A carbon monoxide oxidation catalyst and its preparation method

Abstract

The present invention relates to the technical field of catalysts, and particularly relates to a carbon monoxide oxidation catalyst and a preparation method thereof. The catalyst is prepared by this method. The method includes dissolving the required amounts of platinum salt and promoter salt in water to obtain a mixed solution; dropwise adding the mixed solution to the required amount of tungsten-titanium powder while stirring until a paste is obtained; adding a binder to the paste, and after stirring and mixing evenly, extruding to obtain a monolithic honeycomb mud embryo; successively performing a first drying treatment and a first calcination treatment on the monolithic honeycomb mud embryo to obtain a monolithic honeycomb carrier; soaking the monolithic honeycomb carrier in a tetrabutyl titanate alcohol solution; and successively performing a second drying treatment and a second calcination treatment on the soaked monolithic honeycomb carrier to obtain a carbon monoxide oxidation catalyst. The present invention can prepare a carbon monoxide oxidation catalyst with high catalytic activity, strong anti-poisoning ability and good stability.

Description

Technical Field

[0001] The present invention relates to the technical field of catalysts, and particularly to a carbon monoxide oxidation catalyst and a preparation method thereof. Background Art

[0002] Sintering flue gas generated in the iron and steel sintering process contains a large amount of pollutants, such as SO2, NO x and CO, etc. At present, the desulfurization process can reduce the SO2 concentration to below 35 mg / m³; the SCR technology is used to selectively reduce NO x to nitrogen and water. Among them, the denitrification temperature used is 180 - 280 °C. To reach this denitrification temperature, enterprises often burn coal gas to heat the flue gas, consuming a large amount of cost. It is calculated that for a steel sintering flue gas flow rate of 1 million m³ / h, about 10,000 m³ / h of mixed coal gas is required. And CO in the steel sintering flue gas is generally untreated and directly discharged, which not only wastes the heat energy of CO but also causes environmental pollution.

[0003] At present, the general treatment methods for CO in the industry include adsorption methods, condensation methods, and catalytic oxidation methods, etc. Considering the large flow rate of steel sintering flue gas, if adsorption methods and condensation methods are used to treat CO in steel sintering flue gas, not only a large amount of investment is required, but also the heat energy of CO cannot be effectively utilized. The catalytic oxidation method has attracted much attention because of its small investment, high efficiency, and the ability to release the combustion heat of CO. However, the catalyst used in the catalytic oxidation method is the key factor restricting the treatment or resource utilization of CO in current steel sintering flue gas. Due to the complex composition of steel sintering flue gas and the harsh sintering working conditions, the requirements for the catalyst are extremely high. Existing carbon monoxide oxidation catalysts often have problems such as insufficient catalytic activity, easy poisoning, and poor stability.

[0004] In summary, it is necessary to develop a carbon monoxide oxidation catalyst and a preparation method thereof to solve the problems of insufficient catalytic activity, easy poisoning, and poor stability existing in existing carbon monoxide oxidation catalysts. Summary of the Invention

[0005] The object of the present invention is to provide a carbon monoxide oxidation catalyst and a preparation method thereof, and the specific technical solutions are as follows:

[0006] In the first aspect, the present invention provides a preparation method of a carbon monoxide oxidation catalyst, which includes:

[0007] Step S1: Add 0.01 - 0.04 parts by mass of platinum salt and 0.04 - 0.12 parts by mass of promoter salt into 13 - 15 parts by mass of water and dissolve to obtain a mixed solution; wherein, the promoter salt includes iron salt, cobalt salt and cerium salt; the molar ratio of iron in the iron salt, cobalt in the cobalt salt and cerium in the cerium salt is Fe:Co:Ce = 0.5 - 1:2 - 5:1 - 3;

[0008] Step S2: Dropwise add the mixed solution into 17 - 23 parts by mass of tungsten titanium powder while stirring until a mud-like substance is obtained; wherein, the raw materials of the tungsten titanium powder include titanium dioxide and tungsten trioxide;

[0009] Step S3: Add a binder to the mud-like substance, and after stirring and mixing evenly, extrude to obtain a monolithic honeycomb mud blank;

[0010] Step S4: Subject the monolithic honeycomb mud blank to a first drying treatment and a first calcination treatment in sequence to obtain a monolithic honeycomb carrier;

[0011] Step S5: Immerse the monolithic honeycomb carrier in tetrabutyl titanate alcohol solution; during the immersion treatment, dropwise add water, and control the molar amount of the added water to be 3.5 - 4.5 times the molar amount of tetrabutyl titanate;

[0012] Step S6: Subject the immersed monolithic honeycomb carrier to a second drying treatment and a second calcination treatment in sequence to obtain a monolithic honeycomb catalyst, i.e., a carbon monoxide oxidation catalyst.

[0013] Optionally, the immersion temperature for the immersion treatment is 25 - 50 °C, and the immersion time is 10 - 30 min.

[0014] Optionally, the tetrabutyl titanate alcohol solution includes tetrabutyl titanate and an alcohol solvent; the mass ratio of tetrabutyl titanate to the alcohol solvent is 1:8 - 12.

[0015] Optionally, the drying temperature for the first drying treatment is 100 - 150 °C, and the drying time is 4 - 8 h;

[0016] The calcination temperature for the first calcination treatment is 450 - 550 °C, and the calcination time is 4 - 6 h.

[0017] Optionally, the drying temperature for the second drying treatment is 100 - 150 °C, and the drying time is 4 - 8 h;

[0018] The calcination temperature for the second calcination treatment is 450 - 550 °C, and the calcination time is 4 - 6 h.

[0019] Optionally, the platinum salt includes platinum nitrate; the iron salt includes iron nitrate; the cobalt salt includes cobalt nitrate; the cerium salt includes cerium nitrate.

[0020] Optionally, the mass fraction of the binder used is 0.01 to 0.02 parts; the binder includes carboxymethyl cellulose.

[0021] Optionally, when extruding to obtain the monolithic honeycomb green body, the extrusion pressure used is 3.5 to 4.5 MPa, and the extrusion speed used is 0.3 to 0.5 m / min.

[0022] Optionally, the saturated water absorption rate of the tungsten-titanium powder is 65% to 75%; the tungsten-titanium powder includes raw materials composed of the following mass percentages: 90% to 95% of titanium dioxide and 5% to 10% of tungsten trioxide.

[0023] In a second aspect, the present invention provides a carbon monoxide oxidation catalyst, which is prepared by using the preparation method of the carbon monoxide oxidation catalyst described above.

[0024] Applying the technical solution of the present invention has at least the following beneficial effects:

[0025] The preparation method of a carbon monoxide oxidation catalyst provided by the present invention can prepare a carbon monoxide oxidation catalyst with high catalytic activity, strong anti-poisoning ability and good stability. Specifically:

[0026] In terms of improving catalytic activity, the present invention introduces platinum salts, iron salts, cobalt salts and cerium salts with specific compositions in step S1; among them, CO is adsorbed on the active sites of the co-catalytic components Fe, Co and Ce, and the adsorbed CO can be catalytically oxidized to CO2. At the same time, Fe, Co and Ce are reduced, such as Fe 3+ is reduced to Fe 2+ , Co 3+ is reduced to Co 2+ ; further, the reduced co-catalytic components are oxidized by oxygen in the air, such as Fe 2+ is oxidized to Fe 3+ , Co 2+ is oxidized to Co 3+ , which indicates that the co-catalytic components can undergo redox cycles during the catalytic oxidation of CO to CO2; among them, Ce can promote electron migration, promote the redox cycle of Fe / Co, and thus promote the catalytic oxidation of CO; in addition, CO can also be adsorbed on the active sites of the main catalytic component Pt, and the adsorbed CO can react with the adsorbed oxygen to generate CO2. Therefore, the present invention uses the co-catalytic components Fe, Co and Ce and the main catalytic component Pt to synergistically catalyze the oxidation of CO, greatly improving the catalytic activity.

[0027] In terms of improving the anti-poisoning performance, in the present invention, the mud obtained in step S2 is processed through step S3 and step S4 to obtain a monolithic honeycomb carrier. By means of the immersion treatment of the tetrabutyl titanate alcohol solution in step S5 and the gradual dropwise addition of water, and controlling the molar amount of the added water to be 4.2 times the molar amount of tetrabutyl titanate, it is convenient for tetrabutyl titanate to hydrolyze to form Ti(OH)4 precipitate, which adheres to the surface of the catalyst. After the second calcination treatment in step S6, the Ti(OH)4 precipitate can form a TiO2 film on the surface of the catalyst. This TiO2 film is dense and can block large toxin molecules such as SO2, phosphates, and arsenates, allowing small molecules such as CO to pass through. Therefore, this TiO2 film can not only protect the active sites of the catalyst from being invaded by toxins but also enable CO to pass through the TiO2 film and undergo a catalytic reaction at the active sites. In addition, the TiO2 film can also react with some toxic and harmful substances, acting as a sacrificial agent. Therefore, the TiO2 film can protect the catalyst and improve the anti-poisoning performance of the catalyst.

[0028] In terms of improving the stability of the catalyst, in the present invention, tungsten-titanium powder is selected as the catalyst carrier, and by means of step S2, a mixed solution with a specific composition is gradually dropwise added to a specific mass fraction of tungsten-titanium powder, enabling the active components of the co-catalytic component and the main catalytic component to be uniformly loaded on the surface and inside the pores of the tungsten-titanium powder, preventing the loss and aggregation of the active components, and greatly improving the stability of the catalyst. In addition, the steel sintering flue gas contains components such as sulfur, chlorine, and water. The conventional alumina carrier has poor acid resistance and is prone to react with sulfur, chlorine, and water, subsequently resulting in the structural collapse and pore damage of the alumina carrier. However, the raw materials of the tungsten-titanium powder described in the present invention include titanium dioxide and tungsten trioxide, both of which have stronger acid resistance than alumina and have a large specific surface area, facilitating the uniform loading of the active components. Further, in the present invention, the mixed solution with a specific composition is gradually dropwise added to a specific mass fraction of tungsten-titanium powder. On the one hand, it is considered that the pores of the tungsten-titanium powder carrier have a capillary action. By gradually dropwise adding the mixed solution to the tungsten-titanium powder, not only is the contact area between the mixed solution and the tungsten-titanium powder carrier relatively small, the external diffusion resistance of the active components from the main body of the mixed solution to the surface of the carrier is small, and it is easier to enter the pores, but also the mixed solution has more time to enter the pores by means of capillary action. As a result, each active component can not only be loaded on the surface of the tungsten-titanium powder but also deeply loaded inside the pores of the tungsten-titanium powder. On the other hand, by gradually dropwise adding the mixed solution to the tungsten-titanium powder, it is convenient for each active component to be uniformly loaded on the surface and inside the pores of the tungsten-titanium powder. If the mixed solution is added to the tungsten-titanium powder at one time, due to the large liquid volume and large inlet pressure, the capillary action will be damaged, affecting the penetration of the mixed solution in the pores of the tungsten-titanium powder. In addition, if the mixed solution is added to the tungsten-titanium powder at one time, there will be a situation where the local concentration of the mixed solution is too high, resulting in uneven penetration. Moreover, if the mixed solution is added to the tungsten-titanium powder at one time, it will increase the external diffusion resistance of the mixed solution, causing some active components to possibly aggregate on the surface of the carrier and making it difficult to enter the deep pores.

[0029] In addition to the purposes, features and advantages described above, the present invention has other purposes, features and advantages. The present invention will be further described in detail below with reference to the drawings. Description of the Drawings

[0030] The drawings forming a part of this application are used to provide a further understanding of the present invention. The schematic embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation to the present invention. In the drawings:

[0031] Figure 1 is a test result graph of the catalyst prepared in Example 1 for catalytic oxidation of carbon monoxide;

[0032] Figure 2 is a test result graph of the catalyst prepared in Comparative Example 1 for catalytic oxidation of carbon monoxide;

[0033] Figure 3 is a test result graph of the catalyst prepared in Comparative Example 8 for catalytic oxidation of carbon monoxide;

[0034] Figure 4 is a test result graph of the catalyst prepared in Comparative Example 9 for catalytic oxidation of carbon monoxide;

[0035] Figure 5 is a SEM test result graph of the catalyst prepared in Example 1;

[0036] Figure 6 is a SEM test result graph of the catalyst prepared in Comparative Example 1. Detailed Description of the Embodiments

[0037] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention. Obviously, the described embodiments are only a part of the embodiments of the present invention, rather than all the embodiments. All other embodiments obtained by those of ordinary skill in the art based on the embodiments of the present invention belong to the scope of protection of the present invention.

[0038] Example 1:

[0039] A preparation method of a carbon monoxide oxidation catalyst, comprising:

[0040] Step S1: Dissolve 0.02 parts by mass of a platinum salt and 0.08 parts by mass of an auxiliary salt in 14 parts by mass of water to obtain a mixed solution; wherein, the auxiliary salt includes an iron salt, a cobalt salt and a cerium salt; the molar ratio of iron in the iron salt, cobalt in the cobalt salt and cerium in the cerium salt is Fe:Co:Ce = 0.5 - 1:2 - 5:1 - 3; specifically, the molar ratio Fe:Co:Ce = 0.8:4:2;

[0041] Step S2: Dropwise add the mixed solution into 20 parts by mass of tungsten-titanium powder while stirring until a mud-like substance is obtained. Among them, the raw materials of the tungsten-titanium powder include titanium dioxide and tungsten trioxide.

[0042] Step S3: Add a binder to the mud-like substance, and after stirring and mixing evenly, extrude it through an extruder to obtain a monolithic honeycomb mud blank.

[0043] Step S4: Perform a first drying treatment and a first calcination treatment on the monolithic honeycomb mud blank in sequence to obtain a monolithic honeycomb carrier.

[0044] Step S5: Immerse the monolithic honeycomb carrier in tetrabutyl titanate alcohol solution. During the immersion treatment, water is dropwise added, and the molar amount of the added water is controlled to be 4.2 times the molar amount of tetrabutyl titanate.

[0045] Step S6: Perform a second drying treatment and a second calcination treatment on the immersed monolithic honeycomb carrier in sequence to obtain a monolithic honeycomb catalyst, that is, a carbon monoxide oxidation catalyst.

[0046] The soaking temperature for the soaking treatment is 50 °C, and the soaking time is 30 min.

[0047] The tetrabutyl titanate alcohol solution includes tetrabutyl titanate and an alcohol solvent (specifically ethanol, used to dissolve tetrabutyl titanate); the mass ratio of tetrabutyl titanate to the alcohol solvent is 1:10.

[0048] The drying temperature for the first drying treatment is 100 °C, and the drying time is 6 h.

[0049] The calcination temperature for the first calcination treatment is 500 °C, and the calcination time is 4 h.

[0050] The drying temperature for the second drying treatment is 120 °C, and the drying time is 6 h.

[0051] The calcination temperature for the second calcination treatment is 500 °C, and the calcination time is 4 h.

[0052] The platinum salt is platinum nitrate; the iron salt is iron nitrate; the cobalt salt is cobalt nitrate; the cerium salt is cerium nitrate.

[0053] The mass fraction of the binder is 0.015 parts; the binder is carboxymethyl cellulose.

[0054] When extruding to obtain the monolithic honeycomb mud blank, the extrusion pressure is 3.5 MPa, and the extrusion speed is 0.5 m / min.

[0055] The saturated water absorption rate of the tungsten-titanium powder is 65% - 75% (70% can be specifically selected); the tungsten-titanium powder comprises raw materials with the following mass percentages: 95% of titanium dioxide and 5% of tungsten trioxide.

[0056] Example 2:

[0057] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 0.5:2:1.

[0058] Example 3:

[0059] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 0.5:2:3.

[0060] Example 4:

[0061] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 0.5:5:1.

[0062] Example 5:

[0063] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 0.5:5:3.

[0064] Example 6:

[0065] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 1:2:1.

[0066] Example 7:

[0067] Different from Example 1, the molar ratio of Fe:Co:Ce is controlled to be 1:2:3.

[0068] Comparative Example 1:

[0069] Different from Example 1, step S5 is cancelled.

[0070] Comparative Example 2:

[0071] Different from Example 1, the dosage of the iron salt is zero.

[0072] Comparative Example 3:

[0073] Different from Example 1, the dosage of the cobalt salt is zero.

[0074] Comparative Example 4:

[0075] Different from Example 1, the dosage of the cerium salt is zero.

[0076] Comparative Example 5:

[0077] Different from Example 4, the molar ratio of Fe:Co:Ce was controlled at 0.5:6:1, that is, the dosage of cobalt salt was too high.

[0078] Comparative Example 6:

[0079] Different from Example 3, the molar ratio of Fe:Co:Ce was controlled at 0.5:2:4, that is, the dosage of cerium salt was too high.

[0080] Comparative Example 7:

[0081] Different from Example 6, the molar ratio of Fe:Co:Ce was controlled at 1.5:2:1, that is, the dosage of iron salt was too high.

[0082] Comparative Example 8:

[0083] Different from Example 1, the dosage of platinum salt was zero.

[0084] Comparative Example 9:

[0085] Different from Example 1, the dosages of iron salt, cobalt salt and cerium salt were all zero.

[0086] Samples of the catalysts prepared in Examples 1-7 and Comparative Examples 1-9 were respectively taken for side-line tests on the catalytic oxidation of carbon monoxide in steel sintering flue gas. The test results are shown in Table 1 and Figures 1 to 4 . The test method is as follows:

[0087] The test gas was steel sintering flue gas after desulfurization and denitrification, and its composition was as follows: moisture with a volume fraction of 10% - 15%, low-carbon hydrocarbons of 100 - 300 ppm, CO of 5000 - 6000 ppm, trace amounts of Hg, As, P, etc., trace amounts of heavy metals and alkali metals, sulfur dioxide of 25 mg / m³, and HCl of 10 mg / m³. The flow rate of the test gas was 100 m³ / h. The temperature of the test gas was 280°C. The test instrument was Testo 340 handheld CO concentration analyzer. The catalyst was laid in layers on the catalytic bed, with a length of 150 mm, a width of 150 mm, and a thickness of 300 mm.

[0088] Table 1 Test results of the catalysts in Examples 1-7 and Comparative Examples 2-7

[0089]

[0090] As can be seen from Table 1, compared with Comparative Examples 2-7, the catalysts prepared in Examples 1-7 of the present invention all had a relatively high average conversion rate for CO, showing good catalytic activity. By Figures 1 to 4It is known that, compared with Comparative Examples 1 and 8-9, the catalysts prepared by Examples 1-7 of the present invention can all have a relatively high average conversion rate of CO and a relatively long stable operation time, showing good catalytic activity, anti-poisoning performance and stability.

[0091] Specifically, compared with Example 1, Step S5 was cancelled in Comparative Example 1, that is, a TiO2 film could not be formed on the catalyst surface, and the toxins in the steel sintering flue gas would directly attack the active sites, quickly causing the catalyst to be poisoned and inactivated.

[0092] Compared with Example 1, the co-catalytic components Fe, Co and Ce were respectively missing in Comparative Examples 2-4. Although the stability of the catalyst could also reach more than 200 h, the average conversion rate of CO decreased. This is because Fe has an Fe 2+ / Fe 3+ redox pair, Co has a Co 2+ / Co 3+ redox pair, and the redox pairs of Fe and Co can both promote the catalytic oxidation of CO to CO2; and Ce can promote electron migration and the redox cycle of Fe / Co, thereby promoting the catalytic oxidation of CO. Therefore, the co-catalytic components Fe, Co and Ce cannot synergistically enhance the catalytic activity of the catalyst without each other, that is, the average conversion rate of CO decreases.

[0093] Compared with Example 4, a too high dosage of cobalt salt was used in Comparative Example 5, resulting in too high a cobalt element content; compared with Example 3, a too high dosage of cerium salt was used in Comparative Example 6, resulting in too high a cerium element content; compared with Example 6, a too high dosage of iron salt was used in Comparative Example 7, resulting in too high an iron element content; and in the co-catalytic components of the catalyst, too high a content of one element led to a relatively reduced content of other elements, and a large number of composite oxide structures (such as oxides of Fe, Co and Ce in divalent state and oxides in trivalent state) could not be formed, resulting in Fe, Co and Ce still existing as single oxides and unable to exert excellent synergistic catalytic effects, and the average conversion rate of CO all showed a reduced result.

[0094] Compared with Example 1, in Comparative Example 8, the amount of platinum salt is zero. The catalyst prepared therein is deactivated after running for 120 h, and the average conversion rate of CO is lower than 60%. This shows that the catalyst has low catalytic activity and poor stability. Specifically, Pt, as the main catalytic component, provides the main catalytic activity. Without Pt, the natural catalytic activity decreases. Although trace amounts of Hg, As, P, and sulfur dioxide in the iron and steel sintering flue gas are blocked by the TiO2 film covering the catalyst surface and do not cause poisoning of the active sites, the HCl molecules in the iron and steel sintering flue gas have a smaller molecular diameter, and some HCl molecules may pass through the pores in the TiO2 film and then combine with the cocatalytic components Fe, Co, and Ce to form stable hydrochlorides, which cannot be decomposed, resulting in a decrease in the catalyst activity and even poisoning and deactivation, showing poor stability. In Example 1, with the presence of Pt, the adsorption form formed by Pt and HCl is unstable and is easily dissociated from the catalyst, and the catalyst will not be deactivated.

[0095] Compared with Example 1, in Comparative Example 9, the amounts of iron salt, cobalt salt, and cerium salt are all zero, that is, the cocatalytic components Fe, Co, and Ce are not used, resulting in the average conversion rate of CO of the prepared catalyst being lower than 70% and the stability decreasing. This is because without the cocatalytic components Fe, Co, and Ce, the catalytic activity of the catalyst decreases, showing that the average conversion rate of CO is lower than 70%; the electron cloud density of the cocatalysts (Fe, Co, and Ce) is relatively high, and electrons will be transferred to Pt, thereby weakening the adsorption strength of Pt for HCl, preventing desorption failure due to excessive adsorption, and further affecting the stability. Without the cocatalytic components Fe, Co, and Ce, the HCl molecules adsorbed on the Pt active sites cannot be desorbed from the Pt active sites in time, resulting in the shielding of the Pt active sites after long-term operation, and further leading to a decrease in the catalyst stability.

[0096] Samples of the catalysts prepared in Example 1 and Comparative Example 1 were respectively taken for SEM testing. The test results are shown in Figures 5 to 6 , and it can be seen that a smooth and dense TiO2 film is formed on the surface of the catalyst prepared in Example 1; while no TiO2 film is formed on the surface of the catalyst prepared in Comparative Example 1, and its surface is relatively rough.

[0097] The above are only the preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention can have various modifications and changes. Any modifications, equivalent replacements, improvements, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A preparation method of a carbon monoxide oxidation catalyst, characterized in that, include: Step S1, adding 0.01-0.04 parts by mass of a platinum salt and 0.04-0.12 parts by mass of an auxiliary salt to 13-15 parts by mass of water to dissolve to obtain a mixed solution; wherein the auxiliary salt comprises an iron salt, a cobalt salt, and a cerium salt; the molar ratio of iron in the iron salt, cobalt in the cobalt salt, and cerium in the cerium salt is Fe:Co:Ce=0.5-1:2-5:1-3; Step S2, adding the mixed solution dropwise to 17 to 23 parts by mass of tungsten-titanium powder, stirring while adding, until a sludge is obtained; wherein the raw materials used for the tungsten-titanium powder include titanium dioxide and tungsten trioxide; Step S3, adding a binder to the mud, and after stirring and mixing, extruding to obtain an integral honeycomb mud embryo; Step S4, subjecting the integral honeycomb clay embryo to a first drying process and a first calcining process in sequence to obtain an integral honeycomb carrier; Step S5, placing the monolithic honeycomb substrate in a tetrabutyl titanate alcohol solution for immersion treatment; adding water dropwise during the immersion treatment, and controlling the molar amount of the added water to be 3.5 to 4.5 times the molar amount of the tetrabutyl titanate; Step S6: performing a second drying treatment and a second calcination treatment on the monolithic honeycomb substrate after the soaking treatment in sequence to obtain a monolithic honeycomb catalyst, ie, a carbon monoxide oxidation catalyst.

2. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, characterized in that, The soaking treatment adopts a soaking temperature of 25-50° C. and a soaking time of 10-30 minutes.

3. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, characterized in that, The tetrabutyl titanate alcohol solution includes tetrabutyl titanate and an alcohol solvent; the mass ratio of the tetrabutyl titanate to the alcohol solvent is 1:8-12.

4. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, wherein, The drying temperature used in the first drying treatment is 100-150° C., and the drying time used is 4-8 hours; The first calcination treatment uses a calcination temperature of 450-550° C. and a calcination time of 4-6 hours.

5. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, characterized in that, The second drying process uses a drying temperature of 100-150°C and a drying time of 4-8 hours; The second calcination treatment uses a calcination temperature of 450-550° C. and a calcination time of 4-6 hours.

6. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, characterized in that, The platinum salt includes platinum nitrate; the iron salt includes iron nitrate; the cobalt salt includes cobalt nitrate; and the cerium salt includes cerium nitrate.

7. The method for preparing a carbon monoxide oxidation catalyst according to claim 1, wherein, The binder is used in an amount of 0.01 to 0.02 parts by mass; the binder comprises carboxymethyl cellulose.

8. The preparation method of the carbon monoxide oxidation catalyst according to claim 1, characterized in that, When the integral honeycomb mud embryo is extruded, the extrusion pressure used is 3.5~4.5MPa, and the extrusion speed used is 0.3~0.5m / min.

9. The preparation method of the carbon monoxide oxidation catalyst according to any one of claims 1 to 8, characterized in that, The saturated water absorption rate of the tungsten-titanium powder is 65% to 75%; the tungsten-titanium powder comprises the following raw materials in percentage by mass: 90% to 95% titanium dioxide and 5% to 10% tungsten trioxide.

10. A carbon monoxide oxidation catalyst, characterized in that, The carbon monoxide oxidation catalyst is prepared by the preparation method of the carbon monoxide oxidation catalyst as claimed in claim 9.

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