Novel catalyst for treating industrial silane-containing waste gas as well as preparation method and application thereof

Abstract

The invention discloses a novel efficient catalyst for treating industrial silane-containing waste gas as well as a preparation method and application of the novel efficient catalyst, which can realize deep treatment of the industrial silane-containing waste gas. After industrial waste gas containing hexamethyldisiloxane, allyldimethylsiloxane and trimethoxysilane is treated by the catalyst under the application condition, the silane removal rate reaches 99% or above, the silane content of the tail gas is lower than 0.001 mg / m < 3 >, and the requirements of follow-up waste gas treatment facilities such as CO, RCO and RTO can be met.

Description

Technical Field

[0001] The invention relates to the field of waste gas treatment, and in particular to a high-efficiency catalyst for removing silane, a preparation method and application thereof. Background Art

[0002] In the chemical production process, due to the addition of specific products and catalysts in the front end, the tail gas at the rear end contains silane components. When this component enters the CO, RCO, RTO and activated carbon waste gas treatment facilities for treatment, it will further decompose to form silicon-containing substances, causing the CO and RCO catalysts to deactivate rapidly, and causing the RCO and RTO ceramic heat storage bodies to become blocked, resulting in an increase in bed pressure and a rapid decrease in waste gas treatment efficiency.

[0003] The traditional method of treating silane-containing waste gas is generally to use an incinerator for incineration. However, a large amount of silica powder will be produced during the incineration of silane-containing waste gas, which will lead to problems such as pipe blockage, increased difficulty in cleaning the furnace, increased content of particulate matter in exhaust emissions, and frequent replacement of exhaust filters. Summary of the invention

[0004] In order to solve the problems of high cost and serious catalyst poisoning in the existing industrial silane-containing waste gas treatment, the purpose of the present invention is to provide a new and efficient desilanization catalyst for treating industrial silane-containing waste gas.

[0005] The catalyst can completely remove the silane component in the exhaust gas, reduce the occurrence of catalyst poisoning or heat accumulator blockage problems in the exhaust gas treatment facility, and maintain high-efficiency operation for a long time.

[0006] To achieve the above-mentioned purpose, the present invention is implemented through the following technical solutions.

[0007] In one aspect, the present invention provides a method for preparing a catalyst for treating industrial silane-containing waste gas, the preparation method comprising the following steps:

[0008] (1) dissolving a catalyst active component, a catalyst promoter component and a catalyst site regulator in a dispersant to obtain an impregnation solution;

[0009] (2) fully mixing the impregnation solution obtained in step (1) with the carrier powder and the binder to form a slurry;

[0010] (3) uniformly coating the obtained slurry on the surface of the honeycomb-shaped regular ceramic, or uniformly filling the slurry into a mold for stamping;

[0011] (4) drying the honeycomb-shaped regular catalyst precursor obtained in step (3) to remove free water, crystal water and volatile substances inside the catalyst;

[0012] (5) The catalyst obtained in step (4) needs to be impregnated and activated in a catalyst activation solution;

[0013] (6) The honeycomb structured catalyst obtained in step (5) is subjected to a calcination treatment.

[0014] In the present invention, the catalyst active component in step (1) is selected from one or two of nitrates, sulfates or chlorides of Fe 2+ , Co 2+ , Ni 2+ , Cu 2+ , Mn 2+ ; the catalyst promoter component is selected from one or two of nitrates, sulfates or chlorides of Ce 3+ , Nb 3+ , Eu 3+ , Ho 3+ ; the ion concentration of the catalyst active component is 10 - 300 g / L, and the ion concentration of the catalyst promoter component is 1 - 100 g / L.

[0015] In the present invention, the pH of the impregnation solution is controlled at 2 - 9, and the temperature of the impregnation solution is 40 - 80 °C. The pH can be adjusted by using one or a combination of two or more of ammonia water, sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, hydrochloric acid, sulfuric acid, nitric acid.

[0016] In the present invention, in step (1), the metal ions are dispersed uniformly in the impregnation solution by means of mechanical vibration, stirring, ultrasonic waves, etc.

[0017] In the present invention, the dispersion equipment used in the dispersion process in step (1) is equipment such as an ultrasonic cleaner, a mechanical shaker, a magnetic stirrer, a mechanical stirrer, etc., and the temperature control uses equipment such as a constant temperature water bath, a circulating water bath, an electric heater, etc.

[0018] In the present invention, in step (2), the impregnation duration is 10 - 120 min, the carrier powder is selected from one of titanium oxide, aluminum oxide, cerium oxide, pseudoboehmite, molecular sieve; the binder is selected from one of sodium tungstate, tungsten oxide, potassium chloride, potassium nitrate.

[0019] In the present invention, in step (3), the honeycomb structured ceramic is selected from structured ceramics made of cordierite and diatomite; the coating thickness is 0.1 - 5 mm; the stamping pressure for stamping is 1 - 500 MPa.

[0020] In the present invention, in step (4), the heating rate during drying is 1 - 20 °C / min; the drying temperature is 100 - 500 °C, the drying duration is 1 - 10 h, and the drying process is carried out in an atmosphere of N2, air, Ar or He.

[0021] In the present invention, the main components of the activation solution in step (5) are a solution containing one or more of Fe 2+ , Ni 2+ , Cu 2+ , Zn 2+ , Mn 2+ , Ce 3+ , Nb 3+ , and a solution containing one or more of the ionic regulator solutions of Na + , K + , respectively derived from corresponding metal nitrates, sulfates, chlorides and other substances; the concentration of the main component metal ions in the activation solution is 1 - 200 g / L, the concentration of the catalyst regulator ions is 0.1 - 10 g / L, and the pH of the activation solution is controlled at 2 - 7. The pH is adjusted by using one or more combinations of ammonia water, sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, hydrochloric acid, sulfuric acid, nitric acid.

[0022] In the present invention, the activation temperature in step (5) is 20 - 60 °C, and the activation time is 10 - 120 min.

[0023] In the present invention, the calcination temperature in step (6) is 300 - 800 °C, and the calcination duration is 1 - 10 h.

[0024] In the present invention, the calcination process in step (6) needs to be carried out in an atmosphere of NH3, N2, air, Ar or He, and the heating rate is 1 - 20 °C / min.

[0025] In the second aspect of the present invention, an application of the catalyst in treating silane-containing waste gas is provided.

[0026] The main advantages of the present invention are as follows:

[0027] Using one or more different combinations of Fe 2+ , Co 2+ , Ni 2+ , Cu 2+ , Mn 2+ , Ce 3+ , Nb 3+ , Eu 3+ , Ho 3+ as the active component and promoter component of the catalyst, and using alkali metals Na + , K + as regulators to adjust the acidic sites of the carrier, effectively reducing the catalyst cost compared with noble metal catalysts; using Fe 2+ , Co 2+ , Ni 2+ , Cu 2+ , Mn 2+ , Mg 2+ , Na+ , K + 、Ce 3+ , Nb 3 + 、Eu 3+ 、Ho 3+ The catalyst is prepared by using one or more different combinations of Fe ions to prepare the catalyst, such as conventional impregnation, coating, stamping, drying, and calcination, which effectively reduces the catalyst processing cycle and increases the catalyst yield. 2 + 、Ni 2+ , Cu 2+ 、Zn 2+ , Mn 2+ 、Ce 3+ , Nb 3+ One or more of the above can be combined to configure the catalyst activation solution to effectively regulate the distribution of active metals on the catalyst surface, and by containing Na + , K + and NH4 + Ionic substances regulate the pH, which effectively improves the catalyst pore structure during the calcination process, increases the catalyst nitrogen content, and effectively improves the catalyst activity.

[0028] Appendix Description

[0029] Figure 1 It is a line graph of the treatment effect data of the catalyst treating industrial silane-containing waste gas corresponding to Table 1.

[0030] Figure 2 It is a line graph of the treatment effect data of the catalyst treating industrial silane-containing waste gas corresponding to Table 2. DETAILED DESCRIPTION

[0031] The present invention is further described below in conjunction with embodiments. The present invention includes but is not limited to the following embodiments.

[0032] Raw materials and sources: The raw materials in the following examples are all AR-grade chemical reagents purchased from reagent manufacturers such as Aladdin and Inokai.

[0033] Test method: The catalyst activity was evaluated using a fixed bed device, and the silane content was collected by solvent absorption and then tested by gas phase mass spectrometry.

[0034] Example 1

[0035] (1) firstly, a manganese nitrate solution is filled into a container, and nickel nitrate hexahydrate and cerium nitrate are added thereto;

[0036] (2) Pure water will be added into the container to prepare a solution with a Mn ion content of 120 g / L, a Ni content of 60 g / L, and a Ce ion content of 30 g / L. Subsequently, ammonia water is added to adjust the pH to 5, and the container is placed on a heating stirrer and heated to 60 °C, with continuous stirring at a stirring speed of 300 r / min for 40 min to complete the preparation of the impregnation solution;

[0037] (3) Weigh a certain amount of NaY molecular sieve powder with a mass ratio of carrier to impregnation solution of 2:1. Slowly add the molecular sieve powder into the salt solution and stir continuously at a speed of 300 r / min for 1 h, while maintaining heating at 60 °C;

[0038] (4) When the suspension is stirred into a slurry, a certain mass of sodium tungstate binder is added to the suspension with a mass ratio of binder to carrier of 1:50. The cordierite regular ceramic is immersed in the slurry suspension for coating. After 30 min of immersion, the carrier is fished out to complete the first layer of coating;

[0039] (5) The catalyst is dried in an air atmosphere at a drying temperature of 500 °C for 1 h.

[0040] (6) Repeat steps (4) and (5) until the coating thickness reaches 2 mm.

[0041] (7) Load potassium nitrate into the container, add manganese nitrate and nickel nitrate to it, and add pure water to prepare a solution with a K ion content of 5 g / L, a Mn ion content of 80 g / L, and a Ni ion content of 40 g / L. Subsequently, sodium carbonate is added to adjust the pH to 5, and the container is placed on a heating stirrer and heated to 60 °C, with continuous stirring at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution;

[0042] (8) Immerse the dried catalyst in the activation solution at a temperature of 60 °C for catalyst activation. After 10 min of activation, the catalyst is fished out, and the catalyst is calcined in an air atmosphere at a calcination temperature of 600 °C with a heating rate of 2 °C / min for 5 h. After natural cooling to room temperature, the catalyst preparation is completed;

[0043] (9) Cut the catalyst into a suitable size and load it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , an airspeed of 7000 h -1 , and a reaction temperature of 350 °C. Calculate the silane removal rate of the catalyst by comparing the silane contents at the inlet and outlet of the reactor;

[0044] Verify the long-term silane removal effect of the catalyst, and the data results are shown in Table 1.

[0045] Example 2

[0046] (1) First, fill the container with ferric chloride solution, and add cobalt chloride and niobium chloride to it.

[0047] (2) Add pure water to the container, and configure a solution with 300 g / L of Fe ions, 10 g / L of Co, and 100 g / L of Nb ions. Then add sodium hydroxide to adjust the pH to 9, place the container in an ultrasonic disperser, heat it to 60 °C, and continuously ultrasonically disperse for 40 min to complete the preparation of the impregnation solution.

[0048] (3) Weigh a certain amount of alumina powder, with a mass ratio of the carrier to the impregnation solution of 2:1. Slowly add the alumina powder to the salt solution and continuously stir at a speed of 300 r / min for 10 min, while maintaining heating at 80 °C.

[0049] (4) When the suspension is stirred into a slurry, add a certain mass of potassium chloride binder to the suspension, with a mass ratio of the binder to the carrier of 1:50. Immerse the diatomite regular ceramic in the slurry suspension for coating. After 30 min of immersion, remove the carrier to complete the first layer of coating.

[0050] (5) Dry the catalyst in an air atmosphere at a drying temperature of 100 °C for 10 h.

[0051] (6) Repeat steps (4) and (5) until the coating thickness reaches 0.1 mm.

[0052] (7) Fill the container with sodium chloride, add ferric chloride and cobalt chloride to it, and then add pure water to configure a solution with 10 g / L of Na ions, 1 g / L of Fe ions, and 200 g / L of Co ions. Then add potassium hydroxide to adjust the pH to 9, place the container in a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution.

[0053] (8) Immerse the dried catalyst in the activation solution at a temperature of 40 °C for catalyst activation. After 60 min of activation, remove the catalyst, and then calcine the catalyst in an N2 atmosphere at a calcination temperature of 800 °C, with a heating rate of 20 °C / min, for 1 h of continuous calcination. After natural cooling to room temperature, the catalyst preparation is completed.

[0054] (9) Cut the catalyst into a suitable size and fill it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , a space velocity of 7000 h -1 , and a reaction temperature of 350 °C. Calculate the silane removal rate of the catalyst by comparing the silane content at the inlet and outlet of the reactor.

[0055] Verify the long-term silane removal effect of the catalyst, and the data results are shown in Table 1.

[0056] Example 3

[0057] (1) First, fill the container with ferric sulfate solution, and add copper sulfate and holmium nitrate to it.

[0058] (2) Add pure water to the container to prepare a solution with 10 g / L of Fe ions, 10 g / L of Cu ions, and 1 g / L of Ho ions. Then add hydrochloric acid to adjust the pH to 2, and place the container in a mechanical shaker and disperse for 40 min to complete the preparation of the impregnation solution.

[0059] (3) Weigh a certain amount of pseudoboehmite powder. The mass ratio of the carrier to the impregnation solution is 2:1. Slowly add the pseudoboehmite powder to the salt solution and stir continuously, maintaining a stirring speed of 300 r / min for 120 min, and keep heating at 40 °C during this period.

[0060] (4) When the suspension is stirred into a slurry, add a certain mass of potassium nitrate binder to the suspension. The mass ratio of the binder to the carrier is 1:50. Immerse the cordierite regular ceramic in the slurry suspension for coating. After 30 min of immersion, take out the carrier to complete the first layer of coating.

[0061] (5) Dry the catalyst in an air atmosphere at a drying temperature of 200 °C for 3 h.

[0062] (6) Repeat steps (4) and (5) until the coating thickness reaches 5 mm.

[0063] (7) Fill the container with potassium sulfate, add ferric sulfate and copper sulfate to it, and then add pure water to prepare a solution with 0.1 g / L of K ions, 200 g / L of Fe ions, and 100 g / L of Cu ions. Then add sulfuric acid to adjust the pH to 2, place the container in a heating stirrer and heat up to 60 °C, and keep stirring at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution.

[0064] (8) Immerse the dried catalyst in the activation solution, keep the temperature at 20 °C for catalyst activation. After 120 min of activation, take out the catalyst, and calcine the catalyst in an NH3 atmosphere at a calcination temperature of 300 °C, with a heating rate of 1 °C / min, and continue calcining for 10 h. After natural cooling to room temperature, the catalyst preparation is completed.

[0065] (9) Cut the catalyst into a suitable size and fill it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , and the space velocity is 7000 h -1, the reaction temperature is 350 °C, and the silane removal rate of the catalyst is calculated by comparing the silane contents at the inlet and outlet of the reactor;

[0066] The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 1.

[0067] Example 4

[0068] (1) First, fill the container with a manganese nitrate solution, and add copper nitrate and europium nitrate to it;

[0069] (2) Add pure water to the container to prepare a solution with a Mn ion content of 150 g / L, a Cu content of 75 g / L, and a Eu ion content of 1 g / L. Then add sodium bicarbonate to adjust the pH to 6, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the impregnation solution;

[0070] (3) Weigh a certain amount of titanium oxide powder, with a mass ratio of the carrier to the impregnation solution of 2:1. Slowly add the titanium oxide powder to the salt solution and continuously stir at a speed of 300 r / min for 1 h, while maintaining heating at 60 °C;

[0071] (4) When the suspension is stirred into a slurry, add a certain mass of tungsten oxide binder to the suspension, with a mass ratio of the binder to the carrier of 1:50. Dry the catalyst in an air atmosphere at a drying temperature of 200 °C for 3 h.

[0072] (5) Place the dried catalyst powder in a stamping machine mold for stamping, with a stamping pressure of 20 MPa.

[0073] (6) Fill the container with potassium nitrate, add manganese nitrate and copper nitrate to it, and add pure water to prepare a solution with a K ion content of 0.1 g / L, a Mn ion content of 60 g / L, and a Cu ion content of 30 g / L. Then add sodium bicarbonate to adjust the pH to 6, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution;

[0074] (7) Immerse the dried catalyst in the activation solution at a temperature of 60 °C for catalyst activation. After 30 min of activation, take out the catalyst and calcine the catalyst in an Ar atmosphere at a calcination temperature of 500 °C, with a heating rate of 5 °C / min, and continuously calcine for 2 h. After natural cooling to room temperature, the catalyst preparation is completed;

[0075] (8) Cut the catalyst into a suitable size and fill it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , and an airspeed of 7000 h -1, the reaction temperature is 350 °C, and the silane removal rate of the catalyst is calculated by comparing the silane contents at the inlet and outlet of the reactor;

[0076] The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 1.

[0077] Example 5

[0078] (1) First, fill the container with a manganese nitrate solution, and add nickel nitrate and cerium nitrate to it;

[0079] (2) Add pure water to the container to prepare a solution with a Mn ion content of 120 g / L, a Ni content of 60 g / L, and a Ce ion content of 30 g / L. Then add nitric acid to adjust the pH to 2, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the impregnation solution;

[0080] (3) Weigh a certain amount of cerium oxide powder, with a mass ratio of the carrier to the impregnation solution of 2:1. Slowly add the cerium oxide powder to the salt solution and continuously stir at a speed of 300 r / min for 2 h, while maintaining heating at 120 °C;

[0081] (4) When the suspension is stirred into a slurry, add a certain mass of sodium tungstate binder to the suspension, with a mass ratio of the binder to the carrier of 1:50. Dry the catalyst in an air atmosphere at a drying temperature of 200 °C for 3 h.

[0082] (5) Place the dried catalyst powder in a stamping machine mold for stamping, with a stamping pressure of 1 MPa.

[0083] (6) Fill the container with potassium nitrate, add manganese nitrate and copper nitrate to it, and add pure water to prepare a solution with a K ion content of 5 g / L, a Mn ion content of 80 g / L, and a Ni ion content of 40 g / L. Then add nitric acid to adjust the pH to 2, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution;

[0084] (7) Immerse the dried catalyst in the activation solution at a temperature of 50 °C for catalyst activation. After 20 min of activation, take out the catalyst and calcine the catalyst in a He atmosphere at a calcination temperature of 450 °C, with a heating rate of 10 °C / min, for 3 h of continuous calcination. After natural cooling to room temperature, the catalyst preparation is completed;

[0085] (8) Cut the catalyst into a suitable size and fill it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , and an airspeed of 7000 h -1, the reaction temperature is 350 °C, and the silane removal rate of the catalyst is calculated by comparing the silane content at the inlet and outlet of the reactor;

[0086] The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 1.

[0087] Example 6

[0088] (1) First, fill the container with a manganese nitrate solution, and add nickel nitrate and cerium nitrate to it;

[0089] (2) Add pure water to the container to prepare a solution with a Mn ion content of 120 g / L, a Ni content of 60 g / L, and a Ce ion content of 30 g / L. Then add ammonia water to adjust the pH to 5, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the impregnation solution;

[0090] (3) Weigh a certain amount of molecular sieve powder, with a mass ratio of carrier to impregnation solution of 2:1. Slowly add the molecular sieve powder to the salt solution and continuously stir, maintaining a stirring speed of 300 r / min for 1 h, while maintaining heating at 60 °C;

[0091] (4) When the suspension is stirred into a slurry, add a certain mass of sodium tungstate binder to the suspension, with a mass ratio of binder to carrier of 1:50. Dry the catalyst in an air atmosphere at a drying temperature of 200 °C for 3 h.

[0092] (5) Place the dried catalyst powder in a stamping machine mold for stamping, with a stamping pressure of 500 MPa.

[0093] (6) Fill the container with potassium nitrate, add manganese nitrate and copper nitrate to it, and add pure water to prepare a solution with a K ion content of 5 g / L, a Mn ion content of 80 g / L, and a Ni ion content of 40 g / L. Then add ammonia water to adjust the pH to 5, place the container on a heating stirrer, heat it to 60 °C, and continuously stir at a stirring speed of 300 r / min for 40 min to complete the preparation of the activation solution;

[0094] (7) Immerse the dried catalyst in the activation solution, maintain the temperature at 50 °C for catalyst activation. After 20 min of activation, take out the catalyst, and calcine the catalyst in an air atmosphere at a calcination temperature of 450 °C, with a heating rate of 10 °C / min, for 3 h. After natural cooling to room temperature, the catalyst preparation is completed;

[0095] (8) Cut the catalyst into a suitable size and fill it into the reactor. Configure the inlet gas with a dimethylsiloxane content of 200 mg / m 3 , and an airspeed of 7000 h -1, the reaction temperature is 350 °C, and the silane removal rate of the catalyst is calculated by comparing the silane contents at the inlet and outlet of the reactor;

[0096] The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 1.

[0097] Comparative Example 1

[0098] Except for omitting the addition of cerium nitrate in the impregnating solution in Example 1, other operations and parameters are the same as those in Example 1. The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 2.

[0099] Comparative Example 2

[0100] Except for omitting the addition of potassium nitrate in the activating solution in Example 1, other operations and parameters are the same as those in Example 1. The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 2.

[0101] Comparative Example 3

[0102] Except that in steps (2) and (7) of Example 1, the pH was adjusted to 10, other operations and parameters are the same as those in Example 1. The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 2.

[0103] Comparative Example 4

[0104] Except that in steps (1) and (7) of Example 1, manganese nitrate was replaced by magnesium nitrate and nickel nitrate was replaced by zinc nitrate, other operations and parameters are the same as those in Example 1. The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 2.

[0105] Comparative Example 5

[0106] Except that the dosages of manganese nitrate and nickel nitrate used in Example 1 were both increased to 3 times, other operations and parameters are the same as those in Example 1. The long-term silane removal effect of the catalyst was verified, and the data results are shown in Table 2.

[0107] Table 1 Treatment effects of the catalysts in Examples 1-6 for treating industrial waste gas containing silane

[0108]

[0109] Table 2 Treatment effects of the catalysts in Comparative Examples 1-5 for treating industrial waste gas containing silane

[0110]

Claims

1. A method for preparing a catalyst, the method comprising the following steps: (1) dissolving a catalyst active component, a catalyst promoter component and a catalyst site regulator in a dispersant to obtain an impregnation solution; (2) fully mixing the impregnation solution obtained in step (1) with the carrier powder and the binder to form a slurry; (3) uniformly coating the obtained slurry on the surface of the honeycomb-shaped regular ceramic, or uniformly filling the slurry into a mold for stamping; (4) drying the honeycomb-shaped regular catalyst precursor obtained in step (3) to remove free water, crystal water and volatile substances inside the catalyst; (5) The catalyst obtained in step (4) needs to be activated by immersion in a catalyst activation solution; (6) The honeycomb-shaped structured catalyst obtained in step (5) is subjected to calcination treatment.

2. The method according to claim 1, characterized in that, In the step (1), the catalyst active component is selected from Fe 2+ , Co 2 + , Ni 2+ , Cu 2+ , Mn 2+ of nitrate, sulfate or chloride, one or two of them; and / or, the catalyst promoter component is selected from Ce 3 + , Nb 3+ , Eu 3+ , Ho 3+ of nitrate, sulfate or chloride, one or two of them; and / or, the ion concentration of the catalyst active component is 10 - 300 g / L, and the ion concentration of the catalyst promoter component is 1 - 100 g / L.

3. The method according to claim 1 or 2, characterized in that, The pH of the impregnation solution is controlled at 2-9, and the temperature of the impregnation solution is 40-80° C. Preferably, the pH is adjusted by using one or a combination of two or more of ammonia water, sodium hydroxide, potassium hydroxide, sodium carbonate, sodium bicarbonate, hydrochloric acid, sulfuric acid, and nitric acid.

4. The method according to any one of claims 1 to 3, characterized in that In the step (2), the immersion time is 10 to 120 minutes, the carrier powder is selected from one of titanium oxide, aluminum oxide, cerium oxide, pseudo-boehmite, and molecular sieve; and / or the binder is selected from one of sodium tungstate, tungsten oxide, potassium chloride, and potassium nitrate.

5. The method according to any one of claims 1-4, characterized in that In the step (3), the honeycomb-type structured ceramic is selected from structured ceramics made of cordierite and diatomite; the coating thickness is 0.1 to 5 mm; and / or the stamping pressure of the stamping is 1 to 500 MPa.

6. The method according to any one of claims 1-5, characterized in that, The drying temperature in step (4) is 1 to 20°C / min; the drying temperature is 100 to 500°C; and the drying time is 1 to 10 hours.

7. The method according to any one of claims 1-6, characterized in that In the step (5), the main components of the activation solution contain Fe 2+ , Ni 2+ , Cu 2+ , Zn 2+ , Mn 2+ , Ce 3+ , Nb 3+ in one or more than two kinds of solutions, and an ion regulator solution containing one or more than two kinds of Na + , K + , respectively derived from corresponding metal nitrates, sulfates or chlorides and other substances; The concentration of the metal ions of the main components of the activation solution is 1-200 g / L, the concentration of the catalyst regulator ions is 0.1-10 g / L, and the pH of the activation solution is controlled at 2-7.

8. The method according to any one of claims 1-7, characterized in that, In the step (5), the activation temperature is 20-60° C. and the activation time is 10-120 min; and / or, the calcination temperature in the step (6) is 300-800° C. and the calcination time is 1-10 h.

9. The catalyst prepared by the method according to any one of claims 1 to 8.

10. Use of the catalyst prepared by the method according to any one of claims 1 to 8 in treating silane-containing waste gas.

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