Silicon trapping agent, preparation method and application thereof

Abstract

The present invention provides a silicon scavenger, comprising alumina, pseudo-boehmite and an active component, wherein the active component is a Group VIB metal sulfide and a Group VIII metal sulfide, wherein the Group VIB metal sulfide accounts for 2-20%, the Group VIII metal sulfide accounts for 1-10%, the pseudo-boehmite content is 3-20%, and the specific surface area of ​​the silicon scavenger is 300-400m 2 / g, with a surface hydroxyl content of 1000-2000µmol / g. The silicon scavenger is prepared by impregnating and loading the active component, followed by sulfidation. Pseudoboehmite is then synthesized on the surface of the silicon scavenger using an aluminum source and a precipitant. This provides the silicon scavenger with abundant surface hydroxyl groups, thereby improving its silicon-holding capacity. Sulfidation followed by pseudoboehmite loading avoids subsequent high-temperature treatment, preventing aggregation of pseudoboehmite particles that would reduce the surface hydroxyl content. This also improves the silicon-holding capacity of the silicon-capturing catalyst. The contact surface between the metal sulfide wafer and the pseudoboehmite is increased, enhancing the synergistic effect between the catalyst's hydrogenation performance and silicon-capturing properties.

Description

Technical Field

[0001] The present invention relates to the technical field of oil hydrogenation, and in particular to a silicon scavenger, a preparation method thereof and an application thereof. Background Art

[0002] Currently, my country still has a large number of delayed coking units processing heavy, low-quality oil. Defoamers are used during this process, resulting in a certain amount of silicon in products such as coker dry gas, coker naphtha, and coker diesel. This silicon poisons the catalysts used in subsequent processing of the coker products, leading to permanent deactivation. Therefore, the hydroprocessing of coker dry gas, coker naphtha, and coker diesel requires the installation of silicon-capturing catalysts. Silicides are typically deposited on the catalyst surface by interacting with Al-OH groups. Therefore, increasing the catalyst's surface hydroxyl content can effectively increase both the catalyst's silicon capture capacity and its ability to capture silicon.

[0003] CN201410809089.6 The present invention discloses a coking gasoline desiliconization catalyst and its preparation method. The catalyst uses an Al2O3-TiO2-B2O3 composite oxide as a carrier and Ni-Mo-W-Ce as an active component. The Al2O3-TiO2-B2O3 carrier contains 10-20% TiO2 by weight, 3-10% B2O3 by weight, and the remainder is Al2O3. The active components, by weight, include 1.2-3.9% NiO, 4.2-9.5% MoO3, 5-15% WO3, and 1.5-2.5% CeO2, with the remainder being the carrier. The catalyst is calcined in a steam atmosphere, exhibiting a specific pore size and large pore volume, effectively adsorbing and removing impure silicon, protecting the subsequent coking gasoline main hydrorefining catalyst.

[0004] CN201911020775.4 discloses an oil product silicon scavenger and its preparation method. The oil product silicon scavenger includes a carrier and a hydrogenation active component, wherein the hydrogenation active component is a Group VIII metal sulfide, a Group VIB metal oxide, and a Group VIII metal oxide; based on the total weight of the silicon scavenger, the Group VIII metal sulfide is 0.1wt%-12.2wt%, the Group VIB metal oxide is 0.5wt%-17.2wt%, the Group VIII metal oxide is 0.1wt%-9.0wt%, and the carrier is 61.6%-90.3%. The preparation method includes the following: (1) impregnating the silicon scavenger carrier with an impregnation solution containing a Group VIII metal, then drying the material, and sulfurizing the dried material; (2) impregnating the material after sulfurization in step (1) with an impregnation solution containing Group VIB and Group VIII metals, and then drying and roasting under an inert atmosphere to obtain the oil product silicon scavenger.

[0005] The silicon capture catalyst of the above invention patent is prepared by impregnating active metal into alumina or modified alumina carrier. The active metal will cover part of the alumina surface, resulting in a decrease in the number of surface hydroxyl groups, leading to a decrease in the silicon capture amount and silicon capture capacity. Summary of the Invention

[0006] In view of the deficiencies of the prior art, the present invention provides a silicon scavenger, which increases the specific surface area and surface hydroxyl content of the silicon scavenger by specific means, thereby improving its silicon holding capacity.

[0007] In the context of this specification, FTIR (infrared spectroscopy) was used to analyze the hydroxyl content of the catalyst. The FTIR test conditions included: the catalyst was ground, pressed into a Φ13 mm self-supporting sheet, and placed on the in-situ cell sample holder; the experiment used a Nicolet 6700 Fourier transform infrared spectrometer with 32 scans and a resolution of 4 cm -1 , 4000~650cm -1 Measurements were made using an MCT / A detector. All infrared results were normalized based on catalyst mass. The specific surface area of ​​the silicon scavenger was analyzed using N2 adsorption / desorption. The N2 adsorption / desorption test conditions were as follows: the catalyst was loaded into a sample tube and N2 adsorption and desorption were performed using an ASAP 2420 nitrogen physical adsorption instrument (MICROMERITICS, USA) at 77K.

[0008] In order to achieve the above technical objectives, the technical solutions of the present invention are as follows:

[0009] The technical purpose of the first aspect of the present invention is to provide a silicon scavenger, comprising alumina, pseudo-boehmite and an active component, wherein the active component is a Group VIB metal sulfide and a Group VIII metal sulfide, and based on the total weight of the catalyst, the Group VIB metal sulfide is 2-20%, preferably 3-13%, the Group VIII metal sulfide is 1-10%, preferably 2-5%, and the pseudo-boehmite content is 3-20%, preferably 5-10%; the specific surface area of ​​the silicon scavenger is 300-400m 2 / g, and the surface hydroxyl content is 1000-2000µmol / g, preferably 1200-1800µmol / g.

[0010] Furthermore, the Group VIB metal sulfide and the Group VIII metal sulfide are supported on an alumina carrier, and the pseudo-boehmite is supported on the Group VIB metal sulfide, the Group VIII metal sulfide and the carrier alumina.

[0011] Furthermore, the Group VIB metal sulfide is molybdenum sulfide and / or tungsten sulfide, and the Group VIII metal sulfide is nickel sulfide and / or cobalt sulfide.

[0012] The technical purpose of the second aspect of the present invention is to provide a method for preparing the above-mentioned silicon scavenger, comprising the following steps:

[0013] (1) impregnating an alumina support with a solution containing a Group VIB metal salt and a Group VIII metal salt, drying, calcining, and sulfiding to obtain a catalyst precursor;

[0014] (2) Adding the aluminum source and the precipitant concurrently to the catalyst precursor of step (1), performing precipitation reaction, aging, filtering, washing, and drying to obtain the silicon scavenger.

[0015] Furthermore, the Group VIB metal salt in step (1) is a phosphate and / or an ammonium salt.

[0016] Furthermore, the Group VIII metal salt in step (1) is selected from one or more of nitrates, carbonates, phosphates, sulfates, basic carbonates and acetates.

[0017] Furthermore, the drying conditions of step (1) are: drying temperature 90-300°C, and drying time 3-6 hours.

[0018] Furthermore, the roasting conditions of step (1) are: roasting temperature 300-600°C, drying time 3-6 hours.

[0019] Furthermore, the vulcanization treatment in step (1) is dry vulcanization or wet vulcanization. The vulcanizing agent for dry vulcanization is hydrogen sulfide, and the vulcanizing agent for wet vulcanization is selected from one or two of carbon disulfide, dimethyl disulfide, methyl sulfide, and n-butyl sulfide; the vulcanization pressure is 2.0-6.4 MPa, the vulcanization temperature is 250-400°C, and the vulcanization time is 4-12 hours.

[0020] Furthermore, the aluminum source in step (2) is an acidic aluminum salt or an alkaline aluminum salt. When an acidic aluminum salt is used, the precipitant is selected from one or more of NaOH, NH4OH and NaAlO2; when an alkaline aluminum salt is used, the precipitant is CO2; wherein the acidic aluminum salt is selected from one or more of Al2(SO4)3, AlCl3 and Al(NO3)3, and the alkaline aluminum salt is NaAlO2; wherein the concentration of the aluminum source, calculated as alumina content, is 0.5 g / mL-10 g / mL, preferably 0.5 g / mL-2 g / mL, and the concentration of the precipitant is 0.5 g / mL-10 g / mL, preferably 0.5 g / mL-5 g / mL.

[0021] Furthermore, the conditions of the precipitation reaction in step (2) are: pH value 7.5-11, temperature 50-95° C., and time 30-120 min.

[0022] Furthermore, the aging conditions in step (2) are: temperature of 50-90° C., pH value of 7.5-11, and time of 3-24 hours.

[0023] Furthermore, the drying conditions in step (2) are as follows: drying temperature 90-300°C, drying time 2-12 hours.

[0024] Furthermore, all steps after the sulfurization treatment in step (1) are carried out under an inert atmosphere, wherein the inert atmosphere is one or more of N2 and an inert gas.

[0025] The technical purpose of the third aspect of the present invention is to provide the application of the silicon scavenger, which is used in the hydroprocessing process of silicon-containing oil products.

[0026] Furthermore, the silicon scavenger does not need to be vulcanized before use.

[0027] Compared with the prior art, the silicon scavenger of the present invention has the following advantages:

[0028] (1) The silicon scavenger of the present invention contains pseudo-boehmite components, which provide the silicon scavenger with abundant surface hydroxyl groups, thereby improving its silicon holding capacity.

[0029] (2) In the silicon scavenger of the present invention, the Group VIB metal sulfide and the Group VIII metal sulfide are loaded on an alumina carrier, and the pseudo-boehmite is loaded on the Group VIB metal sulfide, the Group VIII metal sulfide and the carrier alumina. This can increase the contact area between the pseudo-boehmite and the Group VIII metal and the Group VIB metal, improve the synergistic effect between the hydrogenation performance and the silicon capture performance of the catalyst, and improve the silicon holding capacity of the silicon capture catalyst. At the same time, it can also reduce the carbon deposition of the catalyst and prevent the carbon deposition from occupying the silicon capture active sites.

[0030] (3) In the preparation process of the silicon scavenger of the present invention, the VIB group metal and the VIII group metal are first loaded onto the carrier, which is then sulfurized to generate a large number of active metal sulfide wafers, and then the pseudo-boehmite is loaded. On the one hand, the contact surface between the pseudo-boehmite and the VIII group metal and the VIB group metal can be increased, thereby improving the synergistic effect of the hydrogenation performance and silicon capture performance of the catalyst, and improving the silicon holding capacity of the silicon capture catalyst. At the same time, the carbon deposition of the catalyst can be reduced to prevent the carbon deposition from occupying the silicon capture active sites. On the other hand, after the pseudo-boehmite is loaded, it is dried without a calcination process, thereby preventing the aggregation of the pseudo-boehmite particles from causing a decrease in the surface hydroxyl content, thereby improving the silicon holding capacity of the silicon capture catalyst. On the other hand, the catalyst of the present invention is in a sulfurized state and does not require sulfurization treatment during use, thereby preventing temperature fluctuations during the sulfurization process.

[0031] Other features and advantages of the present invention will be described in detail in the following detailed description. DETAILED DESCRIPTION

[0032] The following non-limiting examples may enable those skilled in the art to more fully understand the present invention, but are not intended to limit the present invention in any way.

[0033] The present invention uses FTIR (infrared spectroscopy) to analyze the hydroxyl content of the catalyst. The FTIR test conditions include: after the catalyst is ground, pressed into a Φ13mm self-supporting sheet, and placed on the in-situ cell sample holder. The experiment uses a Nicolet 6700 Fourier transform infrared spectrometer with 32 scans and a resolution of 4cm. -1 , 4000~650cm -1 All infrared experimental results were normalized according to the catalyst mass.

[0034] The present invention uses N2-adsorption / desorption to analyze the specific surface area of ​​the silicon capture agent. The N2-adsorption / desorption test conditions are as follows: the catalyst is loaded into a sample tube, and the ASAP 2420 nitrogen physical adsorption instrument from MICROMERITICS, USA, is used to perform N2 adsorption and desorption tests at a temperature of 77K.

[0035] In the following examples and comparative examples, the contents of metal sulfide and alumina are calculated by the feed amount, and the content of pseudo-boehmite is calculated by the weight difference between the catalyst precursor and the finally prepared silicon scavenger.

[0036] Example 1

[0037] (1) An impregnation solution containing ammonium heptamolybdate and nickel nitrate was impregnated into an alumina carrier in equal volumes. After impregnation, the carrier was dried at 110°C for 3 hours and calcined at 400°C for 3 hours. The carrier was then sulfided with hydrogen containing 1.5% H2S at a temperature of 330°C, a pressure of 3.2 MPa, and a time of 5 hours. The carrier was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0038] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 0.9 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 0.9 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 70°C and the pH value is 8.5. A coprecipitation reaction occurs for 30 minutes, and aging is continued at 70°C and pH value 8.5 for 4 hours. After filtering and washing, the silicon scavenger C-1 is obtained by drying at 110°C in a nitrogen atmosphere for 3 hours.

[0039] The weight percentages of the components in the silicon scavenger C-1 are: MoS2 is 9.3%, NiS is 4.6%, alumina is 80.9%, and pseudo-boehmite is 5.2%.

[0040] Example 2

[0041] (1) An impregnation solution containing ammonium heptamolybdate and cobalt nitrate was impregnated into an alumina support in equal volumes. After impregnation, the solution was dried at 120°C for 5 hours and calcined at 450°C for 4 hours. The solution was then sulfided with hydrogen containing 1.5% H2S at a temperature of 340°C, a pressure of 3.6 MPa, and a time of 5 hours. The solution was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0042] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 1.2 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 1.2 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.5. A coprecipitation reaction occurs for 60 minutes, and aging is continued at 80°C and pH value 8.5 for 4 hours. After filtering and washing, the silicon scavenger C-2 is obtained by drying at 100°C in a nitrogen atmosphere for 4 hours.

[0043] The weight percentages of the components in the silicon scavenger C-2 are: MoS2 is 9.6%, NiS is 3.1%, alumina is 80.5%, and pseudo-boehmite is 6.8%.

[0044] Example 3

[0045] (1) An impregnation solution containing ammonium heptamolybdate, nickel nitrate and cobalt nitrate was impregnated into an alumina support in equal volumes. After impregnation, the solution was dried at 120°C for 4 hours and calcined at 500°C for 3 hours. The solution was then sulfided with hydrogen containing 1.5% H2S at a temperature of 360°C, a pressure of 4.2 MPa and a time of 6 hours. The solution was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0046] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 0.9 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 0.9 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.5. A coprecipitation reaction occurs for 50 minutes, and aging is continued at 80°C and pH value 8.5 for 3 hours. After filtering and washing, the silicon scavenger C-3 is obtained by drying at 100°C in a nitrogen atmosphere for 5 hours.

[0047] The weight percentages of the components in the silicon scavenger C-3 are: MoS2 is 10.6%, NiS is 2.7%, CoS is 1.1%, alumina is 78.4%, and pseudo-boehmite is 7.2%.

[0048] Example 4

[0049] (1) An impregnation solution containing ammonium metatungstate and nickel nitrate was impregnated into an alumina carrier in equal volumes. After impregnation, the carrier was dried at 120°C for 4 hours and calcined at 500°C for 3 hours. The carrier was then sulfided with hydrogen containing 2.5% H2S at a temperature of 360°C, a pressure of 4.2 MPa, and a time of 4 hours. The carrier was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0050] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 1.5 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 1.5 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.5. A coprecipitation reaction occurs for 60 minutes, and the mixture is further aged at 80°C and pH value 8.5 for 3 hours. After filtering and washing, the mixture is dried at 130°C in a nitrogen atmosphere for 5 hours to obtain silicon scavenger C-4.

[0051] The weight percentages of the components in the silicon scavenger C-4 are: WS2 is 11.5%, NiS is 3.6%, alumina is 77%, and pseudo-boehmite is 7.9%.

[0052] Example 5

[0053] (1) An impregnation solution containing ammonium metatungstate and cobalt nitrate was impregnated into an alumina carrier in equal volumes. After impregnation, the carrier was dried at 120°C for 4 hours and calcined at 500°C for 3 hours. The carrier was then sulfided with aviation kerosene containing 3% carbon disulfide at a temperature of 340°C, a pressure of 4.0 MPa, and a time of 6 hours. The carrier was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0054] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 1.8 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 1.8 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.0. A coprecipitation reaction occurs for 50 minutes, and aging is continued at 80°C and pH value 8.0 for 3 hours. After filtering and washing, the silicon scavenger C-5 is obtained by drying at 100°C in a nitrogen atmosphere for 5 hours.

[0055] The weight percentages of the components in the silicon scavenger C-5 are: WS2 is 12.4%, CoS is 4.8%, alumina is 74.7%, and pseudo-boehmite is 8.1%.

[0056] Example 6

[0057] (1) An impregnation solution containing ammonium metatungstate, nickel nitrate and cobalt nitrate was impregnated into an alumina carrier in equal volumes. After impregnation, the solution was dried at 120°C for 4 hours and calcined at 500°C for 3 hours. The solution was then sulfided with aviation kerosene containing 3% carbon disulfide at a temperature of 350°C, a pressure of 4.0 MPa and a time of 6 hours. The solution was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0058] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 1.8 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 1.8 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.5. A coprecipitation reaction occurs for 80 minutes, and aging is continued at 80°C and pH value 8.5 for 3 hours. After filtering and washing, the silicon scavenger C-6 is obtained by drying at 100°C in a nitrogen atmosphere for 5 hours.

[0059] The weight percentages of the components in the silicon scavenger C-6 are: WS2 is 14.2%, NiS is 1.1%, CoS is 2.4%, alumina is 73.1%, and pseudo-boehmite is 9.2%.

[0060] Example 7

[0061] (1) An impregnation solution containing ammonium metatungstate, ammonium heptamolybdate and nickel nitrate was impregnated into an alumina carrier in equal volumes. After impregnation, the solution was dried at 120°C for 4 hours and calcined at 400°C for 3 hours. The solution was then sulfided with aviation kerosene containing 3% carbon disulfide at a temperature of 360°C, a pressure of 4.0 MPa and a time of 6 hours. The solution was then cooled to room temperature in a N2 atmosphere to obtain a catalyst precursor.

[0062] (2) Aluminum sulfate solution (wherein the aluminum oxide content is 1.0 g / mL) and sodium metaaluminate solution (wherein the aluminum oxide content is 1.0 g / mL) are added in parallel to the catalyst precursor prepared in step (1), and the temperature is controlled to 80°C and the pH value is 8.5. A coprecipitation reaction occurs for 60 minutes, and aging is continued at 80°C and pH value 8.5 for 3 hours. After filtering and washing, the silicon scavenger C-7 is obtained by drying at 100°C in a nitrogen atmosphere for 5 hours.

[0063] The weight percentages of the components in the silicon scavenger C-7 are: MoS2 is 6.1%, WS2 is 6.6%, NiS is 1.1%, alumina is 76.8%, and pseudo-boehmite is 6.3%.

[0064] Comparative Example 1

[0065] In step (1), no sulfidation treatment was performed, and the other steps were the same as in Example 1. In step (2), sulfidation treatment was performed after loading pseudo-boehmite, and the other operation processes were the same as in Example 1 to obtain a comparative silicon capture agent DC-1.

[0066] The weight percentages of the components in the comparative silicon capture agent DC-1 are as follows: MoS2 is 9.3%, NiS is 4.6%, alumina is 80.9%, and pseudo-boehmite is 5.2%.

[0067] Comparative Example 2

[0068] Step (1) is the same as in Example 1. Step (2) is to add a calcination process after drying, and the calcination conditions are 450° C. for 3 hours in a nitrogen atmosphere. The other steps are the same as in Example 1 to obtain a comparative silicon trapping agent DC-2.

[0069] The weight percentages of the components in the comparative silicon capture agent DC-2 are as follows: MoS2 is 9.3%, NiS is 4.6%, alumina is 80.9%, and pseudo-boehmite is 5.2%.

[0070] Comparative Example 3

[0071] Step (1) is the same as in Example 1. Step (2) is omitted to obtain a comparative silicon trapping agent DC-3.

[0072] The weight percentages of the components in the comparative silicon capture agent DC-3 are as follows: MoS2 is 9.3%, NiS is 4.6%, and aluminum oxide is 86.1%.

[0073] The physicochemical properties of the silicon scavengers C-1 to C-7 prepared in the above examples and the silicon scavengers DC-1 to DC-3 prepared in the comparative examples were measured, and the analysis results are shown in Table 1.

[0074] Table 1.

[0075]

[0076] Example 7

[0077] This example illustrates the silicon capture activity of the catalyst provided by the present invention for coker naphtha.

[0078] The evaluation raw oil used was coking naphtha provided by a Sinopec refinery, with the following main properties: sulfur content of 3442μg / g, nitrogen content of 89μg / g, and silicon content of 25μg / g. A 200mL fixed-bed hydrogenation unit was used to evaluate the silicon capture capacity of silicon-capturing catalysts C-1 to C-7 and comparative examples DC-1 to DC-3. DC-1 required sulfurization treatment before use, and the sulfurization conditions were as follows: sulfurization treatment was performed using aviation kerosene containing 3% carbon disulfide, the sulfurization temperature was 360°C, the sulfurization pressure was 4.0MPa, and the sulfurization time was 6h. Catalysts C-1 to C-7 and comparative examples DC-2 and DC-3 did not require pre-sulfurization treatment.

[0079] The reaction conditions for evaluation were: operating pressure 3.0 MPa, reaction temperature 300°C, hydrogen / oil volume ratio 200:1, and volume space velocity 5.0 h -1 After running for 300 hours, the silicon scavenger was unloaded and then calcined at 500℃ in a nitrogen atmosphere for 3 hours. The SiO2 content in the silicon scavenger was analyzed by XRF. The evaluation results are shown in Table 2.

[0080] Table 2.

[0081]

[0082] As can be seen from Table 2, the silicon scavenger of the present invention has a higher silicon holding capacity.

Claims

1. A silicon scavenger, characterized in that: The catalyst comprises alumina, pseudo-boehmite and an active component, wherein the active component is a metal sulfide of Group VIB and a metal sulfide of Group VIII. Based on the total weight of the catalyst, the metal sulfide of Group VIB is 2-20%, the metal sulfide of Group VIII is 1-10%, the pseudo-boehmite content is 3-20%, and the specific surface area of ​​the silicon scavenger is 300-400m 2 / g, surface hydroxyl content is 1000-2000µmol / g; The silicon scavenger is prepared by the following steps: (1) impregnating an alumina support with a solution containing a Group VIB metal salt and a Group VIII metal salt, drying, calcining, and sulfiding to obtain a catalyst precursor; (2) Adding the aluminum source and the precipitant concurrently to the catalyst precursor of step (1), performing precipitation reaction, aging, filtering, washing, and drying to obtain the silicon scavenger.

2. The silicon scavenger according to claim 1, characterized in that The Group VIB metal sulfide and the Group VIII metal sulfide are supported on an alumina carrier, and the pseudo-boehmite is supported on the Group VIB metal sulfide, the Group VIII metal sulfide and the carrier alumina.

3. The silicon scavenger according to claim 1, characterized in that The Group VIB metal sulfide is molybdenum sulfide and / or tungsten sulfide, and the Group VIII metal sulfide is nickel sulfide and / or cobalt sulfide.

4. The method for preparing the silicon scavenger according to claim 1, comprising the following steps: (1) impregnating an alumina support with a solution containing a Group VIB metal salt and a Group VIII metal salt, drying, calcining, and sulfiding to obtain a catalyst precursor; (2) Adding the aluminum source and the precipitant concurrently to the catalyst precursor of step (1), performing precipitation reaction, aging, filtering, washing, and drying to obtain the silicon scavenger.

5. The preparation method according to claim 4, characterized in that The Group VIB metal salt in step (1) is a phosphate and / or an ammonium salt.

6. The preparation method according to claim 4, characterized in that The Group VIII metal salt in step (1) is selected from one or more of nitrates, carbonates, phosphates, sulfates, basic carbonates and acetates.

7. The preparation method according to claim 4, characterized in that The drying conditions of step (1) are: drying temperature 90-300°C, and drying time 3-6 hours.

8. The preparation method according to claim 4, characterized in that The calcination conditions of step (1) are: calcination temperature 300-600°C, time 3-6 hours.

9. The preparation method according to claim 4, characterized in that The aluminum source in step (2) is an acidic aluminum salt or an alkaline aluminum salt. When an acidic aluminum salt is used, the precipitant is selected from one or more of NaOH, NH4OH and NaAlO2; when an alkaline aluminum salt is used, the precipitant is CO2.

10. The preparation method according to claim 9, characterized in that The acidic aluminum salt is selected from one or more of Al2(SO4)3, AlCl3 and Al(NO3)3, and the basic aluminum salt is NaAlO2.

11. The preparation method according to claim 9, characterized in that The concentration of the aluminum source, calculated as aluminum oxide content, is 0.5 g / mL-10 g / mL, and the concentration of the precipitant is 0.5 g / mL-10 g / mL.

12. The preparation method according to claim 4, characterized in that The conditions of the precipitation reaction in step (2) are: pH 7.5-11, temperature 50-95° C., and time 30-120 min.

13. The preparation method according to claim 4, characterized in that The aging conditions in step (2) are: temperature of 50-90° C., pH value of 7.5-11, and time of 3-24 hours.

14. The preparation method according to claim 4, characterized in that The drying conditions in step (2) are as follows: drying temperature 90-300°C, and drying time 2-12 hours.

15. The preparation method according to claim 4, characterized in that All steps after step (1) the sulfurization treatment are carried out under an inert atmosphere.

16. Use of the silicon scavenger according to claim 1 in a hydroprocessing process of silicon-containing oil products.

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