KR101092358B1 - Low Temperature Catalyst for Combustion of Organic Compound, And Manufacturing Method thereof - Google Patents

Abstract

The present invention relates to a low temperature catalyst for burning an organic compound and a method of manufacturing the same. More specifically, the present invention is a carrier consisting of a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxide; And a noble metal catalyst component supported on the support, and a low temperature catalyst for burning an organic compound having a zirconium (Zr) content in the support of 50 to 100 wt% and a method of manufacturing the same.

Zirconia, Ceria, Yttrium, Combustion Catalyst, Support, Low Temperature Catalyst, Organic Compound

Description

Low Temperature Catalyst for Combustion of Organic Compounds and Its Manufacturing Method {Low Temperature Catalyst for Combustion of Organic Compound, And Manufacturing Method}

The present invention relates to a low temperature catalyst for burning an organic compound and a method of manufacturing the same. More specifically, the present invention consists of a carrier consisting of a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and a rare earth metal oxide, and a noble metal catalyst component supported on the carrier, the content of zirconium (Zr) in the carrier The low temperature catalyst for the combustion of organic compounds of 50 to 100 wt% and a method for producing the same.

Catalytic combustion is a technique of burning an organic compound containing oxygen such as hydrocarbons (C1 to C5), carbon monoxide, and other harmful organic substances using a catalyst in an unsalt state.

Existing flame combustion methods for burning relatively low molecular weight organic compounds are limited in use when the fuel concentration is low due to the relatively high combustion initiation temperature and the high concentration of fuel capable of sustained combustion. In addition, there is a possibility of the generation of unburned material by incomplete combustion in the combustion process, there is a problem that harmful substances such as nitrogen oxides generated in the combustion process due to the high combustion temperature.

In contrast, catalytic combustion, which uses a catalyst for combustion, enables complete combustion even at low temperatures, which not only suppresses the generation of unburned materials due to incomplete combustion, but also makes it easy to control the temperature so that combustion can occur without generating nitrogen oxides. There is an advantage that it can.

Various types of combustion catalysts used in catalytic combustion reaction are used. As a carrier for burning hydrocarbons (C1 to C5), precious metals such as platinum, palladium, and rhodium may be added to a carrier such as Al ₂ O ₃ , SiO ₂ , or zeolite. Supported catalysts are generally used.

These catalysts have different starting temperatures for combustion reactions, depending on the method of production. However, low temperature combustion catalysts have not been developed yet, even in the low temperature range of about 200 ° C. Various types of combustion catalysts have been studied to lower reaction initiation and activation temperature.

Accordingly, the present inventors have a high activity and combustion efficiency even at a low temperature range of about 200 ° C., in place of a catalyst having a high combustion reaction temperature shown in the prior art, that is, a catalyst (C1) at low temperatures by increasing the conversion rate of the catalyst. C5) and the low temperature combustion catalyst of the present invention, which can maximize the combustion reaction of harmful organic substances such as carbon monoxide, have been developed.

An object of the present invention has a high activity and combustion efficiency even in a low temperature range, low temperature catalyst for combustion of organic compounds that can maximize the conversion of the catalyst to maximize the combustion reaction of harmful organic materials such as hydrocarbons (C1 ~ C5), carbon monoxide even at low temperatures And to provide a method for producing the same.

The present invention for achieving the above object is composed of a carrier consisting of a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxides and a noble metal catalyst component supported on the carrier, zirconium in the carrier A low temperature catalyst for the combustion of organic compounds having a (Zr) content of 50 to 100 wt% is used as the summary.

Here, the composite oxide of ceria (CeO ₂₎ of the composite oxide support is zirconia (ZrO ₂₎ and ceria (CeO ₂₎ - zirconia (ZrO ₂₎ or zirconia (ZrO ₂₎ and the tree uranium (Y ₂ O ₃₎ It is preferable that it is a yttria stabilized zirconia (YSZ) which is a complex oxide of.

In addition, the specific surface area of the zirconia (ZrO ₂ ) carrier is 15 m ² / g or less, and the specific surface area of the composite oxide carrier of the zirconia (ZrO ₂ ) and rare earth metal oxide is 30 m ² / g or less. .

The crystal size of the zirconia (ZrO ₂ ) carrier is 50 nm or more, and the crystal size of the composite oxide support of the zirconia (ZrO ₂ ) and rare earth metal oxides is 40 nm or more.

Further, the precious metal catalyst component is platinum, palladium or oxides thereof, and the supported amount of platinum, palladium or oxides thereof is preferably 0.01 to 5 wt% based on the weight of the carrier.

On the other hand, the present invention for achieving the above object, i) by firing a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxide, the zirconium (Zr) content in the carrier is 50 ~ 100wt A first step of preparing a carrier which is%; ii) impregnating the calcined carrier with a precious metal catalyst component consisting of platinum, palladium or oxides thereof so as to be 0.01 to 5 wt% based on the weight of the carrier; iii) a third step of drying the carrier impregnated with the noble metal catalyst component at 50 to 150 ° C; And iv) a fourth step of surface-modifying and activating the dried carrier by heat-treating the low temperature catalyst for combustion of an organic compound.

Here, it is preferable to sinter the carrier so that the specific surface area of the zirconia (ZrO ₂ ) carrier of the first step is 15 m ² / g or less, and the carrier is calcined so that the crystal size is 50 nm or more.

In addition, it is preferable to sinter the carrier so that the specific surface area of the composite oxide support of the zirconia (ZrO ₂ ) and the rare earth metal oxide of the first step is 30 m ² / g or less, and the carrier is formed so that the crystal size is 40 nm or more. It is preferable to bake.

By using the low temperature catalyst for burning the organic compound of the present invention and its manufacturing method, it has high activity and combustion efficiency even at a low temperature range, and increases the conversion rate of the catalyst to burn harmful organic substances such as hydrocarbons (C1 to C5) and carbon monoxide even at low temperatures. Maximize the reaction.

A low temperature catalyst for combustion of an organic compound and a method of manufacturing the same according to the present invention will be described in detail below with reference to the drawings.

1 is a graph showing the combustion conversion rate of propane gas according to the reaction temperature of the platinum-supported combustion catalyst of the zirconia carrier of Example 2, Figure 2 is a combustion catalyst loaded with platinum on a zirconia carrier having different firing temperature (Example 2, Comparative Example 21, Comparative Example 22) X-ray diffraction analysis results.

3 is an X-ray diffraction analysis result of a platinum-supported combustion catalyst (Example 3, Comparative Example 23) on a yttrium stabilized zirconia carrier having a different firing temperature, and FIG. 4 is a ceria-zirconia carrier having a different firing temperature. This is the result of X-ray diffraction analysis of a combustion catalyst (Example 4, Comparative Example 24) in which platinum was supported.

5 is a graph showing the combustion conversion rate of propane gas according to the reaction temperature of the catalyst in which palladium is supported on the zirconia carrier of Example 5. FIG.

The low temperature catalyst for combustion of an organic compound according to the present invention, which lowers the initiation temperature of the combustion catalyst and maximizes efficiency, may include a carrier made of a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxides; And a noble metal catalyst component supported on the support, wherein the content of zirconium (Zr) in the support is 50 to 100 wt%.

In this case, the complex oxide of ceria (CeO ₂₎ of the composite oxide support is zirconia (ZrO ₂₎ and ceria (CeO ₂₎ - zirconia (ZrO ₂₎ or zirconia (ZrO ₂₎ and the tree uranium (Y ₂ O ₃₎ It is preferable that it is a yttria stabilized zirconia (YSZ) which is a complex oxide of.

In addition, in order to lower the initiation temperature of the combustion catalyst and maximize the efficiency, the zirconia carrier is controlled to have a specific surface area of 15 m ² / g or less and a crystal size of 50 nm or more by controlling the calcination temperature. The carrier consisting of a composite oxide of zirconia (ZrO ₂ ) and a rare earth metal oxide is preferably adjusted to a calcination temperature such that the specific surface area of the zirconia carrier is 30 m ² / g or less and the crystal size is 40 nm or more. Do.

In addition, the noble metal catalyst component is preferably platinum, palladium or oxides thereof, wherein the amount of platinum, palladium or oxides thereof is set in an appropriate range capable of achieving the purpose of low temperature combustion, and is 0.01 to the weight of the carrier. It is preferable that it is -5 wt%.

This is because the lower limit of 0.01% by weight is the minimum supported amount for securing the activity of the catalyst, and even if the upper limit of 5% by weight or more is supported, the improvement in activity (decrease in the active temperature) cannot be detected. Platinum nitride, platinum chloride, palladium nitride, palladium chloride, etc. may be used as the platinum or palladium precursor.

Hereinafter, the reaction start temperature and activity change of the combustion catalyst according to the selection of the carrier, the specific surface area of the combustion catalyst, and the crystal size will be described through Examples 1 to 4 and Comparative Examples 1 to 24.

Example 1

0.099 g of platinum nitride was impregnated in zirconia (ZrO ₂ ) powder having a surface area of less than 5 m ² / g, dried for one day, and then calcined at 500 ° C. for 4 hours at 4 ° C./min to allow platinum to be loaded on the zirconia carrier. A catalyst (platinum catalyst) was obtained.

Platinum loading of this catalyst was 1wt% and the crystal size of zirconia determined by Scherrer's formular method based on X-ray diffraction analysis was 86.0 nm.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. The composition of the gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of 1% propane, 5% oxygen, and 94% He at 100 ml / min at atmospheric pressure. As a result, the temperatures of 10%, 50% and 100% of propane conversion were obtained, respectively, as shown in Table 1 below.

[Comparative Examples 1-20]

0.099 g of platinum nitride was impregnated into 5 g of various types of carriers, dried for one day, and calcined at 500 ° C for 4 hours at 4 ° C / min to obtain a catalyst (platinum catalyst) on which platinum was supported. As the carrier, materials having various kinds and specific surface areas were used as shown in Table 1 below.

The platinum loading of these catalysts is 1 wt%. The platinum catalyst was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. As a result, the temperatures of 10%, 50% and 100% of propane conversion were obtained, respectively, as shown in Table 1 below.

sample Carrier material Specific surface area T ₁₀ (℃) T ₅₀ (℃) T ₁₀₀ (℃) Example 1 ZrO ₂ Less than 5 m ² / g 170.2 172.3 175.0 Comparative Example 1 SiO ₂ 319.2 m ² / g 187.7 192.2 195.0 Comparative Example 2 SiO ₂ 313.4 m ² / g 186.5 192.1 195.0 Comparative Example 3 SiO ₂ 161.0 m ² / g 189.4 197.0 200.0 Comparative Example 4 SiO ₂ 5 m ² / g or less 276.7 296.1 380.0 Comparative Example 5 TiO ₂ 117.4 m ² / g 225.1 227.3 230.0 Comparative Example 6 TiO ₂ 5 m ² / g or less 200.2 202.3 205.0 Comparative Example 7 TiO ₂ 74.1 m ² / g 214.1 217.2 220.0 Comparative Example 8 TiO ₂ 52.7 m ² / g 220.0 222.2 225.0 Comparative Example 9 CeO ₂ 5 m ² / g or less 195.3 197.4 200.0 Comparative Example 10 CeO ₂ 203.0 m ² / g 232.3 253.9 265.0 Comparative Example 11 CeO ₂ 81.2 m ² / g 230.1 232.3 235.0 Comparative Example 12 Si-Al ₂ O ₃ 467.0 m ² / g 195.3 197.4 200.0 Comparative Example 13 SBA-15 718.0 m ² / g 191.0 206.6 210.0 Comparative Example 14 a-Alumina 5 m ² / g or less 273.2 301.9 350.0 Comparative Example 15 g-Alumina 148.0 m ² / g 249.8 265.7 285.0 Comparative Example 16 h-Alumina 257.0 m ² / g 270.3 295.9 310.0 Comparative Example 17 q-Alumina 92.0 m ² / g 213.5 250.1 260.0 Comparative Example 18 d-Alumina 138.0 m ² / g 246.7 268.1 280.0 Comparative Example 19 c-Alumina 164.0 m ² / g 258.6 287.1 300.0 Comparative Example 20 k-Alumina 32.0 m ² / g 216.4 222.2 300.0

It can be seen from Table 1 that the platinum catalyst having zirconia as a carrier among the various carriers exhibited 100% conversion at 175.0 ° C., showing the best activity at low temperatures.

Example 2

Zirconia was prepared by precipitating an aqueous zirconium nitride solution using aqueous ammonia solution and then raising the temperature by 4 ° C. per minute in an air atmosphere to reach 900 ° C., followed by firing for 3 hours.

Thereafter, 0.099 g of platinum nitride was impregnated into 5 g of zirconia powder, which was dried for 1 day, and then calcined at 4 ° C./min at 500 ° C. for 3 hours to obtain a catalyst (platinum catalyst) on which platinum was supported on a zirconia carrier. The platinum loading of this catalyst is 1 wt%.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. Propane conversion with temperature obtained from the compositional analysis of the gas flow at the outlet is shown in FIG. 1.

[Comparative Examples 21-22]

As a carrier, zirconia was prepared by precipitating an aqueous zirconium nitride solution using an aqueous ammonia solution and then raising the temperature by 4 ° C. per minute in an air atmosphere to reach 500 ° C. and 700 ° C., respectively, and then calcining for 3 hours.

Then, as in Example 2, 0.099 g of platinum nitride was impregnated in 5 g of zirconia powder, dried for one day, and then calcined at 4 ° C./min at 500 ° C. for 3 hours to provide a catalyst having platinum supported on the zirconia carrier ( Platinum catalyst). The platinum loading of this catalyst is 1 wt%.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. Propane conversion with temperature obtained from the compositional analysis of the gas flow at the outlet is shown in FIG. 1 together with the results of Example 2.

On the other hand, Figure 2 also confirmed that the results of the X-ray diffraction analysis of the catalysts and the comparative examples are composed only of pure zirconia particles.

In addition, Table 2 below shows the specific surface area and crystal size of the combustion catalyst of Example 2 and Comparative Examples 21 and 22. The crystal size was measured using Scherrer's formular method.

sample Carrier firing temperature (℃) Specific surface area (m ² / g) Crystal size (nm) Example 2 900 3.5 75.1 Comparative Example 21 500 94.0 20.2 Comparative Example 22 700 18.2 45.4

As can be seen from Table 2 and Figure 1, the platinum catalyst having the smallest specific surface area in the outlet flow was confirmed that the combustion reaction occurs at a low temperature. That is, in Example 2 having a specific surface area of about 3.5 m ² / g, the reaction activity was lowered at a temperature of at least 20 ° C. to 70 ° C. lower than that of the comparative example having a specific surface area of 94.0 and 18.2 m ² / g. It was confirmed that high.

Example 3

As a carrier, yttrium-stabilized zirconia (YSZ) calcined at 1000 ° C. for 3 hours in an air atmosphere was used, and platinum was supported as a catalyst metal to prepare a catalyst. The yttria content in the carrier was 14.5%.

0.099 g of platinum nitride was impregnated in 5 g of yttrium-stabilized zirconia (YSZ) powder, dried for one day, and then calcined at 4 ° C./min at 500 ° C. for 3 hours to a yttrium-stabilized zirconia (YSZ) carrier. A platinum-supported catalyst (platinum catalyst) was obtained, at which time the platinum loading of the catalyst was 1 wt%.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. As a result, the conversion rate of propane was 10%, 50% and 100%, respectively.

Comparative Example 23

As a carrier, yttrium-stabilized zirconia (YSZ) calcined at 500 ° C. for 3 hours in an air atmosphere was used, and a catalyst was prepared by supporting platinum as a catalyst metal. The yttria content in the carrier was 14.5%.

Yttrium-stabilized zirconia (YSZ) carrier by impregnating 0.099 g of platinum nitride with 5 g of yttrium-stabilized zirconia (YSZ) powder, drying it for one day, and then firing at 500 ° C for 4 hours at 4 ° C / min. A catalyst (platinum catalyst) on which platinum was supported was obtained. The platinum loading of the catalyst was 1 wt%.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of the gas flow at the outlet was analyzed at 5 ° C intervals while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml / min. As a result, the conversion rate of propane was 10%, 50% and 100%, respectively.

sample T ₁₀ (℃) T ₅₀ (℃) T ₁₀₀ (℃) Example 3 188.7 192.3 195 Comparative Example 23 240.3 242.4 245

In addition, Table 4 shows the specific surface area and the crystal size according to the firing temperature of the catalyst. The crystal size was expressed using Scherrer's formular method.

sample Carrier firing temperature (℃) Specific surface area (m ² / g) Crystal size (nm) Example 3 1000 21.7 43.2 Comparative Example 23 500 142.6 16.2

As can be seen from Tables 3 and 4, as the surface area of the carrier decreases in the outlet flow, it was confirmed that the lowering of the combustion initiation temperature was achieved, and the yttrium-stabilized zirconia (YSZ) containing a large amount of yttria component was observed. It was confirmed that the catalyst efficiently carried out the combustion reaction at a low temperature of 200 ℃ or less.

That is, it was confirmed that exhibit about 21.7m ² / g specific surface area having a third embodiment of the case 142.6m ² / g when the comparative example having a specific surface area of about 50 ℃ more reaction activity at a lower temperature than the.

On the other hand, Figure 3 as a result of the X-ray diffraction analysis of the catalysts, it was confirmed that the examples and comparative examples are composed only of pure yttrium-stabilized zirconia (YSZ) component.

Example 4

Ceria-zirconium oxide calcined at 1000 ° C. for 3 hours was used as a carrier, and platinum was supported as a catalyst metal to prepare a catalyst. 0.099 g of platinum nitride was impregnated into 5 g of ceria-zirconium oxide powder, which was dried for one day, and then calcined at 500 ° C. at 4 ° C./min for 3 hours to carry the platinum supported on the ceria-zirconium carrier. (Platinum catalyst) was obtained. The platinum loading of the catalyst was 1 wt%.

The prepared platinum catalyst was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. As a result, the conversion rate of propane was 10%, 50% and 100%, respectively, to obtain the temperatures shown in Table 5 below.

Comparative Example 24

A catalyst was prepared by supporting ceria-zirconium oxide calcined at 500 ° C. for 3 hours in air as a carrier and supporting platinum as a catalyst metal. 0.099 g of platinum nitride was impregnated with 5 g of ceria-zirconium oxide powder, which was dried for one day, and then calcined at 500 ° C. at 4 ° C./min for 3 hours to carry the platinum supported on the ceria-zirconium carrier. (Platinum catalyst) was obtained. The platinum loading of the catalyst was 1 wt%.

The prepared platinum catalyst was pelletized to charge 0.1 g in a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. As a result, the conversion rate of propane was 10%, 50% and 100%, respectively, to obtain the temperatures shown in Table 5 below.

sample T ₁₀ (℃) T ₅₀ (℃) T ₁₀₀ (℃) Example 4 200.1 202.3 205 Comparative Example 24 233.4 237.2 240

In addition, Table 6 shows the specific surface area and crystal size according to the firing temperature of the catalyst. The crystal size was expressed using Scherrer's formular method.

sample Carrier firing temperature (℃) Specific surface area (m ² / g) Crystal size (nm) Example 4 1000 20.6 41.9 Comparative Example 24 500 104.7 34.3

As can be seen from Tables 5 and 6, it was confirmed that the combustion initiation temperature is lowered as the surface area of the carrier decreases in the outlet stream, and the ceria-zirconium oxide catalyst containing ceria component is around 200 ° C. It was confirmed that the combustion reaction was performed efficiently at low temperature.

That is, it was confirmed that exhibit about 20.6m ² / g specific surface area having a fourth embodiment of the reaction activity in the case of about 40 ℃ degree lower temperature than the case of the comparison with the specific surface area of 104.7m ² / g on.

On the other hand, Figure 4 as a result of the X-ray diffraction analysis of the catalysts, it was confirmed that the examples and comparative examples are composed only of pure ceria-zirconium oxide catalyst component.

Hereinafter, the reaction initiation temperature and activity change of methanol combustion of a propane combustion of a combustion catalyst using a palladium catalyst on a zirconia (ZrO ₂ ) support and a combustion catalyst using a platinum catalyst on a zirconia (ZrO ₂ ) support will be described through Examples 5 and 6 Take a look.

Example 5

0.125 g of palladium nitride is impregnated in 5 g of zirconia (surface area: 5 m ² / g or less) powder, dried for one day, and then calcined at 500 ° C. for 4 hours at 4 ° C./min to support palladium on the zirconia carrier. Obtained catalyst (palladium catalyst).

The palladium loading of this catalyst is 1wt% and the crystal size of zirconia determined by Scherrer's formular method based on X-ray diffraction analysis is 86.0 nm.

Palladium catalyst loaded on zirconia was pelletized to charge 0.1 g into a fixed bed tubular reactor. Here, the composition of gas flow at the outlet was analyzed at intervals of 5 ° C. while flowing a gas having a composition of propane 1%, oxygen 5%, and He 94% at atmospheric pressure at 100 ml per minute. As a result, the conversion rate of propane according to the reaction temperature was obtained and shown in FIG. 5.

Example 6

0.099 g of platinum nitride was impregnated into 5 g of zirconia (surface area: 5 m ² / g) powder, which was dried for one day, and then calcined at 500 ° C. for 4 hours at 4 ° C./min, whereby platinum was supported on the zirconia carrier. A catalyst (platinum catalyst) was obtained.

The platinum loading of this catalyst was 1% by weight and the crystal size of zirconia determined by Scherrer's formular method based on X-ray diffraction analysis was 86.0 nm.

A platinum catalyst supported on zirconia was pelletized to charge 0.1 g in a fixed bed tubular reactor. The composition of the gas flow at the outlet was analyzed while flowing a gas having a composition of 5.4% methanol, 10% oxygen, and 84.6% He at 100 ml / min at atmospheric pressure. As a result, it was confirmed that 100% conversion of methanol at 45 ° C.

As can be seen from the examples and comparative examples of the various conditions described above, using a noble metal catalyst using the zirconia or zirconia-containing composite oxide carrier of the present invention with appropriate control of the specific surface area and crystal size, even in a low temperature range By increasing the conversion rate of the catalyst it is possible to maximize the combustion reaction of harmful organic substances such as hydrocarbons (C1 ~ C5), carbon monoxide, even at low temperatures.

On the other hand, the low temperature catalyst for combustion of an organic compound according to the present invention to lower the starting temperature and maximize the efficiency as described above, i) by firing a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxide, A first step of preparing a carrier having a zirconium (Zr) content in the carrier of 50 to 100 wt%; ii) impregnating the calcined carrier with a precious metal catalyst component consisting of platinum, palladium or oxides thereof so as to be 0.01 to 5 wt% based on the weight of the carrier; iii) a third step of drying the carrier impregnated with the noble metal catalyst component at 50 to 150 ° C; And iv) a fourth step of modifying and activating the surface of the catalyst by heat-treating the dried carrier.

Here, the composite oxide support is prepared in the first step is zirconia (ZrO ₂₎ and ceria (CeO ₂₎ a composite oxide of ceria of (CeO ₂₎ as described in the low-temperature combustion of the organic compound catalyst-zirconia (ZrO ₂ ) Or yttria stabilized zirconia (YSZ), which is a composite oxide of zirconia (ZrO ₂ ) and yttrium (Y ₂ O ₃ ).

On the other hand, in order to lower the initiation temperature of the combustion catalyst and maximize the efficiency, in the first step, it is preferable to fire the zirconia (ZrO ₂ ) carrier so that the specific surface area is 15 m ² / g or less, and the crystal size is 50 nm. It is preferable to fire zirconia (ZrO ₂ ) so that it may become the above.

In addition, it is preferable to fire the carrier so that the specific surface area of the composite oxide carrier of zirconia (ZrO ₂ ) and rare earth metal oxide is 30 m ² / g or less, and it is preferable to fire the carrier so that the crystal size is 40 nm or more. .

In addition, the activation step of the third step may include a) a third step of heat treatment using a gas containing oxygen; And b) a third step of heat treatment using a reducing gas containing hydrogen, wherein the surface of the catalyst component is modified.

The present invention is not limited to the above-described specific embodiments and descriptions, and various modifications can be made to those skilled in the art without departing from the gist of the present invention claimed in the claims. And such modifications are within the scope of protection of the present invention.

1 is a graph showing the combustion conversion rate of propane gas according to the reaction temperature of the combustion catalyst loaded with platinum on the zirconia carrier of Example 2.

2 is an X-ray diffraction analysis of a combustion catalyst (Example 2, Comparative Example 21, Comparative Example 22) in which platinum is supported on zirconia carriers having different firing temperatures.

FIG. 3 shows the results of X-ray diffraction analysis of a combustion catalyst (Example 3, Comparative Example 23) loaded with platinum on a yttrium stabilized zirconia carrier having a different firing temperature.

4 is an X-ray diffraction analysis result of a combustion catalyst (Example 4, Comparative Example 24) loaded with platinum on a ceria-zirconia carrier having a different firing temperature.

FIG. 5 is a graph showing the combustion conversion rate of propane gas according to the reaction temperature of a catalyst having palladium supported on the zirconia carrier of Example 5. FIG.

Claims (13)

Carrier consisting of a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxides; And a noble metal catalyst component supported on the support, wherein the zirconium (Zr) content in the support is 50 to 100 wt%. According to claim 1, wherein the composite oxide support is zirconia (ZrO ₂₎ and ceria (CeO ₂₎ a composite oxide of ceria (CeO ₂₎ in-zirconia (ZrO ₂₎ in the combustion of organic compound catalyst according to claim. The organic compound according to claim 1, wherein the composite oxide carrier is yttria stabilized zirconia (YSZ), which is a composite oxide of zirconia (ZrO ₂ ) and yttrium (Y ₂ O ₃ ). Combustion catalyst. The catalyst for combustion of an organic compound according to claim 1, wherein the specific surface area of the zirconia (ZrO ₂ ) carrier is 15 m ² / g or less. The catalyst for combustion of an organic compound according to claim 1, wherein the specific surface area of the composite oxide carrier of zirconia (ZrO ₂ ) and rare earth metal oxide is 30 m ² / g or less. The catalyst for combustion of an organic compound according to claim 1, wherein the zirconia (ZrO ₂ ) carrier has a crystal size of 50 nm or more. The catalyst for burning an organic compound according to claim 1, wherein the crystal size of the composite oxide support of zirconia (ZrO ₂ ) and rare earth metal oxide is 40 nm or more. The organic compound combustion according to claim 1, wherein the noble metal catalyst component is platinum, palladium or oxides thereof, and the supported amount of platinum, palladium or oxides thereof is 0.01 to 5 wt% based on the weight of the carrier. Catalyst. i) calcining a composite oxide of zirconia (ZrO ₂ ) or zirconia (ZrO ₂ ) and rare earth metal oxides to prepare a carrier having a zirconium (Zr) content of 50 to 100 wt%; ii) impregnating the calcined carrier with a precious metal catalyst component consisting of platinum, palladium or oxides thereof so as to be 0.01 to 5 wt% based on the weight of the carrier; iii) a third step of drying the carrier impregnated with the noble metal catalyst component at 50 to 150 ° C; And iv) a fourth step of modifying and activating a catalyst surface by heat treating the dried carrier; Method for producing an organic compound combustion catalyst comprising a. 10. The method of claim 9, wherein the carrier is calcined such that the specific surface area of the zirconia (ZrO ₂ ) carrier of the first step is 15 m ² / g or less. 10. The method of claim 9, wherein the carrier is calcined such that the crystal size of the zirconia (ZrO ₂ ) carrier of the first step is 50 nm or more. 10. The catalyst for burning an organic compound according to claim 9, wherein the carrier is calcined such that the specific surface area of the composite oxide carrier of the zirconia (ZrO ₂ ) and the rare earth metal oxide of the first step is 30 m ² / g or less. Manufacturing method. 10. The method of claim 9, wherein the support is calcined so that the crystal size of the complex oxide support of the zirconia (ZrO ₂ ) and the rare earth metal oxide of the first step is 40 nm or more.

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