalytic reactions.

[0020] Preferably, n-octadecane is used as a raw material, and a hydroisomerization catalytic reaction is carried out on it to prepare bio-jet fuel; including: loading a transition metal supported catalytic hydroisomerization catalyst into a fixed bed reaction tube, heating to reduce the catalyst, adjusting the reaction temperature after the catalyst reduction is completed, and introducing hydrogen and HVO (hydrogenated vegetable oil) for continuous reaction to obtain SAF (bio-jet fuel).

[0021] The product yield is 93-97%, and the C18 conversion rate is 99.15-99.61%.

[0022] In bio-jet fuel, C5-C18 n-alkanes account for 26.41-28.79%, and C5-C18 isoalkanes account for 71.21-73.59%.

[0023] Compared with the prior art, the beneficial effects of the present invention are as follows:

[0024] This invention provides a method for preparing a transition metal supported catalytic hydrogenation isomer catalyst. The method involves preparing a multi-transition metal supported catalyst in one step via a hydrothermal method. The multiple transition metals enhance the synergistic effect of the active components of the catalyst, thereby improving the catalyst activity and selectivity. Furthermore, the method completes the support formation and active component loading in one step, increasing the interaction between the active components and the support and simplifying the process flow. Detailed Implementation

[0025] The technical solutions in specific embodiments of the present invention will be described in detail and completely below. Obviously, the described embodiments are only some specific implementations of the overall technical solution of the present invention, and not all implementations. Based on the overall concept of the present invention, all other embodiments obtained by those skilled in the art fall within the protection scope of the present invention.

[0026] This invention provides a method for preparing a transition metal-supported catalytic hydrogenation isomer catalyst, comprising: preparing a solution A by dissolving nickel nitrate hexahydrate, cobalt nitrate hexahydrate, ferric nitrate nonahydrate, aluminum nitrate nonahydrate, phosphoric acid, and citric acid; preparing a solution B by adding tetraethyl orthosilicate to anhydrous ethanol; transferring solutions A and B to a high-pressure reactor and reacting them fully at 150-250°C to obtain a catalyst precursor; calcining the catalyst precursor at 550-650°C; and reducing the calcined catalyst with hydrogen to obtain a transition metal-supported catalytic hydrogenation isomer catalyst.

[0027] The preparation method of this invention provides a one-step hydrothermal preparation of a supported catalyst with multiple transition metals. The process is simple, and the use of multiple transition metals enhances the synergistic effect of the catalyst's active components, resulting in a larger specific surface area and more active sites, thus improving catalyst activity and selectivity. Furthermore, the one-step completion of support molding and active component loading increases the interaction between the active components and the support, simplifying the process. Simultaneously, this preparation method does not use precious metals as raw materials, effectively reducing costs.

[0028] It should be emphasized that the preparation of the catalyst of the present invention involves the preparation of the support and the loading of the active component in one step. This simplifies the process, shortens the reaction steps, increases the dispersion of the active component in the support, increases the number of reaction sites, and increases the stability of the catalyst.

[0029] In the above technical solution, by weight, the amount of nickel nitrate hexahydrate is any value of 8-20 parts, the amount of cobalt nitrate hexahydrate is any value of 3-10 parts, the amount of ferric nitrate nonahydrate is any value of 5-16 parts, the amount of aluminum nitrate nonahydrate is any value of 40-100 parts, the amount of phosphoric acid is any value of 5-20 parts, the amount of citric acid is any value of 5-20 parts, and the amount of tetraethyl orthosilicate is any value of 10-40 parts.

[0030] It is understandable that the dosage of nickel nitrate hexahydrate can be any value within the range of 10, 12, 14, 16, 18 parts; the dosage of cobalt nitrate hexahydrate can be any value within the range of 4, 5, 6, 7, 8, 9 parts; the dosage of ferric nitrate nonahydrate can be any value within the range of 7, 9, 11, 13, 15 parts; the dosage of aluminum nitrate nonahydrate can be any value within the range of 50, 60, 70, 80, 90 parts; the dosage of phosphoric acid can be any value within the range of 7, 9, 11, 13, 15, 17 parts; the dosage of citric acid can be any value within the range of 7, 9, 11, 13, 15, 17 parts; and the dosage of tetraethyl orthosilicate can be any value within the range of 15, 20, 25, 30, 35 parts.

[0031] In the above technical solution, the nickel precursor salt is nickel nitrate hexahydrate, the cobalt precursor salt is cobalt nitrate hexahydrate, the iron precursor salt is ferric nitrate nonahydrate, the aluminum precursor salt is aluminum nitrate nonahydrate, and the silicon precursor is tetraethyl orthosilicate. This technical solution specifically defines the types of nickel, cobalt, iron, aluminum, and silicon precursor salts. Nickel, cobalt, and iron precursor salts are common, readily available, and low-cost transition metals, and are also common catalyst active component precursors for catalytic isomerization. Aluminum and silicon precursor salts are common, readily available, and low-cost aluminum and silicon molecular sieve precursors. In a preferred embodiment, solutions A and B are ultrasonically treated and then transferred to a high-pressure reactor. Ultrasonic dispersion facilitates the complete dissolution of solutions A and B, ensuring the homogeneity of the solutions.

[0032] In a preferred embodiment, solutions A and B are transferred to a high-pressure reactor and reacted at 150-250°C for 6-24 hours to obtain a catalyst precursor, which is then extruded into shape.

[0033] The extruded catalyst precursor was calcined at 550-650℃ for 2-8 hours, and the calcined catalyst was reduced with hydrogen to obtain a transition metal supported catalytic hydroisomerization catalyst.

[0034] Understandably, the reaction temperature in the high-pressure reactor can be any value within the range of 180℃, 200℃, 220℃, and the reaction time can be any value within the range of 10 hours, 15 hours, 20 hours, and the calcination temperature can be any value within the range of 570℃, 590℃, 610℃, 630℃, and the calcination time can be any value within the range of 3 hours, 4 hours, 5 hours, 6 hours, 7 hours, and the above hydrogen reduction steps can be carried out in a fixed bed when a catalyst is used.

[0035] In another aspect, the present invention provides a transition metal supported catalytic hydroisomerization catalyst prepared by the preparation method of any of the above technical solutions.

[0036] In a preferred embodiment, the transition metal supported catalytic hydroisomerization catalyst has an ICP content of 7-15% for nickel, 2-8% for cobalt, 3-9% for iron, 12-30% for aluminum, and 4-25% for silicon.

[0037] The specific surface area of ​​the transition metal supported catalytic hydroisomerization catalyst is 211-235 m². 2 / g.

[0038] In the aforementioned transition metal-supported catalytic hydroisomerization catalysts, within the confined environment of the silica-alumina molecular sieve, Ni-Fe-Co may form an alloy structure, and Fe... 2+ / Fe 3+ and Co 2+ / Co 3+ Ni's variable valence properties allow it to participate in redox cycles. 2+ The stable valence state of Fe contributes to the stability of the intermediate state. 3+ Co can be promoted through electron transfer 3+ The formation of cobalt accelerates hydrogen activation in the hydrogenolysis reaction. The high electronegativity of cobalt attracts electrons from the Ni / Fe matrix, forming electron-rich or electron-deficient regions, thus optimizing the adsorption capacity for reactants (such as long-chain alkanes). The one-step hydrothermal synthesis of the catalyst increases the interaction between the metal active component and the support. The microporous structure of the molecular sieve can anchor the metal particles (Ni-Co-Fe alloy) and prevent high-temperature sintering. At the same time, the Fe / Co matrix, after being embedded in the molecular sieve framework, forms Si-OH-Fe / Co bonds, introducing Lewis acidic sites, reducing acid strength, inhibiting cracking side reactions, and increasing isomer selectivity. Meanwhile, the presence of Fe and Co can inhibit the aggregation of Ni particles, ensuring the hydrodehydrogenation activity of the catalyst. The nickel-iron-cobalt active components, through electronic complementarity, functional division of labor, and redox synergy, form multiple synergies with the acidity and pore confinement of the silicon-aluminum molecular sieve support, significantly improving the activity and selectivity of the hydroisomerization reaction.

[0039] This invention also provides the application of the above-mentioned transition metal supported catalytic hydroisomerization catalyst in hydroisomerization catalytic reactions.

[0040] In a preferred embodiment, n-octadecane is used as a raw material, and a hydroisomerization catalytic reaction is performed on it to prepare bio-jet fuel. The process includes: loading a transition metal-supported hydroisomerization catalyst into a fixed-bed reaction tube, heating to reduce the catalyst, adjusting the reaction temperature after catalyst reduction, and continuously introducing hydrogen and HVO (hydrogenated vegetable oil) to obtain SAF (bio-jet fuel). The product yield is 93-97%, and the C18 conversion rate is 99.15-99.61%. The bio-jet fuel contains 26.41-28.79% C5-C18 n-alkanes and 71.21-73.59% C5-C18 isoalkanes.

[0041] To provide a clearer and more detailed description of the transition metal supported catalytic hydrogenation isomer catalyst, its preparation method, and its application provided in the embodiments of the present invention, the following description will be based on specific embodiments.

[0042] Example 1

[0043] 1) Add 10 parts of nickel nitrate hexahydrate, 5 parts of cobalt nitrate hexahydrate, 8 parts of ferric nitrate nonahydrate, 40 parts of aluminum nitrate nonahydrate, 12 parts of phosphoric acid, and 12 parts of citric acid to 200 parts of deionized water and sonicate to fully dissolve them to prepare solution A.

[0044] 2) Add 40 parts of tetraethyl orthosilicate to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0045] 3) Transfer solutions A and B to a high-pressure reactor and react at 200°C for 12 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 550°C in a muffle furnace for 4 hours, and then cooled to obtain the final catalyst.

[0046] Example 2

[0047] 1) Add 15 parts of nickel nitrate hexahydrate, 8 parts of cobalt nitrate hexahydrate, 10 parts of ferric nitrate nonahydrate, 60 parts of aluminum nitrate nonahydrate, 10 parts of phosphoric acid, and 18 parts of citric acid to 200 parts of deionized water and sonicate to fully dissolve them to prepare solution A.

[0048] 2) Add 30 parts of tetraethyl orthosilicate to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0049] 3) Transfer solutions A and B to a high-pressure reactor and react at 250°C for 18 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 600°C in a muffle furnace for 6 hours, and then cooled to obtain the final catalyst.

[0050] Example 3

[0051] 1) Add 8 parts of nickel nitrate hexahydrate, 3 parts of cobalt nitrate hexahydrate, 5 parts of ferric nitrate nonahydrate, 80 parts of aluminum nitrate nonahydrate, 8 parts of phosphoric acid, and 10 parts of citric acid to 200 parts of deionized water and sonicate to fully dissolve them to prepare solution A.

[0052] 2) Add 20 parts of tetraethyl orthosilicate to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0053] 3) Transfer solutions A and B to a high-pressure reactor and react at 150°C for 6 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 550°C in a muffle furnace for 2 hours, and then cooled to obtain the final catalyst.

[0054] Example 4

[0055] 1) Dissolve 20 parts of nickel nitrate hexahydrate, 10 parts of cobalt nitrate hexahydrate, 16 parts of ferric nitrate nonahydrate, 100 parts of aluminum nitrate nonahydrate, 6 parts of phosphoric acid, and 20 parts of citric acid in 200 parts of deionized water by sonication to prepare solution A.

[0056] 2) Add 10 parts of tetraethyl orthosilicate to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0057] 3) Transfer solutions A and B to a high-pressure reactor and react at 200°C for 24 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 550°C in a muffle furnace for 8 hours. After cooling, the final catalyst is obtained.

[0058] Comparative Example 1

[0059] 1) Dissolve 10 parts of nickel nitrate hexahydrate, 5 parts of cobalt nitrate hexahydrate, 8 parts of ferric nitrate nonahydrate, 15 parts of boehmite, 12 parts of phosphoric acid, and 12 parts of citric acid in 200 parts of deionized water by sonication to prepare solution A.

[0060] 2) Add 40 parts of SBA-15 to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0061] 3) Transfer solutions A and B to a high-pressure reactor and react at 200°C for 12 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 550°C in a muffle furnace for 4 hours, and then cooled to obtain the final catalyst.

[0062] Comparative Example 2

[0063] 1) Add 10 parts of nickel nitrate hexahydrate, 5 parts of cobalt nitrate hexahydrate, 8 parts of ferric nitrate nonahydrate, 12 parts of phosphoric acid, and 12 parts of citric acid to 200 parts of deionized water and sonicate to fully dissolve them to prepare solution A.

[0064] 2) Use 100 parts of anhydrous ethanol as solution B;

[0065] 3) Solutions A and B were transferred to a high-pressure reactor and reacted at 200°C for 12 hours. After filtration and washing, the catalyst precursor was obtained. The precursor was then extruded and calcined in a muffle furnace at 550°C for 4 hours, followed by cooling to obtain the final catalyst. Citric acid can complex with metal ions to form chelates, which can then form a sol-gel catalyst precursor under high-temperature hydrothermal conditions.

[0066] Comparative Example 3

[0067] 1) Add 10 parts of nickel nitrate hexahydrate, 40 parts of aluminum nitrate nonahydrate, 12 parts of phosphoric acid, and 12 parts of citric acid to 200 parts of deionized water and sonicate to fully dissolve them to prepare solution A;

[0068] 2) Add 40 parts of tetraethyl orthosilicate to 100 parts of anhydrous ethanol and sonicate to dissolve evenly to prepare solution B;

[0069] 3) Transfer solutions A and B to a high-pressure reactor and react at 200°C for 12 hours. After filtration and washing, the catalyst precursor is obtained. The obtained precursor is then extruded and calcined at 550°C in a muffle furnace for 4 hours, and then cooled to obtain the final catalyst.

[0070] Test case

[0071] The final catalyst obtained from the above examples and comparative examples was weighed at 10g and transferred to a fixed-bed reaction tube. Inert packing materials (silicon carbide, quartz sand, etc.) were filled into the upper and lower parts of the tube. After leak testing, the atmosphere was purged with nitrogen and hydrogen, respectively. The hydrogen flow rate was then set to 100mL / min, and the temperature was raised to 380℃. The tube was kept at this temperature for 4 hours, then cooled to 300℃. The hydrogen flow rate was set to 60mL / min, and n-octadecane was introduced at a flow rate of 0.2mL / min. The feed was stabilized for 12 hours, and the reaction continued for another 12 hours. Samples were collected, yields were calculated, and samples were analyzed by gas chromatography to determine the reaction conversion and isomer selectivity. The results are shown in Table 1. The gas chromatography method was as follows: HP-5MS column, initial column temperature 50℃, increased to 280℃ at 3℃ / min, held for 8 minutes, FID detector, injection volume 0.2μL, split ratio 39:1, vaporization chamber 250℃, detector 300℃.

[0072] Table 1 Results of gas chromatography analysis

[0073]

[0074] In Table 1, the percentage of C15-C18 n-alkanes refers to the percentage of C15-C18 n-alkanes in the total amount of C15-C18 n-alkanes and C15-C18 isoalkanes, while the percentage of C15-C18 isoalkanes refers to the percentage of C15-C18 isoalkanes in the total amount of C15-C18 n-alkanes and C15-C18 isoalkanes. This reflects the degree to which the catalyst isomerizes the feedstock. C9-C18 are the main components of bio-jet fuel products. In Table 1, C9-C18% refers to the percentage of C9-C18 obtained in the total product.

[0075] The catalyst was characterized by ICP and BET tests. For ICP testing, a small amount of catalyst was weighed, mixed with nitric acid, hydrofluoric acid, and hydrochloric acid, and digested in a microwave digester. The mixture was then diluted with deionized water before ICP testing (using an inductively coupled plasma mass spectrometer, NexION 1000G). For BET testing, 50-100 mg of the catalyst was added to a sample tube, degassed at 200℃ for 6 hours, and then the specific surface area was measured using a NOVA touchTM LX2 surface area analyzer. The results are shown in Table 2.

[0076] Table 2. ICP and BET characterization results

[0077]

[0078] The following conclusions can be drawn from the results of the embodiments and comparative examples in Tables 1 and 2:

[0079] The catalyst fixed-bed reaction results in Examples 1-4 all showed high C18 conversion, high isomer selectivity and low cracking selectivity, which enabled the production of high-quality jet fuel products in high yield.

[0080] By comparing Comparative Example 1 with Example 1, it can be found that although the amounts of nickel, cobalt and iron salts used in the preparation are similar, the actual catalyst has a lower loading capacity because a well-formed commercial support is used, resulting in poor interaction between the active components of the catalyst and the support. At the same time, its specific surface area is also lower than that of the self-made catalyst, which leads to poor conversion and selectivity of the reaction and low yield.

[0081] By comparing Comparative Example 2 with Example 1, it can be found that after preparing the unsupported catalyst without using a support, the specific surface area of ​​the catalyst is much smaller than that of the supported catalyst. This will result in fewer active sites on the catalyst surface, which in turn affects the activity and selectivity of the catalyst.

[0082] By comparing Comparative Example 3 with Example 1, it can be found that if only Ni is used as the active component without using other active components, the lack of synergistic effect between the metal active components leads to a decrease in the activity and selectivity of the catalyst.

Claims

1. A method for preparing a transition metal supported catalytic hydroisomerization catalyst, characterized in that, include: Prepare solution A by mixing nickel nitrate hexahydrate, cobalt nitrate hexahydrate, ferric nitrate nonahydrate, aluminum nitrate nonahydrate, phosphoric acid, and citric acid. Tetraethyl orthosilicate was added to anhydrous ethanol to prepare solution B; Solution A and solution B were transferred to a high-pressure reactor and reacted at 150-250℃ to obtain the catalyst precursor. The catalyst precursor was calcined at 550-650℃, and the catalyst obtained after calcination was reduced with hydrogen to obtain a transition metal supported catalytic hydroisomerization catalyst. By weight, the amount of nickel nitrate hexahydrate is any value of 8-20 parts, the amount of cobalt nitrate hexahydrate is any value of 3-10 parts, the amount of ferric nitrate nonahydrate is any value of 5-16 parts, the amount of aluminum nitrate nonahydrate is any value of 40-100 parts, the amount of phosphoric acid is any value of 5-20 parts, the amount of citric acid is any value of 5-20 parts, and the amount of tetraethyl orthosilicate is any value of 10-40 parts. The transition metal supported catalytic hydroisomerization catalyst has an ICP content of 7-15% for nickel, 2-8% for cobalt, 3-9% for iron, 12-30% for aluminum, and 4-25% for silicon.

2. The method for preparing the transition metal supported catalytic hydroisomerization catalyst according to claim 1, characterized in that, Solution A and solution B were subjected to ultrasonic treatment and then transferred to a high-pressure reactor.

3. The method for preparing the transition metal supported catalytic hydroisomerization catalyst according to claim 1, characterized in that, Solution A and solution B are transferred to a high-pressure reactor and reacted at 150-250℃ for 6-24 hours to obtain a catalyst precursor. The catalyst precursor is then extruded into shape. The extruded catalyst precursor was calcined at 550-650℃ for 2-8 hours, and the calcined catalyst was reduced with hydrogen to obtain a transition metal supported catalytic hydroisomerization catalyst.

4. The transition metal supported catalytic hydroisomerization catalyst prepared by the method according to any one of claims 1-3.

5. The transition metal supported catalytic hydroisomerization catalyst according to claim 4, characterized in that, The transition metal supported catalytic hydroisomerization catalyst has an ICP content of 7-15% for nickel, 2-8% for cobalt, 3-9% for iron, 12-30% for aluminum, and 4-25% for silicon. The specific surface area of ​​the transition metal supported catalytic hydroisomerization catalyst is 211-235 m². 2 / g.

6. The application of the transition metal supported catalytic hydroisomerization catalyst according to claim 4 or 5 in hydroisomerization catalytic reactions.

7. The application of the transition metal supported hydroisomerization catalyst according to claim 6 in hydroisomerization catalytic reactions, characterized in that, Bio-jet fuel was prepared by hydroisomerization catalysis of n-octadecane as a raw material. The product yield is 93-97%, and the C18 conversion rate is 99.15-99.61%. In bio-jet fuel, C5-C18 n-alkanes account for 26.41-28.79%, and C5-C18 isoalkanes account for 71.21-73.59%.

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