Catalytic purification catalyst for CO in industrial flue gas and preparation method of catalytic purification catalyst

Abstract

The invention provides a CO catalytic purification catalyst for industrial flue gas and a preparation method thereof. The catalyst comprises the following components in percentage by mass: 90%-95% of a dispersion carrier and 5%-10% of an active component, the dispersion carrier is a TiO2-ZnO bimetallic oxide system, the content of a TiO2 component is 60%-90%, and the content of a ZnO component is 10%-40%; the active component is Pt-V2O5-WO3, and the active component is Pt-V2O5-WO3.

Description

Technical Field

[0001] The invention belongs to the technical field of environmental catalysis, and in particular relates to a catalyst for catalytic purification of CO in industrial flue gas and a preparation method thereof. Background Art

[0002] As the greenhouse effect poses an increasingly prominent threat to human survival, green environmental protection will also be an inevitable requirement for future industrial development. The sintering process of the steel industry is the process with the largest proportion of air pollution emissions, among which particulate matter, NOx, and SO2 emissions account for 50% of the entire industry, and unconventional pollutants dioxins account for more than 90%. In addition, incomplete combustion of coal during steel sintering will emit high concentrations of CO (about 1%). Carbon monoxide (CO) is a colorless, odorless, and non-irritating gas, but it has serious harm to human health. Once inhaled, carbon monoxide will bind to hemoglobin to form carbon monoxide hemoglobin, which will prevent oxygen from binding to hemoglobin and reduce the oxygen content in the blood. This may lead to hypoxia, and in severe cases, even coma, brain damage, or even death. In addition, CO will react with pollutants such as NOx, SO2, and VOCs emitted from flue gas to form photochemical smog, which seriously affects the quality of atmospheric air. Therefore, it has become a top priority to find an efficient and reliable catalyst to effectively solve the pollution problem of CO emissions in industrial flue gas.

[0003] In view of this, the present invention is proposed. Summary of the invention

[0004] The purpose of the present invention is to provide a catalyst for catalytic purification of CO in industrial flue gas and a preparation method thereof, which can effectively solve the pollution problem of CO emission from industrial flue gas.

[0005] In order to achieve the above objectives, the present invention particularly adopts the following technical solutions:

[0006] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas. The catalyst comprises a dispersed carrier and an active component by mass ratio, wherein the dispersed carrier has a mass percentage of 90% to 95% and the active substance has a mass percentage of 5% to 10%; the dispersed carrier is a TiO2-ZnO bimetallic oxide system, wherein the TiO2 component content is 60% to 90% and the ZnO component content is 10% to 40%;

[0007] The active component of the active component is Pt-V2O5-WO3.

[0008] Preferably, the TiO2 in the dispersed carrier is anatase TiO2, with a TiO2 content of ≥98%, a heteroelement content of ≤2%, and a specific surface area of ​​250-320 m 2 / g, pore volume ≥0.45cc / g, sulfate impurity content ≤1.0%, chloride impurity content ≤0.5%;

[0009] The ZnO in the dispersed carrier has an effective ZnO content of ≥96%, a content of impurity elements of ≤1%, and a specific surface area of ​​40-60 m 2 / g, pore volume ≥0.3cc / g, sulfate impurity content ≤0.6%, chloride impurity content ≤0.1%.

[0010] Preferably, WO3 in the active component is a co-catalyst component, and Pt-V2O5 is a main catalytic component, wherein:

[0011] Preferably, the Pt precursor salt in the active component is platinum nitrate, the V2O5 precursor salt in the active component is ammonium metavanadate, and the WO3 precursor salt in the active component is ammonium metatungstate.

[0012] The present invention provides a method for preparing the catalyst for catalytic purification of CO in industrial flue gas, comprising the following steps:

[0013] 1) Preparation of catalyst dispersed carrier: Mix TiO2 and ZnO mixed powder with water, acid solution and dispersant mixed solution to form a mixture slurry, grind the mixture slurry, and dry it to obtain a dispersed carrier powder;

[0014] 2) Preparation of catalyst precursor: V2O5 precursor salt, WO3 precursor salt, water and the dispersed carrier powder obtained in step 1) are mixed and dried to obtain catalyst precursor powder;

[0015] 3) Preparation of platinum loading: water, platinum precursor salt and sodium caseinate are mixed, and then sodium hydroxide is added to form a mixed solution, the catalyst precursor powder obtained in step 2) is mixed with the mixed solution, N2-H2S mixed gas is introduced, heated, filtered, washed, dried and calcined to obtain a CO catalytic purification catalyst for industrial flue gas.

[0016] Preferably, in step 1), the raw material ratios for preparing the dispersed carrier are as follows: water: 65%-80%, TiO2: 15%-25%, ZnO: 2%-10%, acid solution: 0.5%-1.3%, dispersant: 2.5%-3.0%, by mass ratio, wherein:

[0017] Preferably, the acid solution includes one or more of H3PO4, citric acid, acetic acid and oxalic acid. The acid solution can enrich the microscopic pores of TiO and ZnO, and form micropores with a diameter of less than 0.5 nm inside the carrier material. The micropores with a diameter of less than 0.5 nm can filter out the macromolecular sulfur-containing substances that poison the catalyst, and more importantly, improve the acid strength of TiO2 and ZnO, and improve the catalyst's ability to resist sulfur poisoning.

[0018] The water is demineralized water, the conductivity is ≤20us / cm, the purity of H3PO4 is 90%-95%, and the dispersant is ammonium polyacrylate type dispersant or ammonium dodecyl sulfonate type dispersant.

[0019] Preferably, in step 1), the viscosity of the mixture slurry is 150-300 mPa.s, the grinding time is 10-15 h, and the grinding environment temperature is 10-30 ° C;

[0020] The drying temperature is 180℃-220℃.

[0021] Preferably, in step 2), the raw material ratio for preparing the catalyst precursor powder is as follows, by mass ratio: V2O5 precursor salt: 0.2%-0.8%, WO3 precursor salt: 0.4%-1.0%, water: 70%-80%, and dispersed carrier powder: 20%-30%.

[0022] Preferably, in step 2), the stirring time is 2h-5h, the drying temperature is 180°C-220°C, and the drying time is 4h-7h.

[0023] Preferably, in step 3), by mass ratio, the catalyst precursor powder is: 25%-30%, the platinum precursor salt is: 0.7%-1.0%, the sodium caseinate is: 0.5%-0.7%, the sodium hydroxide is: 0.3%-0.5%, and the water is: 65%-72%, wherein the role of the sodium caseinate is to complex Pt to prevent its precipitation from causing larger Pt grains and reducing the catalytic ability; the role of the sodium hydroxide is to enhance the complexing effect of caseinic acid on Pt, promote the attachment of Pt to the deep microporous sites of TiO2 and ZnO, avoid Pt only attaching to the outer layer, and improve the anti-poisoning ability.

[0024] Preferably, in step 3), the mixed gas is introduced during the stirring process, and the aeration is stopped after aeration and stirring for 22-26 hours, and the mixture is heated to 40°C-60°C, the drying temperature is 130°C-160°C, the drying is 6h-9h, the roasting temperature is 500°C-560°C, and the roasting time is 2h-4h.

[0025] Preferably, the H2S concentration in the N2-H2S mixed gas is 10ppm-100ppm. The main function of H2S is to increase the dispersion of the active component Pt and improve the catalytic performance.

[0026] Beneficial effects of the present invention:

[0027] (1) The catalyst of the present invention has obvious anti-poisoning performance and can be applied to flue gas with humidity ≥20% and SO2 concentration of 1000-5000mg / Nm 3 When the K2O concentration is ≥15% and the heavy metal Pb content is 1%-5%, there will be no problem of decreased CO conversion rate.

[0028] (2) The catalyst of the present invention has a long service life, and its service life under real industrial complex flue gas conditions is ≥ 24000h. It meets the following conditions: the flue gas temperature changes by 50-150°C / min, the humidity changes by 10-30% / min, the CO concentration changes by 1000-6000ppm / min, the SO2 concentration changes by 300-1800ppm / min, etc., and can be used to stably remove CO under drastic changes.

[0029] (3) The catalytic selectivity of the present invention is good. The CO oxidation catalyst used in industrial flue gas is generally arranged after SCR denitration. Since there is a certain concentration of ammonia escape in the flue gas after SCR denitration, the conventional CO oxidation catalyst has a strong oxidation capacity in the formulation system to achieve the purpose of complete CO oxidation, and a certain concentration of ammonia escape in the flue gas is oxidized to NO, resulting in the emission of pollutant NO, which reduces the effect of SCR denitration. The catalyst of the present invention has obvious ammonia escape oxidation selectivity, controls the oxidation capacity of the system, ensures the efficient conversion of CO, and oxidizes the ammonia escape in the flue gas to N2. The catalyst has very good N2 selectivity. DETAILED DESCRIPTION

[0030] In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution in the embodiments of the present invention will be described clearly and completely below. Obviously, the described embodiments are only part of the embodiments of the present invention, not all of the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention.

[0031] First, the present invention is explained as a whole, as follows:

[0032] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas and a preparation method thereof, comprising the following method:

[0033] Step 1: Preparation of catalyst dispersion carrier

[0034] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the carrier is a TiO2-ZnO bimetallic oxide system, wherein the TiO2 component content is 60%-90%, the ZnO component content is 10%-40%, the TiO2 is anatase TiO2, the TiO2 content is ≥98%, the impurity element content is ≤2%, and the specific surface area is preferably 250-320m 2 / g, the pore volume is preferably ≥0.45cc / g, the sulfate impurity content is ≤1.0%, and the chloride impurity content is ≤0.5%; the effective ZnO content in the ZnO is ≥96%, the impurity element content is ≤1%, and the specific surface area is preferably 40-60m 2 / g, the pore volume is preferably ≥0.3cc / g, the sulfate impurity content is ≤0.6%, and the chloride impurity content is ≤0.1%.

[0035] Preparation of dispersed carrier: Mix TiO2 powder and ZnO powder in a formula ratio, add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio, wherein the deionized water is conventional industrial water with an electrical conductivity of ≤20us / cm, H3PO4 is industrial grade with a purity of 95%, and the dispersant is preferably an ammonium polyacrylate type dispersant or an ammonium dodecylsulfonate type dispersant. The mixed powders of TiO2 and ZnO are mixed and stirred with the mixed solution of deionized water, H3PO4 and a dispersant to form a mixture slurry, and the viscosity of the mixture slurry is 150-300mpa.s. The mixed slurry is wet ground for 10-15hh and a grinding environment temperature of 10-30°C. After grinding, the mixed slurry is released for rotary spray drying at a drying temperature of 180°C-220°C. After drying, the dispersed carrier powder of the present invention for the catalytic purification of CO in industrial flue gas is obtained. Among them, the raw material ratio for the preparation of the dispersed carrier is shown in the following table:

[0036] Material Name Component ratio / % water 65％-80％ <![CDATA[TiO2]]> 15％-25％ ZnO 2％-10％ <![CDATA[H3PO4]]> 0.5％-1.3％ Dispersants 2.5％-3.0％

[0037] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0038] Step 2: Catalyst precursor preparation

[0039] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0040] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0041] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed in a formula ratio for 2h-5h. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 180°C-220°C for 4h-7h. The powder obtained after drying is a catalyst precursor powder.

[0042] The raw material ratio for preparing catalyst precursor powder is shown in the following table:

[0043] Material Name Component ratio / % Ammonium metavanadate 0.2％-0.8％ Ammonium Metatungstate 0.4％-1.0％ water 70％-80％ Carrier powder 20％-30％

[0044] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0045] Step 3: Platinum loading preparation

[0046] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, introduce N2-H2S mixed gas (the H2S concentration in the mixed gas is 10-100ppm, preferably 50-80ppm) into the mixed system during the stirring process, stop aeration after ventilation and stirring for 22-26h, heat the suspended mixed solution to 40-60℃ for full reaction, then filter and precipitate, wash the filtered precipitate with deionized water, and end washing when the pH of the filtered water is ≤7.0. Dry and roast the washed filtered precipitate at a drying temperature of 130℃-160℃, dry for 6h-9h, roast at a maximum temperature of 500℃-560℃, and roast at a maximum temperature of 2h-4h. After roasting, a CO catalytic purification catalyst for industrial flue gas is obtained.

[0047] The raw material ratios for platinum loading preparation are shown in the following table:

[0048] Material Name Component ratio / % Precursor powder 25％-30％ Platinum nitrate 0.7％-1.0％ Sodium Caseinate 0.5％-0.7％ Sodium hydroxide 0.3％-0.5％ water 65％-72％

[0049] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0050] Specifically, in all embodiments of the present invention, the TiO2 used is anatase TiO2, with a TiO2 content of 98.6%, a content of impurities of 1.3%, and a specific surface area of ​​preferably 287 m 2 / g, the pore volume is preferably 0.45cc / g, the sulfate impurity content is 0.32%, and the chloride impurity content is 0.27%; the effective ZnO content of the ZnO used is 96.2%, the impurity element content is 0.63%, and the specific surface area is preferably 45.9m 2 / g, pore volume is 0.3cc / g, sulfate impurity content is 0.32%, chloride impurity content is 0.06%. The conductivity of the desalted water used is 12.7us / cm. The H3PO4 used is industrial grade with a purity of 95%, and the dispersant is polyacrylate ammonium type dispersant.

[0051] Example 1

[0052] Step 1: Preparation of catalyst dispersion carrier

[0053] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0054] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0055] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0056] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0057] Step 2: Catalyst precursor preparation

[0058] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0059] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0060] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0061] The raw material ratios for preparing catalyst precursor powder are shown in the following table:

[0062] Material Name Mass / Kg Component ratio Ammonium metavanadate 2.4 0.60 Ammonium Metatungstate 3.1 0.77 water 300 73.97 Carrier powder 100 24.66

[0063] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0064] Step 3: Platinum loading preparation

[0065] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 40°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, the CO catalytic purification catalyst for industrial flue gas of the present invention is obtained.

[0066] The raw material ratios for platinum loading preparation are shown in the following table:

[0067]

[0068] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0069] Example 2

[0070] Step 1: Preparation of catalyst dispersion carrier

[0071] Mix TiO2 powder and ZnO powder in a formula ratio, and add desalted water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix the TiO2 and ZnO mixed powders with the desalted water, H3PO4 and a dispersant mixed solution and stir to form a mixture slurry, the viscosity of which is 172mpa.s. Wet grind the mixed slurry for 15 hours at a grinding environment temperature of 15°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 220°C. After drying, obtain the dispersed carrier of the catalyst for catalytic purification of CO in industrial flue gas.

[0072] Ratio of raw materials for preparing dispersed carrier:

[0073] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 70 18.62 ZnO 25 6.6 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0074] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0075] Step 2: Catalyst precursor preparation

[0076] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0077] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0078] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 180° C. for 7 hours. The powder obtained after drying is a catalyst precursor powder.

[0079] Raw material ratio for preparing catalyst precursor powder:

[0080] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 2.4 0.60 Ammonium Metatungstate 3.1 0.77 water 300 73.97 Carrier powder 100 24.66

[0081] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0082] Step 3: Platinum loading preparation

[0083] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 50°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, the CO catalytic purification catalyst for industrial flue gas of the present invention is obtained.

[0084] The raw material ratios for platinum loading preparation are shown in the following table:

[0085] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.05 Platinum nitrate 3 0.84 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.13

[0086] The above is the mass ratio, the comprehensive ratio of each component is 100%

[0087] Example 3

[0088] Step 1: Preparation of catalyst dispersion carrier

[0089] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. The TiO2 and ZnO mixed powders are mixed with the deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry, and the slurry viscosity is 172mpa.s. The mixed slurry is wet-ground for 13 hours at a grinding environment temperature of 20°C. After the grinding is completed, the mixed slurry is released for rotary spray drying at a drying temperature of 200°C. The powder obtained after drying is used as a dispersed carrier of a CO catalytic purification catalyst in industrial flue gas.

[0090] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0091]

[0092]

[0093] The above is the mass ratio, the comprehensive ratio of each component is 100%

[0094] Step 2: Catalyst precursor preparation

[0095] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0096] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0097] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed in a formula ratio for 3 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 220° C. for 4 hours. The powder obtained after drying is a catalyst precursor powder.

[0098] The raw material ratios for preparing catalyst precursor powder are shown in the following table:

[0099] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 2.4 0.60 Ammonium Metatungstate 3.1 0.77 water 300 73.97 Carrier powder 100 24.66

[0100] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0101] Step 3: Platinum loading preparation

[0102] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 45°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7 hours, the maximum roasting temperature is 500°C, and the maximum high temperature roasting time is 4 hours. After roasting, the CO catalytic purification catalyst for industrial flue gas of the present invention is obtained.

[0103] The raw material ratios for platinum loading preparation are shown in the following table:

[0104] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.05 Platinum nitrate 3 0.84 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.13

[0105] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0106] Example 4

[0107] Step 1: Preparation of catalyst dispersion carrier

[0108] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0109] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0110]

[0111]

[0112] The above is the mass ratio, the comprehensive ratio of each component is 100%

[0113] Step 2: Catalyst precursor preparation

[0114] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0115] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0116] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0117] The raw material ratios for preparing catalyst precursor powder are shown in the following table:

[0118] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 3 0.74 Ammonium Metatungstate 2 0.49 water 300 74.08 Carrier powder 100 24.69

[0119] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0120] Step 3: Platinum loading preparation

[0121] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir to form a mixed solution b, mix the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after 24 hours of ventilation and stirring, heat the suspended mixed solution to 55°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 160°C, the drying time is 9 hours, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2 hours. After roasting, a CO catalytic purification catalyst for industrial flue gas in the technical solution is obtained.

[0122] The raw material ratios for platinum loading preparation are shown in the following table:

[0123] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.05 Platinum nitrate 3 0.84 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.13

[0124] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0125] Example 5

[0126] Step 1: Preparation of catalyst dispersion carrier

[0127] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0128] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0129] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0130] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0131] Step 2: Catalyst precursor preparation

[0132] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0133] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0134] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0135] The raw material ratio for preparing catalyst precursor powder is shown in the following table:

[0136] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 1 0.25 Ammonium Metatungstate 4 0.98 water 300 74.08 Carrier powder 100 24.69

[0137] The above is the mass ratio, the comprehensive ratio of each component is 100%

[0138] Step 3: Platinum loading preparation

[0139] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir to form a mixed solution b, mix the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after 24 hours of ventilation and stirring, heat the suspended mixed solution to 60°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted at a drying temperature of 150°C for 7 hours, a maximum roasting temperature of 540°C, and a maximum high temperature roasting time of 2 hours. After roasting, a CO catalytic purification catalyst for industrial flue gas in the technical solution is obtained.

[0140] The raw material ratios for platinum loading preparation are shown in the following table:

[0141] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.05 Platinum nitrate 3 0.84 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.13

[0142] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0143] Example 6

[0144] Step 1: Preparation of catalyst dispersion carrier

[0145] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix the TiO2 and ZnO mixed powders with the deionized water, H3PO4 and a dispersant mixed solution and stir to form a mixture slurry, the viscosity of which is 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. The powder obtained after drying is the dispersed carrier of the catalyst for catalytic purification of CO in industrial flue gas described in the present invention.

[0146] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0147] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0148] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0149] Step 2: Catalyst precursor preparation

[0150] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0151] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0152] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0153] The raw material ratio for preparing catalyst precursor powder is shown in the following table:

[0154]

[0155]

[0156] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0157] Step 3: Platinum loading preparation

[0158] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 55°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, the CO catalytic purification catalyst for industrial flue gas of the present invention is obtained.

[0159] The raw material ratios for platinum loading preparation are shown in the following table:

[0160] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.05 Platinum nitrate 2.5 0.70 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.27

[0161] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0162] Example 7

[0163] Step 1: Preparation of catalyst dispersion carrier

[0164] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0165] Ratio of raw materials for preparing dispersed carrier:

[0166] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0167] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0168] Step 2: Catalyst precursor preparation

[0169] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0170] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0171] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0172] The raw material ratios for preparing catalyst precursor powder are shown in the following table:

[0173]

[0174]

[0175] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0176] Step 3: Platinum loading preparation

[0177] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 50ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 40°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, the CO catalytic purification catalyst for industrial flue gas of the present invention is obtained.

[0178] The raw material ratios for platinum loading preparation are shown in the following table:

[0179] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.01 Platinum nitrate 3.5 0.98 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.03

[0180] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0181] Example 8

[0182] Step 1: Preparation of catalyst dispersion carrier

[0183] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0184] Ratio of raw materials for preparing dispersed carrier:

[0185] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0186] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0187] Step 2: Catalyst precursor preparation

[0188] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0189] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0190] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0191] The raw material ratio for preparing catalyst precursor powder is shown in the following table:

[0192] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 3 0.74 Ammonium Metatungstate 2 0.49 water 300 74.08 Carrier powder 100 24.69

[0193] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0194] Step 3: Platinum loading preparation

[0195] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 80ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 55°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, a CO catalytic purification catalyst for industrial flue gas is obtained.

[0196] The raw material ratios for platinum loading preparation are shown in the following table:

[0197] Material Name Mass / Kg Component ratio / % Precursor powder 100 28.01 Platinum nitrate 3.5 0.98 Sodium Caseinate 2 0.56 Sodium hydroxide 1.5 0.42 water 250 70.03

[0198] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0199] Example 9

[0200] Step 1: Preparation of catalyst dispersion carrier

[0201] Mix TiO2 powder and ZnO powder in a formula ratio, and add deionized water, H3PO4 and a dispersant mixed solution in a formula ratio. Mix TiO2 and ZnO mixed powders with deionized water, H3PO4 and a dispersant mixed solution to form a mixture slurry with a viscosity of 172mpa.s. Wet grind the mixed slurry for 12 hours at a grinding environment temperature of 25°C. After grinding, release the mixed slurry for rotary spray drying at a drying temperature of 200°C. After drying, a dispersed carrier for a CO catalytic purification catalyst in industrial flue gas is obtained.

[0202] The raw material ratios for preparing the dispersed carrier are shown in the following table:

[0203] Material Name Mass / Kg Component ratio / % water 270 71.6 <![CDATA[TiO2]]> 60 15.9 ZnO 35 9.32 <![CDATA[H3PO4]]> 2 0.53 Dispersants 10 2.65

[0204] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0205] Step 2: Catalyst precursor preparation

[0206] The present invention provides a catalyst for catalytic purification of CO in industrial flue gas, wherein the active component of the catalyst is Pt-V2O5-WO3, wherein WO3 is a co-catalytic component and Pt-V2O5 is a main catalytic component. The precursor salt of the active component Pt is platinum nitrate, the precursor salt of the active component V2O5 is ammonium metavanadate, and the precursor salt of the co-catalytic component WO3 is ammonium metatungstate.

[0207] The present invention provides a method for loading active components of a catalyst for catalytic purification of CO in industrial flue gas:

[0208] Ammonium metavanadate, ammonium metatungstate, deionized water and the dispersed carrier obtained in step 1 are stirred and mixed for 2 hours. The mixed slurry obtained by stirring is spray-dried at a drying temperature of 200° C. for 5 hours. The powder obtained after drying is a catalyst precursor powder.

[0209] The raw material ratios for preparing catalyst precursor powder are shown in the following table:

[0210] Material Name Mass / Kg Component ratio / % Ammonium metavanadate 3 0.74 Ammonium Metatungstate 2 0.49 water 300 74.08 Carrier powder 100 24.69

[0211] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0212] Step 3: Platinum loading preparation

[0213] Weigh water, platinum nitrate (10% solution) and sodium caseinate in a formula ratio and stir and mix to form a mixed solution a, add sodium hydroxide in a formula ratio to the mixed solution a and stir and mix to form a mixed solution b, mix and stir the catalyst precursor powder obtained in step 2 with the mixed solution b, and introduce N2-H2S mixed gas into the mixed system during stirring, wherein the H2S concentration in the mixed gas is 80ppm, and stop aeration after aeration and stirring for 24 hours, heat the suspended mixed solution to 55°C for full reaction, and then filter and precipitate, and wash the filtered precipitate with deionized water, and when the pH of the filtered water is 7.0, the washing is terminated. The washed filtered precipitate is dried and roasted, the drying temperature is 150°C, the drying is 7h, the maximum roasting temperature is 540°C, and the maximum high temperature roasting time is 2h. After roasting, a CO catalytic purification catalyst for industrial flue gas is obtained.

[0214] The raw material ratios for platinum loading preparation are shown in the following table:

[0215]

[0216]

[0217] The above is the mass ratio, and the comprehensive ratio of each component is 100%.

[0218] The performance of the catalyst prepared in the above examples was verified, mainly for the three indicators of CO conversion rate, N2 selectivity and anti-poisoning ability of the prepared catalyst. The anti-poisoning ability index was based on the catalyst under complex flue gas conditions (humidity 25%, SO2 concentration 3000mg / Nm 3 , K2O concentration 15%, PbO concentration 1.5%) after running for 1680h CO conversion attenuation rate is the measurement index. The performance data of the catalyst prepared in the above embodiment are shown in the following table:

[0219] Example CO conversion rate (200℃) <![CDATA[N2 Selectivity (200 °C)]]> 1680hCO conversion attenuation rate / % Example 1 90.74 99.8 19.3 Example 2 90.42 98.5 20.1 Example 3 90.77 81.9 19.6 Example 4 90.91 99.7 10.1 Example 5 90.76 99.8 50.9 Example 6 82.14 99.9 11.6 Example 7 95.72 99.4 10.9 Example 8 98.73 99.6 10.7 Example 9 99.14 99.5 10.6

[0220] The catalyst of the invention can be used for the efficient and stable removal of CO in industrial flue gas, and is particularly suitable for the removal of CO in the flue gas of sintering machines in the steel industry and the removal of CO in the flue gas emitted by dry coke quenching in the coking industry.

[0221] Please note that the technical features of the above embodiments can be combined arbitrarily. In order to make the description concise, all possible combinations of the technical features in the above embodiments are not described. However, as long as there is no contradiction in the combination of these technical features, they should be considered to be within the scope of this specification. The above embodiments only express several implementation methods of the present application, and their descriptions are relatively specific and detailed, but they cannot be understood as limiting the scope of the invention patent. It should be pointed out that for ordinary technicians in this field, without departing from the concept of the present application, several variations and improvements can be made, which all belong to the scope of protection of the present application. Therefore, the scope of protection of the patent in this application shall be based on the attached claims.

Claims

1. A catalyst for catalytic purification of CO in industrial flue gas, characterized in that: The catalyst comprises a dispersed carrier and an active component by mass ratio, wherein the dispersed carrier mass percentage is 90% to 95% and the active substance mass percentage is 5% to 10%; the dispersed carrier is a TiO2-ZnO bimetallic oxide system, wherein the TiO2 component content is 60% to 90% and the ZnO component content is 10% to 40%; The active component of the active component is Pt-V2O5-WO3.

2. The catalyst according to claim 1, characterized in that The TiO2 in the dispersed carrier is anatase TiO2, the TiO2 content is ≥98%, the impurity element content is ≤2%, and the specific surface area is 250-320m 2 / g, pore volume ≥0.45cc / g, sulfate impurity content ≤1.0%, chloride impurity content ≤0.5%; The ZnO in the dispersed carrier has an effective ZnO content of ≥96%, a content of impurity elements of ≤1%, and a specific surface area of ​​40-60 m 2 / g, pore volume ≥0.3cc / g, sulfate impurity content ≤0.6%, chloride impurity content ≤0.1%.

3. The catalyst according to claim 1, characterized in that WO3 in the active component is a co-catalytic component, and Pt-V2O5 is a main catalytic component, wherein: Preferably, the Pt precursor salt in the active component is platinum nitrate, the V2O5 precursor salt in the active component is ammonium metavanadate, and the WO3 precursor salt in the active component is ammonium metatungstate.

4. A method for preparing a catalyst for catalytic purification of CO in industrial flue gas according to any one of claims 1 to 3, comprising the following steps: 1) Preparation of catalyst dispersed carrier: Mix TiO2 and ZnO mixed powder with water, acid solution and dispersant mixed solution to form a mixture slurry, grind the mixture slurry, and dry it to obtain a dispersed carrier powder; 2) Preparation of catalyst precursor: V2O5 precursor salt, WO3 precursor salt, water and the dispersed carrier powder obtained in step 1) are mixed and dried to obtain catalyst precursor powder; 3) Preparation of platinum loading: water, platinum precursor salt and sodium caseinate are mixed, and then sodium hydroxide is added to form a mixed solution, the catalyst precursor powder obtained in step 2) is mixed with the mixed solution, N2-H2S mixed gas is introduced, heated, filtered, washed, dried and calcined to obtain a CO catalytic purification catalyst for industrial flue gas.

5. The preparation method according to claim 4, characterized in that: In step 1), the raw material ratio of the dispersed carrier is as follows: Water: 65%-80%, TiO2: 15%-25%, ZnO: 2%-10%, acid solution: 0.5%-1.3%, dispersant: 2.5%-3.0%, among which, Preferably, the acid solution includes one or more of H3PO4, citric acid, acetic acid and oxalic acid. The water is demineralized water, the conductivity is ≤20us / cm, the purity of H3PO4 is 90%-95%, and the dispersant is ammonium polyacrylate type dispersant or ammonium dodecyl sulfonate type dispersant.

6. The preparation method according to claim 4, characterized in that: In step 1), the viscosity of the mixture slurry is 150-300 mPa.s, the grinding time is 10-15 h, and the grinding environment temperature is 10-30 ° C; The drying temperature is 180℃-220℃.

7. The preparation method according to claim 4, characterized in that: In step 2), the raw material ratios for preparing the catalyst precursor powder are as follows: V2O5 precursor salt: 0.2%-0.8%, WO3 precursor salt: 0.4%-1.0%, water: 70%-80%, and dispersed carrier powder: 20%-30%, calculated by mass ratio.

8. The preparation method according to claim 4, characterized in that: In step 2), the stirring time is 2h-5h, the drying temperature is 180°C-220°C, and the drying time is 4h-7h.

9. The preparation method according to claim 4, characterized in that: In step 3), by mass ratio, catalyst precursor powder: 25%-30%, platinum precursor salt: 0.7%-1.0%, sodium caseinate: 0.5%-0.7%, sodium hydroxide: 0.3%-0.5%, water: 65%-72%.

10. The preparation method according to claim 4, characterized in that: In step 3), the mixed gas is introduced during the stirring process, and the aeration is stopped after the aeration and stirring for 22-26 hours, and the mixture is heated to 40°C-60°C, the drying temperature is 130°C-160°C, the drying is 6h-9h, the roasting temperature is 500°C-560°C, and the roasting time is 2h-4h. Preferably, the H2S concentration in the N2-H2S mixed gas is 10ppm-100ppm.

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