CN109772309B - Catalyst for catalytic combustion of ketobenzene-containing tail gas and preparation method thereof - Google Patents
Catalyst for catalytic combustion of ketobenzene-containing tail gas and preparation method thereof Download PDFInfo
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Abstract
The invention discloses a monolithic catalyst for catalytic oxidation of ketobenzene-containing tail gas and a preparation method thereof, wherein the active component of the catalyst is Pd or Pt or Pd-Pt with a certain proportion, and the carrier coating is (1-a) Al2O3‑aMxOyA composite oxide. The active component of the catalyst is loaded by an isovolumetric impregnation/excess impregnation method, and the transition metal composite oxide is prepared by coprecipitation, sol-gel, mechanical ball milling and other methods. The catalyst has higher combustion activity and stability of the ketobenzene tail gas, and can also be used in the catalytic removal process of other VOCs gases containing phenol, ketone and the like.
Description
Technical Field
The invention relates to a catalyst for catalytic combustion of a ketobenzene-containing tail gas and a preparation method thereof, in particular to a catalyst for catalytic combustion of a ketobenzene-containing tail gas and a preparation method thereof.
Background
At present, the VOCs treatment technology at home and abroad is mainly based on catalytic combustion and adsorption, and particularly the catalytic combustion has the advantages of low requirement on the concentration of VOCs, no secondary pollution and the like, thereby being the most effective VOCs purification technology. However, the combustion catalysts used in our country are imported, and the main suppliers are Johnson Matthey, BASF in Germany, Sud-Chemie in Germany (purchased by Clariant), Topsoe in Denmark, etc. From the viewpoint of active components, there are mainly two types of noble metal catalysts and composite oxide catalysts, wherein the active components of the noble metal catalysts are mainly Pd, Pt, Rh, and the like. CN101204654A discloses a noble metal catalyst for low-temperature catalytic oxidation of benzene series; CN101367045A relates to a copper-manganese composite oxide catalyst for catalyzing and burning ethylene, a preparation method and application thereof; CN101733127B discloses a catalyst for treating organic waste gas and a preparation method thereof. However, this is not soThe disclosed catalysts are all particle catalysts, the discharge pressure of industrial VOCs is low, and the particle catalysts increase the system power consumption and reduce the technical economy due to high bed resistance drop. Therefore, the monolithic honeycomb catalyst has obvious technical advantages in the field of VOCs catalytic removal. CN200910188158.5 discloses a preparation method of a catalytic combustion catalyst, wherein, alumina sol is coated on the surface of cordierite honeycomb ceramic, then rare earth metal is impregnated, noble metal is impregnated, and the preparation process is complicated; patent CN1504260A relates to an integral combustion catalyst and its preparation method, the active components of the catalyst are transition metal oxides such as iron, manganese, nickel, cobalt, etc. CN104107700A relates to a combustion catalyst for industrial organic waste gas and a preparation method thereof, and active components are CuO, MnO and Fe2O3、CeO2And a composite oxide of AgO. The transition metal oxide is used as an active component, the activation temperature of the catalyst is high, and the operation cost is increased. Therefore, the noble metal monolithic honeycomb combustion catalyst is still the mainstream technology of industrial application, and the activity and stability of the catalyst are improved by reducing the noble metal content of the catalyst as much as possible through the addition of the auxiliary agent.
Disclosure of Invention
In the production process of the lubricating oil, in order to remove normal paraffin and isoparaffin (namely wax) in raw materials, the freezing point is reduced, the low-temperature flow property of oil products is improved, and the use requirement under low temperature is met. Dewaxing is carried out with a butanone-toluene mixed solvent. The process tail gas contains butanone-toluene and other organic gases, and is used to meet the exhaust standard of atmospheric pollutants. Aiming at the defects of the prior art, the invention provides the ketobenzene tail gas combustion catalyst and the preparation method thereof, and the catalyst has the advantages of long service life, high removal rate and the like in the catalytic combustion process of treating the waste gas, so that the long-term stable operation of a catalytic combustion tail gas purification device is ensured.
A combustion catalyst for catalytic combustion of the tail gas containing ketobenzene uses honeycomb ceramics as carrier, whose surface is sequentially coated with alumina and metallic oxide MxOyComposite oxide slurry, active component Pd or Pt orPd-Pt in a certain proportion; the alumina is derived from AlOOH and Al (OH) in a certain proportion3、 Al2O3With Al (NO)3)3And (4) ball milling to obtain the product.
A combustion catalyst for the catalytic combustion of the tail gas containing ketobenzene contains Pd or Pt as active component and Al as carrier coating (1-a)2O3-aMxOyA composite oxide;
wherein: m is Si, Mg, Ba and other main cluster elements; or Ti, Mn, Cu, Co, Ni, Fe, Zr and other transition metal elements; or La, Ce and other rare earth elements; al (Al)2O3AlOOH, Al (OH) from a certain ratio3、Al2O3And Al (NO)3)3(ii) a a is 0.01-0.99, x is 1-3; y is 1 to 4.
The honeycomb ceramic carrier of the present invention is usually cordierite, and (1-a) Al is used as the carrier2O3-aMxOyThe composite metal oxide accounts for 10-40%, preferably 20-30%. Al in composite metal oxide2O3Is between 1% and 99%, preferably between 20% and 80%.
The content of active component Pd or Pt or a certain proportion of Pd-Pt accounts for 0.01% -1%, preferably 0.05% -0.5% of the total weight of the catalyst; wherein M is main cluster elements such as Si, Mg, Ba and the like, or transition metal elements such as Ti, Mn, Cu, Co, Ni, Fe, Zr and the like, or rare earth elements such as La, Ce and the like.
A process for preparing the ketobenzene-contained catalyst used for catalytic combustion of tail gas includes (1-a) Al2O3-aMxOyThe preparation process of the composite oxide slurry, the cordierite honeycomb carrier metal oxide coating process and the active component precious metal impregnation process comprises the following specific steps:
1) will be mixed with Al2O3Calculated by the weight ratio of AlOOH (0-90 percent), Al (OH)3(0-90％)、 γ-Al2O3(0-80％)、Al(NO3)3(0-90%) two or more compositions and MxOyPrecursor salts of metal oxides or M (as M)xOyAccounting for 10-60 percent of the mass ratio of the composite oxide) to prepare the composite oxide;
2) adding water or dilute nitric acid into the prepared composite oxide, and ball-milling for 0.5-6h to prepare composite oxide slurry A;
3) adding dilute nitric acid or water into the composite oxide slurry A to adjust the pH value to be 1-6 and the viscosity to be 10-300 mPa.s;
4) immersing the cordierite honeycomb carrier in the composite oxide slurry A for 1-5min, taking out, blowing off redundant slurry in gaps by using compressed air, drying at 50-200 ℃ overnight, and roasting to obtain B;
5) preparing a noble metal solution with the concentration of 1mg/ml to 60mg/ml, soaking the prepared B coated with the composite oxide in the prepared solution for 0.5 to 10min, blowing redundant feed liquid by using compressed air, and drying, baking and firing to obtain a catalyst C;
6) catalyst C produced in 10vol.% H2-90vol.％N2Reducing for 2 hours at 450 ℃ in the atmosphere to obtain the reduced catalyst S with the integral structure.
(1-a) Al in the method of the present invention2O3-aMxOyThe preparation process of the composite oxide slurry comprises the following steps ofxOyThe preparation process comprises the steps of preparing the compound by a homogeneous phase method, a precipitation method and a rapid decomposition method; the slurry preparation process is to prepare MxOyAnd AlOOH, Al (OH)3、Al(NO3)3、γ-Al2O3One or more of them are mixed, or M isxOySoluble salts of (A) with AlOOH, Al (OH)3、Al(NO3)3、γ-Al2O3Mixing one or more of the above raw materials, adding a certain amount of water or dilute nitric acid, and ball milling for 0.5-6h to obtain composite oxide slurry A.
The cordierite honeycomb carrier metal oxide coating process in the method is that dilute nitric acid or water is added into the composite oxide slurry A to adjust the pH value to be 1-6 and the viscosity to be 10-300 mPa.s; then, immersing the cordierite honeycomb carrier in the composite oxide slurry A for 1-5min, taking out, blowing off redundant slurry in pores by using compressed air, and then drying at 50-200 ℃ overnight or microwave drying for 2-10 min; the cordierite honeycomb coated with the composite metal oxide coating is roasted for 2 to 4 hours at the temperature of 300-700 ℃, and the process is repeated for one or more times until the loading of the metal oxide reaches 10 to 40 percent based on the weight of the carrier to prepare B;
the active component noble metal dipping process in the method is to prepare a noble metal aqueous solution or alcohol solution with a certain concentration of 1mg/ml to 60mg/ml, put the prepared B coated with the composite oxide into the solution, keep the solution for 0.5 to 10min, then purge redundant feed liquid by compressed air, and then dry the solution at 50 to 200 ℃ overnight or dry the solution by microwave for 2 to 10 min; then, the catalyst C is prepared by roasting at 400-500 ℃ for 2-4 hours.
Compared with the prior art, the invention has the following advantages:
1. the invention relates to a catalyst for catalytic combustion of ketobenzene-containing tail gas in gamma-Al2O3Other metal oxides are added, and gamma-Al is taken into consideration2O3The catalyst has excellent catalytic combustion performance and the catalytic catalysis performance of the transition metal oxide and the rare earth metal oxide, and improves the activity and the stability of the catalyst;
2. the invention adopts AlOOH and Al (OH) in a certain proportion3、Al(NO3)3、γ-Al2O3The slurry coating and the honeycomb ceramic carrier have good combination effect when the slurry is prepared by ball milling, and the defects of weak adhesion force, easy shedding, low coating amount and the like of the slurry coating in the prior art are avoided, so that the catalytic combustion catalyst has long service life and high activity stability;
3. AlOOH and Al (OH) in a certain proportion used in the invention3、Al(NO3)3、γ-Al2O3The slurry prepared by ball milling has high binding force, the binding strength between the carrier and the coating can be further improved, the abrasion resistance of the catalyst is greatly improved, and the catalyst can still have long service life when running at higher airspeed;
4. the invention uses AlOOH and Al (OH) in a certain proportion3、Al(NO3)3、γ-Al2O3The catalyst coated by the slurry prepared by ball milling has higher BET surface area, is beneficial to high dispersion of the active component of the noble metal, and improves the activity of the catalyst;
5. the catalytic combustion catalyst has strong adaptability to treatment of VOCs waste gas, can efficiently treat various complex VOCs waste gas, and has simple preparation method and equipment, and easy operation and industrial production.
Drawings
FIG. 1 is a continuous 1000 hour stability test for catalyst S-2.
Detailed Description
The following detailed description of the present invention is merely a preferred embodiment of the present invention, and is not intended to limit the scope of the invention. All the equivalent changes and modifications made according to the claims of the present invention should fall within the scope covered by the present invention.
Example 1
Weighing CeO prepared by homogeneous phase method21g of pseudo-foil 10g, 6.5g of aluminum nitrate nonahydrate, gamma-Al2O31.3g, aluminum hydroxide Al (OH)36.5g of water and 30g of water are added into a ball milling tank for ball milling for 4 hours to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2The reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain the reduced monolithic catalyst S-1(0.1 wt% Pd/20 wt.% (0.94 Al)2O3-0.06CeO2) Cordierite honeycomb).
Example 2
Weighing cerium ammonium nitrate 8.0g, pseudo-thin 10g, aluminum nitrate 6.5g, gamma-Al2O31.3g, aluminum hydroxide Al (OH)36.5g of water and 30g of water are added into a ball milling tank for ball milling for 2 hours to prepareObtaining slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a platinum nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-2(0.2 wt% Pt/30 wt.% (0.86 Al)2O3-0.14CeO2) Cordierite honeycomb). Catalyst S-2 was tested for stability for 1000 consecutive hours as shown in FIG. 1.
Example 3
Weighing 2.5g of manganese nitrate, 5g of pseudo-thin film, 4g of aluminum nitrate and gamma-Al2O38.2g, aluminum hydroxide Al (OH)33g of dilute nitric acid and 30g of dilute nitric acid are added into a ball milling tank for ball milling for 4 hours to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst was prepared at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-3(0.1 wt% Pd/23 wt.% (0.94 Al)2O3-0.06MnO2) Cordierite honeycomb).
Example 4
Weighing 2.35g of copper nitrate, 4g of pseudo-thin copper nitrate and 6g of aluminum nitrate, and gamma-Al2O33.2g, aluminum hydroxide Al (OH)37.62g of water and 30g of water are added into a ball milling tank to be ball milled for 2 hours, so as to prepare slurry A; 1ml of 400 mesh honeycomb ceramic carrier was immersed in the slurry for 5min and taken out, and excess slurry in the pores was blown out with compressed air and then micrometricDrying by waves, and roasting for 2 hours at 600 ℃ to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate and palladium nitrate mixed solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, roasting for 4 hours at 550 ℃, thereby preparing the catalyst C with the integral structure. The catalyst produced was at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-4(0.15 wt% Pd-0.05 wt% Pt/27 wt.% (0.93 Al)2O3-0.07 CuO)/cordierite honeycomb).
Example 5
Weighing 3.6g of cobalt nitrate, 1g of pseudo-thin cobalt nitrate, 25g of aluminum nitrate and gamma-Al2O33.7g, aluminum hydroxide Al (OH)310g of water and a ball milling tank are added for ball milling for 4 hours to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was in 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-5(0.19 wt% Pd/29 wt.% (0.94 Al)2O3-0.06Co3O4) Cordierite honeycomb).
Example 6
Weighing 8.9g of nickel nitrate, gamma-Al2O34.6g, aluminum hydroxide Al (OH)315g of water and 30g of water are added into a ball milling tank to be ball milled for 4 hours, so as to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting for 2 hours at 600 ℃ to obtain a carrier B coated with a mixed oxide coating; the carrier B coated with the mixed oxide coating was dipped in a palladium nitrate solution and excess in the pores of the honeycomb carrier was blown off with compressed airA solution; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-6 (0.05 wt% Pd/30 wt.% (0.87 Al)2O3-0.13 NiO)/cordierite honeycomb).
Example 7
0.76g of iron nitrate, 10g of a pseudo-thin film, 6g of aluminum nitrate, aluminum hydroxide Al (OH)38.2g of water and 30g of water are added into a ball milling tank to be ball milled for 4 hours, so as to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a platinum nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain reduced monolithic catalyst S-7(0.10 wt% Pt/18 wt.% (0.75 Al)2O3-0.25Fe2O3) Cordierite honeycomb).
Example 8
3.48g of zirconium nitrate, 11g of a pseudo-thin film, aluminum hydroxide Al (OH)38.2g of water and 30g of water are added into a ball milling tank to be ball milled for 4 hours, so as to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting for 2 hours at 600 ℃ to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-8(0.11 wt% Pd/21 wt.% (0.93 Al)2O3-0.07ZrO2) Cordierite honeycomb).
Example 9
Weighing 1g of titanium oxide, 8g of aluminum nitrate and Al (OH) aluminum hydroxide320g of water and 20g of ball milling tank are added into the ball milling tank for ball milling for 4 hours to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90 vol.％N2Reduction was carried out at 450 ℃ for 2 hours under an atmosphere to obtain a reduced monolithic catalyst S-9 (0.13 wt% Pd/25 wt.% (0.71 Al)2O3-0.29TiO2) Cordierite honeycomb).
Comparative example 1
Weighing gamma-Al2O310g of alumina sol, 12g of alumina sol and 23g of water are added into a ball milling tank and ball milled for 4 hours to prepare slurry A; soaking 1ml of 400-mesh honeycomb ceramic carrier in the slurry for 5min, taking out, blowing out excessive slurry in pores by using compressed air, then drying by microwave, and roasting at 600 ℃ for 2 hours to obtain a carrier B coated with a mixed oxide coating; dipping the carrier B coated with the mixed oxide coating into a palladium nitrate solution, and blowing the redundant solution in the pores of the honeycomb carrier by using compressed air; after microwave drying for 5 minutes, the catalyst C with the monolithic structure is prepared by roasting at 550 ℃ for 4 hours. The catalyst produced was at 10vol.% H2-90vol.％N2Reducing the mixture for 2 hours at 45 ℃ under the atmosphere to obtain a reduced monolithic catalyst B-1(0.2 wt% Pd/30 wt.% gamma-Al)2O3Cordierite honeycomb).
For the above catalyst at GHSV of 20,000h-1The activity of the catalyst is evaluated under the atmosphere of 2000ppm butanone and 320ppm toluene; at GHSV of 20,000h-1Butanone 2000ppm, toluene 320ppm, catalyst activity in air equilibrium atmosphereThe performance of the catalyst was evaluated as follows:
Claims (9)
1. a combustion catalyst for catalytic combustion of ketobenzene-containing tail gas is characterized in that: the active component of the catalyst is Pd or Pt or Pd-Pt, and the carrier coating is (1-a) Al2O3-aMxOyThe carrier of the composite oxide is cordierite honeycomb ceramic;
wherein: m is one of Ti, Mn, Cu, Co, Ni and Fe; al (Al)2O3AlOOH, Al (OH) from a certain mixture ratio3、γ-Al2O3And Al (NO)3)3(ii) a a is 0.01-0.99, x is 1-3; y is 1 to 4;
the preparation method of the combustion catalyst for the catalytic combustion of the ketobenzene-containing tail gas is characterized by comprising the following specific steps of:
1) mixing AlOOH, Al (OH)3、γ-Al2O3、Al(NO3)3Two or more kinds of compositions and MxOyThe precursor salt of the metal oxide or M is blended to prepare a composite oxide; with Al2O3Calculated by the weight ratio of the composite oxide, 0 to 90 percent of AlOOH and Al (OH)3 0-90%、γ-Al2O30-80%、Al(NO3)3 0 to 90 percent; with MxOyMeter, MxOyThe precursor salt of the metal oxide or M accounts for 10-60% of the composite oxide by mass;
2) adding water or dilute nitric acid into the prepared composite oxide, and ball-milling for 0.5-6h to prepare composite oxide slurry A;
3) adding dilute nitric acid or water into the composite oxide slurry A to adjust the pH value to 1-6 and the viscosity to 10-300 mPa.s;
4) immersing the cordierite honeycomb carrier in the composite oxide slurry A for 1-5min, taking out, blowing off redundant slurry in gaps by using compressed air, drying at 50-200 ℃ overnight, and roasting to obtain B;
5) preparing 1-60 mg/mL active component solution, soaking the prepared B coated with the composite oxide in the prepared solution for 0.5-10min, blowing redundant feed liquid by using compressed air, and then drying and roasting to prepare a catalyst C;
6) catalyst C produced in 10vol.% H2-90 vol.%N2Reducing for 2 hours at 450 ℃ in the atmosphere to obtain the reduced catalyst S with the integral structure.
2. The combustion catalyst as claimed in claim 1, wherein the content of the active components Pd, Pt and Pd-Pt is 0.01-1% by weight, and the coating layer (1-a) is made of Al2O3-aMxOyThe composite oxide accounts for 10-40% of the total weight of the carrier.
3. The combustion catalyst for catalytic combustion of ketobenzene-containing tail gas as claimed in claim 1, wherein the content of the active components Pd, Pt and Pd-Pt of the catalyst is 0.05-0.5% by weight of the total weight of the catalyst; the coating (1-a) is Al2O3-aMxOyThe composite oxide accounts for 20-30% of the total weight of the carrier.
4. The combustion catalyst for catalytic combustion of ketobenzene-containing exhaust gas as claimed in claim 1, wherein said coating is (1-a) Al2O3-aMxOyA is 0.01 to 0.8.
5. The combustion catalyst as claimed in claim 1, wherein M is an aromatic hydrocarbonxOyThe oxide is prepared by a homogeneous phase method, a precipitation method and a rapid decomposition method.
6. The combustion catalyst as claimed in claim 1, wherein the gamma-Al is selected from the group consisting of2O3Is prepared from AlOOH, Al (OH)3、Al(NO3)3、γ-Al2O3One or more of the above-mentioned materials can be made up by using precipitation or roasting process.
7. The combustion catalyst as claimed in claim 1, wherein the calcination temperature in step 4) is 300-700 ℃ and the calcination time is 2-4 hours to obtain B.
8. The combustion catalyst as claimed in claim 1, wherein the calcination temperature in step 5) is 400-500 ℃ and the calcination time is 2-4 hours to obtain the catalyst C.
9. The combustion catalyst as claimed in claim 1, wherein the active component solution in step 5) is an aqueous solution or an alcoholic solution thereof.
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