A highly dispersed natural gas hydrodesulfurization catalyst carrier, catalyst and preparation method

Abstract

The application discloses a high-dispersion natural gas hydrodesulfurization catalyst carrier, a catalyst and a preparation method. A mixed oxide solution is prepared by taking titanium isopropoxide and aluminum isopropoxide as precursors, polyalcohol as a pore-forming agent and n-propanol as a solvent; the mixed oxide solution and an ammonium carbonate solution are reacted; and a composite carrier is obtained through aging, drying and calcination. A promoter component and an active component are loaded onto the carrier by using an impregnation method, so as to obtain the high-dispersion natural gas hydrodesulfurization catalyst. The application can improve the catalytic activity, improve the space velocity of the hydrodesulfurization reaction under the premise of ensuring the utilization rate of the catalyst, and improve the production capacity of equipment.

Description

Technical Field

[0001] This invention relates to the field of natural gas hydrodesulfurization technology, specifically to a highly dispersed natural gas hydrodesulfurization catalyst support, catalyst, and preparation method. Background Technology

[0002] my country is a country with a diversified resource structure, possessing abundant reserves of coal, oil, and natural gas. In recent years, oil resources have become increasingly scarce, and coal chemical industry has stagnated due to environmental, safety, and energy consumption issues. With the growing demand for clean energy, natural gas is playing an increasingly important role in chemical production and the overall energy structure. The GB 17820-2018 standard for natural gas, promulgated and implemented in 2018, imposes stricter requirements on the total sulfur content in commercial gas from natural gas purification plants, raising the total sulfur concentration (as S) of Class I gas from no more than 60 mg / m³. 3 Increased to 20mg / m 3 Furthermore, my country's medium- to long-term goal is to control total sulfur to 8 mg / m³. 3 The introduction of this standard presents both significant opportunities and challenges for upgrading desulfurization technology in natural gas purification plants. Natural gas is primarily composed of methane, and natural gas from underground reservoirs typically contains varying levels of acidic components such as H2S, CO2, and organic sulfides (RSH, COS, RSSR, R′SR, and C4H4S). When natural gas is used as a chemical feedstock, these acidic components can cause catalyst poisoning, and corrosion of equipment and pipelines during extraction, gathering, transportation, and processing. Therefore, natural gas desulfurization is of paramount importance.

[0003] The most commonly used natural gas desulfurization method is the amine process, but its absorption of organic sulfides is limited, requiring the addition of a strong alkaline absorption process. Furthermore, amine solutions are expensive and have high consumption rates, significantly increasing operating costs. Hydrodesulfurization, on the other hand, can directly convert difficult-to-remove organic sulfides into H2S, which is then removed by a zinc oxide desulfurizing agent. Traditional natural gas hydrodesulfurization catalysts typically use Co-Mo or Fe-Mo based active components; the support is generally a porous inorganic oxide, usually one or more of alumina, silica, zirconium dioxide, or aluminosilicates; and one or more of the elements F, Si, P, Mn, Ca, and Zn are typically used as co-catalyst components.

[0004] In the aforementioned heterogeneous catalysis, the form in which the active components exist on the support surface directly affects the catalyst activity. The form in which the active components exist is closely related to the composition ratio of the impregnation solution. To prepare a highly active hydrogenation catalyst, the hydrogenation components should also have a reasonable atomic ratio. This is because the metal content has an optimal value for catalyst activity, and the reasonable atomic ratio is directly related to the composition ratio of the impregnation solution. Conventional organic sulfur hydrogenation catalysts use low space velocities, resulting in low organic sulfur conversion rates, which hinders efficient catalyst utilization and miniaturization of equipment. In most catalytic systems, the catalyst activity is not only related to the inherent catalytic activity of its active phase but also to the catalyst's texture properties (specific surface area, pore volume, pore size, etc.) and physicochemical characteristics. In heterogeneous catalytic reactions, controlling the specific surface area and pore size of the catalyst to obtain higher catalytic activity is crucial. Therefore, increasing the specific surface area of ​​the hydrogenation catalyst and increasing the contact area between organic sulfur and the active components of the catalyst has become an important research topic for natural gas hydrodesulfurization catalysts. Summary of the Invention

[0005] The present invention aims to provide a highly dispersed natural gas hydrodesulfurization catalyst support, catalyst, and preparation method, which can improve catalytic activity and achieve the goal of increasing the space velocity of the hydrodesulfurization reaction and improving equipment production capacity while ensuring catalyst utilization.

[0006] To solve the above technical problems, the specific solution adopted in this invention is as follows: a highly dispersed natural gas hydrodesulfurization catalyst support, which is a TiO2 / Al2O3 composite support, wherein the molar ratio of TiO2 to Al2O3 is TiO2 / (TiO2+Al2O3) of 0.4-0.6.

[0007] Preferably, the molar ratio of TiO2 to Al2O3 is TiO2 / (TiO2+Al2O3) = 0.5.

[0008] A method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support involves using titanium isopropoxy and aluminum isopropoxy as precursors, a polymeric alcohol as a pore-forming agent, and n-propanol as a solvent to prepare a mixed oxide solution. The mixed oxide solution is then reacted with an ammonium carbonate solution, followed by aging, drying, and calcination to obtain a composite support.

[0009] Preferably, it includes the following steps:

[0010] 1) Weigh titanium isopropoxide and aluminum isopropoxide at a mass ratio of (200-284):408 and add them to n-propanol solvent. Add a polymer alcohol at a ratio of 7.2-7.8 mL of pore-forming agent per 1.2 g of oxide to prepare a mixed oxide solution.

[0011] 2) Pour the mixed oxide solution obtained in step 1) into an ammonium carbonate solution. The resulting precipitate is aged, filtered, washed, dried and then calcined to obtain a highly dispersed natural gas hydrodesulfurization catalyst support.

[0012] Preferably, in step 1), the mass ratio of titanium isopropoxide to aluminum isopropoxide is 284:408.

[0013] Preferably, in step 1), the ratio of the added polymer alcohol is 7.5 mL of pore-forming agent for every 1.2 g of oxide.

[0014] Preferably, the pore-forming agent is one or more of polyethylene glycol, polypropylene glycol, and polyvinyl alcohol.

[0015] Preferably, in step 2), the mass ratio of ammonium carbonate to water in the ammonium carbonate solution is 1:(30-112).

[0016] Preferably, the calcination conditions in step 2) are 300-850℃ for 12-28h.

[0017] Preferably, the calcination conditions in step 2) are 350-700℃ for 20-24h.

[0018] Preferably, the aging conditions in step 2) are 0-120℃ and 0.1-24h.

[0019] Preferably, the aging conditions in step 2) are 10-90℃ for 0.5-2h.

[0020] Preferably, the drying conditions in step 2) are 80-150℃ for 0.2-50h.

[0021] Preferably, the drying conditions in step 2) are 90-120℃ for 0.5-25h.

[0022] A highly dispersed natural gas hydrodesulfurization catalyst comprises three parts: a support a, an active component b, and a co-catalyst component c. The support a is a two-component support of TiO2 and Al2O3, with TiO2 accounting for 5-80 wt% of the total catalyst mass and Al2O3 accounting for 4-57 wt% of the total catalyst mass. The active component b is a mixed component of Mo and Co, with Mo accounting for 5.0-80 wt% of the total catalyst mass and Co accounting for 0-75 wt% of the total catalyst mass. The catalyst component c is one or more of B, F, P, Si, Mn, Ca, and Zn, totaling 0-5 wt% of the total catalyst mass.

[0023] A method for preparing a highly dispersed natural gas hydrodesulfurization catalyst involves preparing a support a using the aforementioned method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support, and then loading the co-catalyst component c and the active component b onto the support a using an impregnation method, thereby obtaining the highly dispersed natural gas hydrodesulfurization catalyst.

[0024] Preferably, both the co-catalyst component c and the active component b are mixed with the carrier a in the form of soluble nitrates, and then impregnated, dried and calcined to obtain catalyst powder. The catalyst powder is mixed with a binder and deionized water to form a slurry, and the slurry is shaped and heat-treated to obtain a highly dispersed natural gas hydrodesulfurization catalyst.

[0025] Preferably, the co-catalyst component c is first mixed with the carrier a in an aqueous solution, and then ultrasonically impregnated, dried and calcined to obtain a semi-finished catalyst powder; then the active component b is mixed with the semi-finished catalyst powder in an aqueous solution, and then ultrasonically impregnated, dried and calcined to obtain an organic sulfur hydrogenation catalyst powder.

[0026] Beneficial effects

[0027] For the catalyst support in this invention, the traditional catalyst support for hydrorefining processes is γ-Al₂O₃. Studies have shown that using TiO₂ as a substitute support can increase the hydrodesulfurization activity of the catalyst by 3 to 5 times. However, TiO₂ has disadvantages such as low specific surface area and poor thermal stability, resulting in high initial activity, poor stability, and rapid deactivation of the catalyst. γ-Al₂O₃ support, on the other hand, has advantages such as high specific surface area and strong thermal stability, making it an ideal support material that can compensate for the disadvantages of TiO₂ support. Therefore, this invention combines the advantages of both supports, synthesizing a highly dispersed TiO₂ / Al₂O₃ composite support with high specific surface area through a specific method and a specific molar ratio.

[0028] Many methods have been reported to improve the specific surface area of ​​catalyst supports. Most methods adjust the specific surface area by regulating the pH during the sol-gel preparation process, and the average pore size of the support can also be improved by adding pore-expanding agents or additives. Some studies have also focused on improving the specific surface area of ​​the support by adding template agents (usually quaternary ammonium salt ions). In this invention, however, ammonium carbonate solution is used instead of water in the catalyst support preparation process. The specific interaction between ammonium carbonate and aluminum in the mixed oxides forms NH4-CO3 in the solution. 2- -Al compounds, without interacting with titanium in the mixed oxides, and subsequently NH4 during calcination. + With CO3 2- The decomposition generates gases that escape, resulting in a unique multi-level porous structure in the composite carrier, which also significantly increases the specific surface area and porosity.

[0029] Furthermore, this invention reveals that the ratio of TiO2 to Al2O3 in the catalyst support plays a crucial role in regulating the specific surface area and porosity of the support itself. In the most preferred embodiment of this invention, the obtained catalyst support exhibits optimal specific surface area and porosity. Increasing or decreasing the ratio in this most preferred embodiment reduces both the specific surface area and porosity of the obtained catalyst support. The catalyst support preparation in this invention utilizes isopropoxytitanium and isopropoxyaluminum as precursors because they possess weak Lewis acidity, enabling more efficient reaction. The polymeric alcohol pore-forming agent added during catalyst support preparation is one or more of polyethylene glycol (PEG), polypropylene glycol (PPG), and polyvinyl alcohol (PVA), which can increase the specific surface area of ​​the composite support and improve its pore structure.

[0030] For the hydrodesulfurization catalyst of this invention, because it uses a TiO2 / Al2O3 composite with a high specific surface area as a support, the presence of TiO2 not only provides more dispersion sites for the supported catalyst active components, increasing the number of catalyst active centers, but also interacts with the active components, making the active components easier to sulfide, thereby improving the hydrodesulfurization efficiency per unit mass of active components. This allows the prepared catalyst to maintain a high conversion rate of organic sulfur in natural gas even at high space velocities. Consequently, this invention has the advantages of high hydrodesulfurization conversion rate and long lifespan. Seeking catalysts with simple processes, strong feedstock adaptability, and low operating costs is of great significance for expanding the feedstock supply for hydrogen production units in oil refineries and large fertilizer plants. Attached Figure Description

[0031] Figure 1 Electron micrographs of the catalyst supports prepared in Examples 1, 4, and 5. Detailed Implementation

[0032] The following describes a highly dispersed natural gas hydrodesulfurization catalyst support and its preparation method according to the present invention through five examples (Examples 1-5). Then, based on the optimal catalyst support prepared in the five examples, three more examples (Examples 6-8) illustrate a highly dispersed natural gas hydrodesulfurization catalyst and its preparation method according to the present invention.

[0033] Example 1

[0034] 284 g of titanium isopropoxide and 408 g of aluminum isopropoxide were weighed as catalyst support precursors and added to n-propanol solvent to prepare a mixed oxide solution. 1638 mL of polypropylene glycol (PPG) was added at a ratio of 7.5 mL of pore-forming agent per 1.2 g of support oxide, followed by slow addition to 1500 mL of ammonium carbonate (NH4)2CO3 aqueous solution (where the mass ratio of (NH4)2CO3 to H2O was 1:30 to 1:112). The resulting precipitate was aged for 24 h under slow stirring, then filtered and washed at least three times. The precipitate was then dried at 110 °C for 24 h and subsequently calcined at 500 °C for 24 h to obtain a TiO2 / Al2O3 composite support powder sample. The molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3), was 0.5. This support powder sample was named ZT1.

[0035] Example 2

[0036] 200g of titanium isopropoxide and 408g of aluminum isopropoxide were weighed as catalyst support precursors and added to n-propanol solvent to prepare a mixed oxide solution. 1200mL of polypropylene glycol (PPG) was added at a ratio of 7.5mL pore-forming agent per 1.2g of support oxide, followed by slow addition to 1500mL of ammonium carbonate (NH4)2CO3 aqueous solution (where the mass ratio of (NH4)2CO3 to H2O was 1:30 to 1:112). The resulting precipitate was aged for 24h under slow stirring, then filtered and washed at least three times, and then dried at 110℃ for 24h. Finally, it was calcined at 500℃ for 24h to obtain a TiO2 / Al2O3 composite support powder sample. The molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3), was 0.4. This support powder sample was named ZT2.

[0037] Example 3

[0038] 326 g of titanium isopropoxide and 408 g of aluminum isopropoxide were weighed as catalyst support precursors and added to n-propanol solvent to prepare a mixed oxide solution. 2312 mL of polypropylene glycol (PPG) was added at a ratio of 7.5 mL of pore-forming agent per 1.2 g of support oxide, followed by slow addition to 1500 mL of ammonium carbonate (NH4)2CO3 aqueous solution (where the mass ratio of (NH4)2CO3 to H2O was 1:30 to 1:112). The resulting precipitate was aged for 24 h under slow stirring, then filtered and washed at least three times, and then dried at 110 °C for 24 h. Finally, it was calcined at 500 °C for 24 h to obtain a TiO2 / Al2O3 composite support powder sample. The molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3), was 0.6. This support powder sample was named ZT3.

[0039] Example 4

[0040] 284 g of titanium isopropoxide and 408 g of aluminum isopropoxide were weighed as catalyst support precursors and added to n-propanol solvent to prepare a mixed oxide solution. 1638 mL of polyethylene glycol (PEG) was added at a ratio of 7.5 mL pore-forming agent per 1.2 g of support oxide, followed by slow addition to 1500 mL of ammonium carbonate (NH4)2CO3 aqueous solution (where the mass ratio of (NH4)2CO3 to H2O was 1:30 to 1:112). The resulting precipitate was aged for 24 h with slow stirring, then filtered and washed at least three times. The precipitate was then dried at 110 °C for 24 h and subsequently calcined at 500 °C for 24 h to obtain a TiO2 / Al2O3 composite support powder sample. The molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3), was 0.5. This support powder sample was named ZT4.

[0041] Example 5

[0042] 284 g of titanium isopropoxide and 408 g of aluminum isopropoxide were weighed as catalyst support precursors and added to n-propanol solvent to prepare a mixed oxide solution. 1638 mL of polyvinyl alcohol (PVA) was added at a ratio of 7.5 mL of pore-forming agent per 1.2 g of support oxide, followed by slow addition to 1500 mL of ammonium carbonate (NH4)2CO3 aqueous solution (where the mass ratio of (NH4)2CO3 to H2O was 1:30 to 1:112). The resulting precipitate was aged for 24 h with slow stirring, then filtered and washed at least three times. The precipitate was then dried at 110 °C for 24 h and subsequently calcined at 500 °C for 24 h to obtain a TiO2 / Al2O3 composite support powder sample. The molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3), was 0.5. This support powder sample was named ZT5.

[0043] Figure 1Electron micrographs of TiO2 / Al2O3 composite carrier powders using polypropylene glycol (PPG), polyethylene glycol (PEG), and polyvinyl alcohol (PVA) as pore-forming agents are shown. A comparison of the composite carriers obtained in Examples 1, 4, and 5 reveals that the morphologies of the composite carriers prepared using different polyols as pore-forming agents are completely different. In Example 1, when polypropylene glycol (PPG) was used as the pore-forming agent, the carrier oxides were more uniformly dispersed. Table 1 also shows that the carrier prepared in Example 1 using polypropylene glycol (PPG) as the pore-forming agent has a higher specific surface area (380.25 m² / g) compared to the carrier prepared in Example 4 using polyethylene glycol (PEG) and the carrier prepared in Example 5 using polyvinyl alcohol (PVA). The TiO2 / Al2O3 composite carrier prepared in Example 1 also has a larger pore volume (0.57 mL / g) and an average pore size of 5.91 nm.

[0044] Table 1 Physical properties of catalyst supports

[0045] sample Sample Name Specific surface (m 2 / g) Pore ​​volume (mL / g) Average pore size (nm) Example 1 ZT1 380.25 0.57 5.91 Example 2 ZT2 358.22 0.51 5.30 Example 3 ZT3 329.10 0.40 5.21 Example 4 ZT4 371.52 0.46 5.00 Example 5 ZT5 280.42 0.36 6.13

[0046] As can be seen from the comparison of Examples 1, 2 and 3, under the same preparation conditions, the specific surface area, pore volume and average pore size of the carrier prepared when the molar ratio of TiO2 to Al2O3, TiO2 / (TiO2+Al2O3) is 0.5, are all optimal. When the molar ratio of TiO2 to Al2O3 increases or decreases, the performance of the prepared carrier decreases.

[0047] Example 6

[0048] 4.6 g of manganese nitrate and 18.3 g of zinc nitrate were weighed and uniformly dispersed in 90 mL of deionized water to prepare a mixed solution of the auxiliary components. This solution was then uniformly mixed with 80 g of TiO2 / Al2O3 composite support powder ZT1 obtained in Example 1. The mixture was then ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain a semi-finished catalyst powder. Next, 98.8 g of cobalt nitrate hexahydrate and 132.8 g of molybdenum nitrate pentahydrate were weighed and uniformly dispersed in 50 mL of deionized water to prepare a mixed solution of the active components. This semi-finished catalyst powder was then uniformly mixed with the active component solution, ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain the catalyst powder. Finally, the catalyst powder was mixed with 3.5 wt% adipic acid (an organic binder) and deionized water to form a slurry. The slurry was then shaped and dried at 105°C for 12 h and calcined at 450°C for 4 h to remove water and the organic binder, thus obtaining the shaped catalyst. This catalyst was named CAT1.

[0049] Example 7

[0050] 9.8 g of manganese nitrate and 5.8 g of zinc nitrate were weighed and uniformly dispersed in 90 mL of deionized water to prepare a mixed solution of the auxiliary components. This solution was then uniformly mixed with 80 g of TiO2 / Al2O3 composite support powder ZT1 obtained in Example 1. The mixture was then ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain a semi-finished catalyst powder. Next, 98.8 g of cobalt nitrate hexahydrate and 132.8 g of molybdenum nitrate pentahydrate were weighed and uniformly dispersed in 50 mL of deionized water to prepare a mixed solution of the active components. This semi-finished catalyst powder was then uniformly mixed with the active component solution, ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain the catalyst powder. Finally, the catalyst powder was mixed with 3.5 wt% adipic acid (an organic binder) and deionized water to form a slurry. The slurry was then shaped and dried at 105°C for 12 h and calcined at 450°C for 4 h to remove water and the organic binder, thus obtaining the shaped catalyst. This catalyst was named CAT2.

[0051] Example 8

[0052] 18.2 g of manganese nitrate and 4.6 g of zinc nitrate were weighed and uniformly dispersed in 90 mL of deionized water to prepare a mixed solution of the auxiliary components. This solution was then uniformly mixed with 80 g of TiO2 / Al2O3 composite support powder ZT1 obtained in Example 1. The mixture was then ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain a semi-finished catalyst powder. Next, 98.8 g of cobalt nitrate hexahydrate and 132.8 g of molybdenum nitrate pentahydrate were weighed and uniformly dispersed in 50 mL of deionized water to prepare a mixed solution of the active components. This semi-finished catalyst powder was then uniformly mixed with the active component solution, ultrasonically impregnated for 2 h, dried at 110 °C for 24 h, and calcined at 500 °C for 5 h to obtain the catalyst powder. Finally, the catalyst powder was mixed with 3.5 wt% adipic acid (an organic binder) and deionized water to form a slurry. The slurry was then shaped and dried at 105°C for 12 h and calcined at 450°C for 4 h to remove water and the organic binder, thus obtaining the shaped catalyst. This catalyst was named CAT3.

[0053] The component contents of the catalysts prepared in Examples 6-8 are shown in Table 2 below:

[0054] Table 2 Content of each component in the catalyst

[0055] Example Catalyst name CoO (wt%) Mo203 (wt%) MnO (wt%) ZnO (wt%) Example 6 CAT1 20 40 1 4 Example 7 CAT2 20 40 3 2 Example 8 CAT3 20 40 4 1

[0056] The catalysts prepared in Examples 6, 7, and 7 were used in natural gas hydrodesulfurization reaction experiments. The reaction performance of the catalysts is shown in Table 3 below. The reaction conditions for the natural gas hydrodesulfurization reaction were: hydrogen content in the feed gas was 0-12%, sulfur content was 60-350 ppm; reaction temperature was 300-350℃, reaction pressure was 2.0-2.5 MPa; and feed gas space velocity was 5000-20000 h⁻¹. -1 .

[0057] Table 3 Catalyst Reaction Performance

[0058] Example Catalyst name <![CDATA[Air speed (h -1 )]]> Desulfurization rate (%) Organic sulfur residue (ppm) after reaction Example 6 CAT1 20000 99.996 0.008 Example 7 CAT2 20000 99.991 0.019 Example 8 CAT3 20000 99.957 0.086

Claims

1. A highly dispersed natural gas hydrodesulfurization catalyst support, characterized in that: The TiO2 / Al2O3 composite support is used, and the molar ratio of TiO2 to Al2O3 is 0.4-0.6 for TiO2 / (TiO2+Al2O3). The preparation method of the highly dispersed natural gas hydrodesulfurization catalyst support includes the following steps: 1) Weigh titanium isopropoxide and aluminum isopropoxide at a mass ratio of (200-284):408 and add them to n-propanol solvent. Add a polymeric alcohol at a ratio of 7.2-7.8 mL of pore-forming agent per 1.2 g of carrier oxide to prepare a mixed oxide solution. The pore-forming agent is one or more of polyethylene glycol, polypropylene glycol, and polyvinyl alcohol. 2) Pour the mixed oxide solution obtained in step 1) into an ammonium carbonate solution. The resulting precipitate is aged, filtered, washed, dried and then calcined to obtain a highly dispersed natural gas hydrodesulfurization catalyst support. In step 2), the mass ratio of ammonium carbonate to water in the ammonium carbonate solution is 1:(30-112).

2. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 1, characterized in that: Includes the following steps: 1) Weigh titanium isopropoxide and aluminum isopropoxide at a mass ratio of (200-284):408 and add them to n-propanol solvent. Add a polymeric alcohol at a ratio of 7.2-7.8 mL of pore-forming agent per 1.2 g of carrier oxide to prepare a mixed oxide solution. The pore-forming agent is one or more of polyethylene glycol, polypropylene glycol, and polyvinyl alcohol. 2) Pour the mixed oxide solution obtained in step 1) into an ammonium carbonate solution. The resulting precipitate is aged, filtered, washed, dried and then calcined to obtain a highly dispersed natural gas hydrodesulfurization catalyst support. In step 2), the mass ratio of ammonium carbonate to water in the ammonium carbonate solution is 1:(30-112).

3. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: Step 1) The mass ratio of titanium isopropoxide to aluminum isopropoxide is 284:

408.

4. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: In step 1), the ratio of added polyol is 7.5 mL of pore-forming agent for every 1.2 g of carrier oxide.

5. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The roasting conditions in step 2) are 300-850℃ for 12-28h.

6. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The roasting conditions in step 2) are 350-700℃ for 20-24 hours.

7. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The aging conditions in step 2) are 0-120℃ and 0.1-24h.

8. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The aging conditions in step 2) are 10-90℃ for 0.5-2 hours.

9. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The drying conditions in step 2) are 80-150℃ for 0.2-50h.

10. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 2, characterized in that: The drying conditions in step 2) are 90-120℃ for 0.5-25h.

11. A highly dispersed natural gas hydrodesulfurization catalyst, comprising three parts: a support a, an active component b, and a co-catalyst component c, characterized in that: The support a is the highly dispersed natural gas hydrodesulfurization catalyst support as described in claim 1, with TiO2 accounting for 5-80 wt% of the total catalyst and Al2O3 accounting for 4-57 wt% of the total catalyst. The active component b is a mixed component of Mo and Co, with Mo accounting for 5.0-80 wt% of the total catalyst and Co accounting for 0-75 wt% of the total catalyst, and not being zero. The catalyst component c is one or more of B, F, P, Si, Mn, Ca, and Zn, totaling 0-5 wt% of the total catalyst, and not being zero.

12. A method for preparing a highly dispersed natural gas hydrodesulfurization catalyst, characterized in that: The carrier a is prepared by any of the preparation methods of the highly dispersed natural gas hydrodesulfurization catalyst support described in claims 2-10, and the co-catalyst component c and active component b are loaded onto the carrier a by impregnation method, thereby obtaining the highly dispersed natural gas hydrodesulfurization catalyst.

13. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst as described in claim 12, characterized in that: Both the co-catalyst component c and the active component b are mixed with the support a in the form of soluble nitrates. The mixture is then impregnated, dried, and calcined to obtain catalyst powder. The catalyst powder is mixed with a binder and deionized water to form a slurry. The slurry is then shaped and heat-treated to obtain a highly dispersed natural gas hydrodesulfurization catalyst.

14. The method for preparing a highly dispersed natural gas hydrodesulfurization catalyst as described in claim 13, characterized in that: First, the aqueous solution of co-catalyst component c is mixed with carrier a, and then ultrasonically impregnated, dried and calcined to obtain a semi-finished catalyst powder; then the aqueous solution of active component b is mixed with the semi-finished catalyst powder, and then ultrasonically impregnated, dried and calcined to obtain the catalyst powder.

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