An oxidation desulfurization catalyst, a preparation method and application thereof

Abstract

The application discloses an oxidative desulfurization catalyst, which is a litchi shell activated carbon loaded with phosphomolybdic acid; the litchi shell activated carbon is prepared by activating litchi shell carbon. The phosphomolybdic acid is loaded on the litchi shell activated carbon carrier, which not only combines with the oxygen-containing functional groups on the surface of the litchi shell activated carbon, but also disperses the HPMo on the surface of the litchi shell activated carbon carrier, so that more HPMo acid centers are provided for the oxidation reaction, and the catalytic oxidative desulfurization activity is good. The oxidative desulfurization catalyst is prepared by the impregnation method, the phosphomolybdic acid is easy to be loaded on the surface of the litchi shell activated carbon, and the Keggin structure of the phosphomolybdic acid is not destroyed, that is, the HPMo molecules with the complete Keggin structure exist on the catalyst, the Mo(VI) sites of the HPMo molecules can interact with the oxidant hydrogen peroxide to produce active free radical species, so that the desulfurization efficiency is effectively improved.

Description

Technical Field

[0001] This invention relates to the field of catalytic desulfurization technology, specifically to an oxidative desulfurization catalyst, its preparation method, and its application. Background Technology

[0002] The use of sulfur-containing fuel oil will cause a series of problems, such as SO2 produced by the combustion of sulfur-containing fuel oil. x This not only leads to permanent poisoning of the catalyst in the vehicle's exhaust purification system, significantly reducing its effectiveness in treating NOx in the exhaust, but also contributes to acid rain and acid fog, causing environmental pollution. The main sulfur-containing compounds in fuel oil include: thiols, sulfides, disulfides, tetrahydrothiophene, thiophene, benzothiophene (BT), dibenzothiophene (DBT), methyldibenzothiophene, and 4,6-dimethylbenzothiophene.

[0003] Depending on the characteristics of the sulfides contained in the oil, different physical or chemical methods can be used for desulfurization. Currently, catalytic hydrogenation, catalytic oxidation, complexation, solvent extraction, and alkaline treatment are commonly used technologies for reducing the sulfur content of oil. With increasingly stringent restrictions on the sulfur content in oil, deep desulfurization will become an essential step in the production of clean oil products. Hydrodesulfurization (HDS) is a mature diesel desulfurization technology, but it has disadvantages such as difficulty in removing thiophene organic sulfur, high hydrogen consumption, large investment in equipment, and harsh operation. Oxidative desulfurization (ODS) technology can oxidize sulfur-containing compounds into highly polar sulfones under normal pressure and near-normal temperature conditions, and then achieve deep desulfurization through extraction, adsorption, and filtration. It has a high removal efficiency for DBT, which is difficult to remove by catalytic hydrogenation, and can meet the requirements of ultra-deep desulfurization. Compared with hydrodesulfurization, oxidative desulfurization requires less investment, does not use expensive hydrogen sources, and has milder reaction conditions, making it a green desulfurization process. Current research uses carbonaceous materials such as activated carbon and carbon black as catalysts for oxidative desulfurization, but the current activated carbon catalysts have only moderate catalytic desulfurization effects, and further research is needed to develop activated carbon catalysts with high catalytic efficiency. Summary of the Invention

[0004] To overcome the problems existing in the prior art, one objective of this invention is to provide an oxidative desulfurization catalyst. A second objective is to provide a method for preparing the aforementioned oxidative desulfurization catalyst. A third objective is to provide applications of the aforementioned oxidative desulfurization catalyst. A fourth objective is to provide a method for desulfurizing petroleum products.

[0005] To achieve the above objectives, the technical solution adopted by the present invention is as follows:

[0006] The first aspect of the present invention provides an oxidative desulfurization catalyst, wherein the oxidative desulfurization catalyst is litchi shell activated carbon supported on phosphomolybdic acid; the litchi shell activated carbon is obtained by activating litchi shell carbon.

[0007] Preferably, the mass ratio of litchi shell activated carbon to phosphomolybdic acid in the litchi shell activated carbon loaded with phosphomolybdic acid is (0.1-0.5):1.

[0008] Preferably, the litchi shell activated carbon contains HPMo molecules with a complete Keggin structure.

[0009] More preferably, the diameter of the HPMo molecule is 3-5 nm.

[0010] A second aspect of the present invention provides a method for preparing the above-mentioned oxidative desulfurization catalyst, comprising the following steps:

[0011] S1. Litchi shell activated carbon is prepared by mixing litchi shell charcoal with an activator and heating to react.

[0012] S2. The litchi shell activated carbon is impregnated in a phosphomolybdic acid solution, filtered and dried to obtain litchi shell activated carbon loaded with phosphomolybdic acid, which is an oxidative desulfurization catalyst.

[0013] Preferably, the litchi shell charcoal is prepared by the following steps: litchi shells are washed, dried, and ground to obtain litchi shell powder, which is then kept at 500-600℃ in an argon atmosphere for 2-3 hours to obtain litchi shell charcoal. More preferably, the particle size of the litchi shell powder is less than 50-60 mesh.

[0014] Preferably, the activator is potassium carbonate or potassium hydroxide.

[0015] Preferably, the mass ratio of the activator to the litchi shell charcoal is (2-4):1.

[0016] Preferably, in step S1, the heating rate is 5-10℃ / min.

[0017] Preferably, in step S1, the reaction temperature is 600-800℃.

[0018] Preferably, in step S1, the reaction time is 0.5-2 hours.

[0019] Preferably, in step S1, the litchi shell activated carbon also undergoes a drying process. More preferably, the drying process involves baking at 100-150°C for 10-15 hours.

[0020] Preferably, in step S2, the concentration of the phosphomolybdic acid solution is 0.001-0.02 g / mL.

[0021] More preferably, the solute used in the phosphomolybdic acid solution is phosphomolybdic acid hydrate, and the purity of the phosphomolybdic acid hydrate is Mo: 45%-63%.

[0022] Preferably, in step S2, the solvent for the phosphomolybdic acid solution is water.

[0023] Preferably, in step S2, the immersion temperature is room temperature.

[0024] Preferably, in step S2, the soaking time is 10-15 hours.

[0025] The third aspect of the present invention provides the application of the above-mentioned oxidative desulfurization catalyst in the oxidative desulfurization of catalytic oil products.

[0026] The fourth aspect of the present invention provides a method for desulfurizing petroleum products, comprising the following steps: contacting petroleum products containing sulfur compounds with an oxidant and the above-mentioned oxidative desulfurization catalyst to perform desulfurization.

[0027] Preferably, the sulfur compound is selected from at least one of thiophenes, benzothiophenes, and dibenzothiophenes.

[0028] More preferably, the concentration of the sulfur compound in the petroleum product is 200-2000 ppm.

[0029] Preferably, the oxidant is selected from one or more of hydrogen peroxide, ozone, and chloric acid.

[0030] More preferably, the ratio of the oxidative desulfurization catalyst to the oxidant is 1g:(0.1-0.4)mL.

[0031] The beneficial effects of this invention are:

[0032] This invention provides an oxidative desulfurization catalyst, wherein the oxidative desulfurization catalyst is litchi shell activated carbon supported on phosphomolybdic acid. The phosphomolybdic acid supported on the litchi shell activated carbon carrier not only combines with the oxygen-containing functional groups on the surface of the litchi shell activated carbon, but also utilizes the litchi shell activated carbon carrier to highly disperse HPMo on its surface, providing more HPMo acidic centers for the oxidation reaction. As the HPMo loading increases, its acidity increases, and it has better catalytic oxidative desulfurization activity.

[0033] Compared with the prior art, the present invention also has the following beneficial effects:

[0034] 1) In this invention, molybdate is directly loaded onto litchi shell activated carbon. HPMo is uniformly dispersed on the surface and in the pores of the activated carbon without clogging the pore structure of the activated carbon. This provides a reaction site for the smooth diffusion process of organic sulfides and is more conducive to the oxidative desulfurization reaction to a certain extent.

[0035] 2) This invention uses an impregnation method to prepare an oxidative desulfurization catalyst. Phosphomolybdic acid is easily loaded onto the surface of litchi shell activated carbon, and the Keggin structure of phosphomolybdic acid is not broken. That is, there are HPMo molecules with complete Keggin structure on the catalyst. The Mo(VI) sites of HPMo molecules can interact with the oxidant hydrogen peroxide to generate active free radical species, thereby effectively improving the desulfurization efficiency, which can reach up to 99.5%. Attached Figure Description

[0036] Figure 1 Infrared spectra of catalysts with different loadings and pure HPMo;

[0037] Figure 2 BET plots for catalysts with different loadings and pure HPMo;

[0038] Figure 3 Pore ​​size distribution diagrams for catalysts with different loadings and pure HPMo;

[0039] Figure 4 XRD patterns of catalysts with different loadings and pure HPMo;

[0040] Figure 5 SEM characterization of HPMo; where a1 is the surface morphology magnified 1000 times and a2 is the surface morphology magnified 5000 times;

[0041] Figure 6 SEM characterization of A-LC; where b1 is the surface morphology magnified 3000 times and b2 is the surface morphology magnified 5000 times;

[0042] Figure 7 SEM characterization of 20% HPMo / A-LC; where c2 is the surface morphology magnified 5000 times and c3 is the surface morphology magnified 10000 times;

[0043] Figure 8 SEM characterization of 30% HPMo / A-LC; where d2 is the surface morphology magnified 5000 times and d3 is the surface morphology magnified 10000 times;

[0044] Figure 9 SEM characterization of 40% HPMo / A-LC; where e2 is the surface morphology magnified 5000 times and e3 is the surface morphology magnified 10000 times;

[0045] Figure 10 The effects of different experimental conditions on the catalytic oxidation desulfurization effect were investigated, including (a) HPMo loading; (b) catalyst dosage; (c) initial sulfur content; (d) extractant dosage; (e) reaction temperature; and (f) oxygen-sulfur molar ratio. Detailed Implementation

[0046] The present invention will be further described in detail below through specific embodiments. Unless otherwise specified, the raw materials used in the following embodiments can be obtained from conventional commercial channels or prepared and isolated through simple synthesis; unless otherwise specified, the processes employed are conventional processes in the art.

[0047] All solvents and reactants used in the following examples did not require further purification. The hydrogen peroxide solution concentration was 30%, the acetonitrile concentration was 99.9%, the purity of phosphomolybdic acid hydrate was Mo: 45%-63%, and p-benzoquinone and isopropanol were from Aladdin Holdings Group Limited. Lychee peels were purchased from Dashenlin Pharmaceutical Group Limited.

[0048] Example 1

[0049] Take 100g of lychee shells, rinse with tap water to remove dust particles, and dry in an oven at 80℃ for 24 hours. Grind into a fine powder, pass through a 50-60 mesh sieve, place in a ceramic boat, and put into a tube furnace. After evacuation, introduce argon gas for protection. Set the heating rate of the tube furnace to 5℃ / min for 100min, and hold at 500℃ in an argon atmosphere for 2.5 hours to obtain lychee shell charcoal powder. Approximately 3.4g of lychee shell charcoal powder is obtained from 10g of lychee shell powder. Using potassium carbonate as an activator, weigh appropriate amounts of potassium carbonate and lychee shell charcoal powder into a beaker according to a potassium carbonate:lychee shell charcoal powder ratio of 2.5:1, stir evenly, and place in a vacuum tube furnace. Set the heating program to 7℃ / min and hold at 700℃ for 1 hour to obtain black charcoal powder. The solution was repeatedly washed with deionized water until the pH value was neutral, and then placed in an oven at 120°C for 12 hours until constant weight was achieved, and then removed to obtain litchi shell activated carbon (A-LC).

[0050] Litchi shell carbon-based / phosphomolybdic acid catalysts with different loadings were prepared using an equal-volume impregnation method. The specific steps are as follows: First, according to the required experimental loading, an appropriate amount of phosphomolybdic acid was weighed and dissolved in a certain amount of deionized water. Then, an appropriate amount of activated carbon support was weighed, impregnated and stirred at room temperature for 12 hours, and then dried in an oven at 120℃ for 6 hours to obtain the litchi shell carbon-based phosphomolybdic acid catalyst. For example, 0.4 g of phosphomolybdic acid hydrate was weighed into 30 mL of deionized water and magnetically stirred at room temperature for 2 hours until fully dissolved. Next, 1.0 g of A-LC was weighed and poured into the dissolved phosphomolybdic acid solution, and magnetically stirred at room temperature for 12 hours until fully adsorbed. Then, it was placed in an oven and dried at 120℃ for 6 hours to obtain the litchi shell carbon-based phosphomolybdic acid catalyst (denoted as 40% HPMo / A-LC). Repeat the above steps to prepare 20% ωt HPMo / A-LC, 30% ωt HPMo / A-LC, and 40% ωt HPMo / A-LC catalysts, respectively.

[0051] Example 2

[0052] The preparation process of the litchi shell carbon-based phosphomolybdic acid catalyst is the same as that in Example 1, except that the amount of phosphomolybdic acid hydrate used is 0.2g. The litchi shell carbon-based phosphomolybdic acid catalyst is denoted as 20%HPMo / A-LC.

[0053] Example 3

[0054] The preparation process of the litchi shell carbon-based phosphomolybdic acid catalyst is the same as that in Example 1, except that the amount of phosphomolybdic acid hydrate used is 0.3g. The litchi shell carbon-based phosphomolybdic acid catalyst is denoted as 30%HPMo / A-LC.

[0055] Catalyst characterization

[0056] XRD patterns of the samples were recorded using an X-ray diffractometer manufactured by PANalytical, Netherlands. Ni filter material and Cu K were used. α The radiation source was set with a tube voltage of 45 kV and a tube current of 40 mA, and data were acquired in the range of 10°–80° with a step size of 0.02° / s. A Tianjin Gangdong Technology Co., Ltd. HW-10 Fourier transform infrared spectrometer was used, with a wavenumber range of 4000–6000 cm⁻¹, 32 scans, a measurement accuracy of 0.01 cm⁻¹, and a resolution higher than 4 cm⁻¹. -1 Specific surface area and pore size analysis (BET) characterization were performed using a BSD-660 series physical adsorption analyzer (automated adsorption type) from Best Instruments Technology (Beijing) Co., Ltd. Surface morphology was measured using an S-4800 scanning electron microscope manufactured by Hitachi Optical & Electronics Co., Ltd., Japan.

[0057] 1. Infrared Spectroscopy (FT-IR) Characterization

[0058] Figure 1 The FT-IR spectra of HPMo, 40% HPMo / A-LC, 30% HPMo / A-LC, 20% HPMo / A-LC, and A-LC are shown. The FT-IR spectra of 40% HPMo / A-LC, 30% HPMo / A-LC, and 20% HPMo / A-LC are shown in the range of 700–1100 cm⁻¹. -1 The four characteristic absorption peaks of the Keggin structure appear at 1044 cm⁻¹. -1 (PO), 967cm -1 (Mo=O), 878cm -1 (Mo-Ob-Mo) and 722cm -1 (Mo-Oc-Mo) indicates that the Keggin structure of phosphomolybdic acid on the A-LC surface remains intact, preserving the Keggin structure, meaning that HPMo molecules with a complete Keggin structure exist on the catalyst. Furthermore, the 967 cm⁻¹ of the loaded catalyst... -1The red shift in the (Mo=O band) indicates that the strength of the Mo=O bond weakens and the oxygen supply activity increases when activated carbon is used as a support, which is beneficial for oxidative desulfurization.

[0059] 2. BET characterization

[0060] Before the test, the sample was vacuum degassed at 120℃ for 6 hours to remove volatile substances and moisture that may be contained in the catalyst. Figure 2 The treated A-LC activated carbon and its phosphomolybdic acid-supported catalyst both exhibited a type I IUPAC isotherm and contained micropores. Activated carbon prepared from litchi shells and its phosphomolybdic acid-supported catalyst also showed micropores and mesopores. Furthermore, the adsorption plateaus of the activated carbon and its HPMo catalysts with different loadings were not completely horizontal, all exhibiting an H4-type hysteresis loop. Under relatively low pressures (P / P0), the adsorption capacities of the A-LC, 20% HPMo / A-LC, 30% HPMo / A-LC, and 40% HPMo / A-LC catalysts increased rapidly, possibly due to the rapid occupation of adsorption sites on the activated carbon, reaching 100 cm⁻¹. 3 After / g, the isotherm flattens out with increasing relative pressure, possibly due to the filling of micropores in the catalyst caused by the reduction of adsorption sites. The HPMo adsorption-desorption isotherm starts from 0 and gradually increases with pressure, but its adsorption capacity is much smaller than other samples. The linear adsorption-desorption isotherm of HPMo indicates that its specific surface area is too small. Table 1 lists the specific surface area and pore structure of five samples, revealing that the A-LC loaded with HPMo has a smaller surface area and fewer adsorption sites compared to the unloaded A-LC.

[0061] Further analysis, Figure 3 The pore size distributions of catalysts with different loadings and pure HPMo are shown in Table 1, which displays the specific surface area and pore structure. Figure 3 As shown in Table 1, micropores and mesopores exist in all catalysts, with a relatively dense distribution of micropores. Furthermore, the 20% HPMo / A-LC, 30% HPMo / A-LC, and 40% HPMo / A-LC catalysts mainly have pores at 2.7 nm, exhibiting a narrow pore size distribution. Micropores and mesopores are present in A-LC and HPMo and their loadings, and their distribution gradually becomes sparser with increasing average pore size. Pore volume is directly proportional to pore size; as pore size increases, pore volume increases. Compared to A-LC, HPMo supported on activated carbon with different loadings exhibits a more dense micropore distribution.

[0062] Table 1 Specific surface area and pore structure

[0063]

[0064] 3. XRD characterization

[0065] from Figure 4 The characteristic peaks of the Keggin structure of HPMo can be observed. For HPMo, 2θ diffraction peaks appear at 7-10°, 1-22°, and 25-30°, within which diffraction peaks of MoO3 units are present. However, these characteristic peaks are not observed or are not obvious on HPMo / A-LC, indicating that HPMo clusters are well dispersed on the A-LC support. This further demonstrates that HPMo is easily loaded onto the A-LC support and thus binds to the functional groups on the A-LC surface, exhibiting good catalytic oxidative desulfurization activity. Then, the loading of HPMo on A-LC with different loading amounts was determined. Characteristic diffraction peaks of A-LC are observed at 20% ωt HPMo / A-LC, 30% ωt HPMo / A-LC, and 40% ωt HPMo / A-LC. Due to the large specific surface area of ​​A-LC, it can fully accommodate HPMo molecules, allowing HPMo to enter the pore structure of A-LC. However, the characteristic peaks of the Keggin structure of catalysts with different HPMo loadings were not obvious. This may be due to insufficient phosphomolybdic acid loading, resulting in only a thin film forming on the surface. Another reason is that HPMo molecules bind to oxygen-containing functional groups on the A-LC surface, causing the crystal phase to be obscured and thus making the Keggin structure less obvious.

[0066] 4. SEM characterization

[0067] To more intuitively represent the pore structure and surface morphology of the HPMo / A-LC catalyst, scanning electron microscopy (SEM) images were used for characterization. The working distance of the SEM was 10.1 mm, the accelerating voltage was 20 kV, and the beam size was 6.0 mm. Figure 5-9 The figures shown are at magnifications of 3000x, 5000x, and 10000x for HPMo, A-LC, 20% ωt HPMo / A-LC, 30% ωt HPMo / A-LC, and 40% ωt HPMo / A-LC, respectively. From... Figure 5-9 As can be seen, all three catalysts with different HPMo loadings exhibit abundant pore structures. HPMo is uniformly dispersed on the surface and within the pores of the A-LC, achieving not only uniform coverage but also preventing clogging of the A-LC's pore structure. This provides a suitable reaction site for the diffusion of organosulfur compounds, thus favoring the oxidative desulfurization reaction to a certain extent. Compared to pure HPMo, the A-LC support highly disperses HPMo on its surface, providing more HPMo acidic centers for the oxidation reaction. With increasing HPMo loading, the acidity increases, leading to improved catalyst activity and consequently, a higher oxidative desulfurization rate.

[0068] Desulfurization Experimental Analysis

[0069] 1. Experimental conditions

[0070] To prepare 500 mL of model oil with a sulfur content of 500 ppm: Weigh 1.4395 g of DBT and dissolve it in 10 mL of tetradecane in a 500 mL volumetric flask, then dilute to the mark with n-decane.

[0071] A dry three-necked flask was filled with 0.04 g of catalyst, 10 mL of 500 ppm model oil, 5.0 mL of acetonitrile extractant, and 0.12 mL of 30% H₂O₂. The mixture was stirred magnetically at a constant temperature and speed, and then refluxed. Samples (0.5 mL each) were collected at 15 min, 30 min, 45 min, 60 min, 75 min, and 90 min. After centrifugation, the upper organic phase was analyzed by gas chromatography to calculate the desulfurization rate. Sulfur content was determined using an Agilent Technologies 7820A gas chromatograph with a 1 μL needle and 5 cm needle length Microliter Syringes microsyringe. The desulfurized catalyst was recovered by centrifugation, and the oil phase was collected, washed three times in acetonitrile (MeCN), dried in an oven, and reused under the same conditions to study the catalyst's reusability.

[0072] Based on the above catalytic oxidation desulfurization experiments, p-benzoquinone and isobutanol were used to capture superoxide anion radicals and hydroxyl radicals, respectively, under optimal desulfurization conditions.

[0073] The centrifuged sample was analyzed using a gas chromatograph. The desulfurization rate of the sample after the reaction can be calculated using the following formula:

[0074]

[0075] Where C0 is the initial sulfur concentration of the simulated oil, mg / L; C A The value represents the sulfur concentration of the oil sample after the reaction, in mg / L.

[0076] 2. Experimental Results

[0077] The effects of HPMo loading, catalyst dosage, initial sulfur content, extractant dosage, reaction temperature, and oxygen-sulfur molar ratio on the oxidative desulfurization performance of simulated oil were investigated. Optimal reaction conditions were selected for further research, and the results are as follows: Figure 10 As shown, the results indicate that the optimal desulfurization conditions are: HPMo loading of 40% ( Figure 10 a) The catalyst dosage is 0.03-0.06g ( Figure 10 b) The initial sulfur content is 200-1500 ppm. Figure 10 c), the amount of extractant used is 5 mL ( Figure 10 d), the reaction temperature is 55-70℃ ( Figure 10 e), hydrogen peroxide is used as the oxidant and the oxygen-sulfur molar ratio is 3:1. Figure 10 f). Under the above-mentioned optimal desulfurization conditions, the desulfurization rate of 40% HPMo / A-LC reaches as high as 99.5%.

[0078] The above embodiments are preferred embodiments of the present invention, but the embodiments of the present invention are not limited to the above embodiments. Any changes, modifications, substitutions, combinations, or simplifications made without departing from the spirit and principle of the present invention shall be considered equivalent substitutions and shall be included within the protection scope of the present invention.

Claims

1. An oxidative desulfurization catalyst, characterized in that, The oxidative desulfurization catalyst is litchi shell activated carbon supported on phosphomolybdic acid; the litchi shell activated carbon is obtained by activating litchi shell carbon. The preparation method of the oxidative desulfurization catalyst includes the following steps: S1. Litchi shell activated carbon is prepared by mixing litchi shell charcoal with an activator and heating to react. S2. The litchi shell activated carbon is impregnated in a phosphomolybdic acid solution, filtered and dried to obtain litchi shell activated carbon loaded with phosphomolybdic acid, i.e., an oxidative desulfurization catalyst. The activator is potassium carbonate.

2. The oxidative desulfurization catalyst according to claim 1, characterized in that, The mass ratio of litchi shell activated carbon to phosphomolybdic acid in the litchi shell activated carbon loaded with phosphomolybdic acid is (0.1-0.5):

1.

3. The method for preparing the oxidative desulfurization catalyst according to claim 1 or 2, characterized in that, The steps include the following: S1. Litchi shell activated carbon is prepared by mixing litchi shell charcoal with an activator and heating to react. S2. The litchi shell activated carbon is impregnated in a phosphomolybdic acid solution, filtered and dried to obtain litchi shell activated carbon loaded with phosphomolybdic acid, which is an oxidative desulfurization catalyst.

4. The method for preparing the oxidative desulfurization catalyst according to claim 3, characterized in that, The mass ratio of the activator to the litchi shell charcoal is (2-4):

1.

5. The method for preparing the oxidative desulfurization catalyst according to claim 3, characterized in that, In step S1, the conditions for the heating reaction are selected from one or more of the following; A) The heating rate is 5-10 ℃ / min; B) The reaction temperature is 600-800℃; C) The reaction time is 0.5-2 h.

6. The method for preparing the oxidative desulfurization catalyst according to claim 3, characterized in that, In step S2, the concentration of the phosphomolybdic acid solution is 0.001-0.02 g / mL; And / or, the solvent for the phosphomolybdic acid solution is water.

7. The application of the oxidative desulfurization catalyst according to claim 1 or 2 in the oxidative desulfurization of catalytic oil products.

8. A method for desulfurizing petroleum products, characterized in that, The process includes the following steps: contacting petroleum products containing sulfur compounds with an oxidant and the desulfurization catalyst described in claim 1 or 2 to carry out desulfurization.

9. The method for desulfurizing petroleum products according to claim 8, characterized in that, The sulfur compound is selected from at least one of thiophene compounds, benzothiophene compounds, and dibenzothiophene compounds.

10. The method for desulfurizing petroleum products according to claim 8, characterized in that, The oxidant is selected from one or more of hydrogen peroxide, ozone, and chloric acid.

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