Exhaust gas purification catalytic converter composition and exhaust gas purification catalytic converter

Description

TECHNICAL FIELD

[0001] The present invention relates to an exhaust gas purification catalyst composition which is used for purifying an exhaust gas to be emitted from an internal-combustion engine such as a gasoline engine of two-wheel or four-wheel automobiles or the like and an exhaust gas purification catalyst in which the composition is supported on a substrate. More specifically, the invention relates to an exhaust gas purification catalyst having excellent purification performance for NO x under lean conditions.BACKGROUND ART

[0002] An exhaust gas of automobiles which use gasoline for fuel contains hazardous components such as hydrocarbon (THC), carbon monoxide (CO), and nitrogen oxide (NO x ). Therefore, it is necessary to purify each of the hazardous components in such a manner that the hydrocarbon (THC) is converted into water and carbon dioxide by oxidation; the carbon monoxide (CO) is converted into the carbon dioxide by oxidation; and the nitrogen oxide (NO x ) is converted into nitrogen by reduction.

[0003] As a catalyst (hereinafter, referred to as an "exhaust gas purification catalyst") adapted to treat these exhaust gases, three way catalysts (TWC) capable of being used for a redox of CO, THC, and NO x have been used.

[0004] Three way catalysts are well known, in which a precious metal such as Pt, Pd, and Rh is supported on a refractory oxide porous material having a high-specific surface area, for example, an alumina porous material having a high-specific surface area and the precious metal is supported on a substrate, for example, a monolithic substrate made of a refractory ceramic or metallic honeycomb structure or on refractory particles.

[0005] Since purification characteristics (three way characteristics) for CO, HC, and NO x due to the three way catalysts are closely related to a stoichiometric air-fuel ratio (A / F) representing the atmosphere of an automobile exhaust gas, the three way catalysts were generally controlled to the following conditions in the past: A / F was around 14.6 (stoichiometric air-fuel ratio) in which exhaust gas purification function was sufficiently exhibited, in other words, an excess air ratio λ was near 1.

[0006] In recent years, from the viewpoint of improving fuel efficiency and reducing the carbon dioxide emission amount, an engine is desirably controlled in a slightly lean area in which the air-fuel ratio is higher than the stoichiometric air-fuel ratio (A / F = 14.6), that is, satisfies a level of 14.6 < A / F ≤ 16.0. In the case of a slightly lean control to make a lean combustion in an oxygen-rich atmosphere, since the amount of fuel to be used is reduced, the fuel efficiency can be improved and the generation of CO 2 as a combustion exhaust gas can also be suppressed.

[0007] However, since the oxygen becomes excessive and the purification performance of exhaust gas purification catalyst for NO x is extremely deteriorated under the lean condition as described above, catalysts have been desirably developed which can purify NO x with high efficiency even under the lean condition.

[0008] As the catalyst capable of purifying NO x with high efficiency even under the lean condition, the applicant has proposed a catalyst in which Rh is supported on a carrier consisting of zirconium phosphate (Patent Document 1).

[0009] JP H06 55075 A discloses an exhaust gas purification catalyst comprising a platinum group metal supported on zirconium phosphate and ceria.CITATION LISTPATENT DOCUMENT

[0010] Patent Document 1: WO 2013035568 A1 corresponding to EP 2 754 489 A1SUMMARY OF THE INVENTIONPROBLEM TO BE SOLVED BY THE INVENTION

[0011] Compared with the catalyst disclosed in Patent Document 1, that is, the catalyst in which Rh is supported on the carrier consisting of the zirconium phosphate, the invention is to provide a novel catalyst that can further improve the purification performance for NO x under the lean condition.MEANS FOR SOLVING PROBLEM

[0012] The invention is to propose an exhaust gas purification catalyst composition including: a carrier A comprising a zirconium phosphate; a catalytically active component (a) comprising Rh supported on the carrier A; a carrier B consisting of one or more inorganic oxide porous materials selected from silica, ceria-zirconia, lanthana, alumina, and titania; and a catalytically active component (b) which is Pt supported on the carrier B.

[0013] In addition, as an exhaust gas purification catalyst, the invention is to propose an exhaust gas purification catalyst having a structure in which the exhaust gas purification catalyst composition is supported on a substrate and an exhaust gas purification catalyst having a structure in which the exhaust gas purification catalyst composition is formed into a pellet shape.EFFECT OF THE INVENTION

[0014] According to the exhaust gas purification catalyst composition of the invention and the catalyst using the same, it is possible to further improve the purification performance for NO x under the lean condition even compared with the catalyst disclosed in Patent Document 1, that is, the catalyst in which Rh is supported on the carrier consisting of the zirconium phosphate. More specifically, it is possible to accelerate a reduction reaction of NO x using each of CO and C 3 H 6 as a reducing agent (CO-NO reaction, C 3 H 6 -NO reaction) and to exhibit the particularly excellent purification performance for NO x in an area of 14.6 < A / F ≤ 16.0 even under the lean condition. MODE(S) FOR CARRYING OUT THE INVENTION

[0015] Next, embodiments of the invention will be described.<Present catalyst composition>

[0016] An exhaust gas purification catalyst composition (referred to as a "present catalyst composition") according to an embodiment is an exhaust gas purification catalyst composition comprising: a carrier A comprising a zirconium phosphate; a catalytically active component (a) comprising Rh supported on the carrier A; a carrier B consisting of one or more inorganic oxide porous materials selected from silica, ceria-zirconia, lanthana, alumina, and titania; and a catalytically active component (b) which is Pt supported on the carrier B.(Carrier A)

[0017] The carrier A is a carrier comprising a zirconium phosphate.

[0018] The zirconium phosphate may be either a crystalline substance or an amorphous substance. Among them, the crystalline zirconium phosphate is preferred, and a zirconium phosphate represented by ZrP 2 O 7 is particularly preferred.

[0019] A method of producing the zirconium phosphate is not particularly limited. Examples of the method may include a coprecipitation method and a hydrothermal method.

[0020] The carrier A comprising the zirconium phosphate is not a porous material and is different from an inorganic porous material such as alumina or zirconia in terms of being present in a dense state.

[0021] A specific surface area of the carrier A comprising a zirconium phosphate has usually a value of 1 to 100 m 2< / g which is measured by a BET method. In order to sufficiently obtain reaction activity, it is preferable to ensure a specific surface area of a certain value or more. However, when an initial specific surface area is too high, pores are filled when a thermal load is applied and a precious metal present on a surface can be easily buried. From this viewpoint, the specific surface area of the carrier A comprising a zirconium phosphate is preferably 1 m 2< / g or more or 30 m 2< / g or less and more preferably 3 m 2< / g or more or 15 m 2< / g or less as a value measured by the BET method.

[0022] An average diameter of the carrier A comprising a zirconium phosphate is usually 1 to 40 µm and preferably 5 µm or more or 20 µm or less. With respect to the average diameter of the carrier A, the carrier A is directly observed by SEM to measure its diameter, and thus the average diameter can be calculated.(Catalytically active component (a))

[0023] From the viewpoint of increasing purification performance for NO x under lean conditions, the catalytically active component (a) includes rhodium (Rh).

[0024] In terms of enhancing catalyst activity and preventing aggregation of components when subjected to a thermal load, the catalytically active component (a) may be contained in the carrier A by a ratio of 0.1 to 1.0 wt% and is preferably contained in the carrier A by a ratio of 0.1 to 0.5 wt%.(Carrier B)

[0025] The carrier B consists of one or more inorganic oxide porous materials.

[0026] In order to increase activity of a precious metal, the porous material preferably has proper acidity. Therefore, the inorganic oxide porous material contained in the carrier B may preferably be an oxide porous material having a Hammett acidity function H 0max of -10 < H 0max < 15. Sintering of an active component can be suppressed when the H 0max is greater than -10, whereas the reduction in activity due to stabilization of an active component oxide can be suppressed when the H 0max is less than 15. From these viewpoints, the inorganic oxide porous material contained in the carrier B may preferably be an oxide porous material having a Hammett acidity function H 0max of -10 < H 0max < 15 and may further preferably be an oxide porous material having a Hammett acidity function H 0max of 0 or more or 10 or less.

[0027] The oxide porous materials are selected from silica, ceria-zirconia, lanthana, alumina, and titania. Each of these oxide porous materials can be used singly or two kinds or more thereof can be used in combination with each other. From the viewpoint of increasing purification performance for NO x under lean conditions, the oxide porous material particularly preferably includes titania.

[0028] A specific surface area of the carrier B has usually a value of 10 to 200 m 2< / g and preferably 30 m 2< / g or more or 150 m 2< / g or less which is measured by the BET method.

[0029] An average diameter of the carrier B is usually 1 µm to 40 µm and preferably 5 µm or more or 20 µm or less.

[0030] With respect to the average diameter of the carrier B, the carrier B is directly observed by SEM to measure its diameter, and thus the average diameter can be calculated.

[0031] The sizes of the carrier A and the carrier B are not particularly limited as long as the sizes of the carrier A and the carrier B are different from each other to such an extent that the carrier A supports the carrier B and vice versa. Accordingly, the ratio of the average diameter of the carrier A to that of the carrier B may be 1 : 40 to 40 : 1 and particularly preferably 5 : 20 to 20 : 5.

[0032] The carrier A and the carrier B may contain impurities within a range of not damaging effects of the invention.(Catalytically active component (b))

[0033] From the viewpoint of increasing purification performance for NO x under lean conditions, the catalytically active component (b) particularly preferably is platinum (Pt).

[0034] In terms of enhancing catalyst activity and preventing aggregation of components when subjected to a thermal load, the catalytically active component (b) may be contained in the carrier B by a ratio of 0.1 to 1.0 wt% and is preferably contained in the carrier B by a ratio of 0.1 to 0.5 wt%.(Other components capable of being contained in present catalyst composition)

[0035] The present catalyst composition may contain other components. For example, the present catalyst composition may contain a binder, a stabilizer, an OSC material, or other components.

[0036] Examples of the binder component may include an inorganic binder, for example, an aqueous solution such as alumina sol, silica sol, or zirconia sol. These can take a form of an inorganic oxide when being calcined.

[0037] Examples of the stabilizer may include an alkaline-earth metal or an alkaline metal. Particularly, the stabilizer can be selected from one kind or two or more kinds of metals selected from the group consisting of magnesium, barium, calcium, and strontium, and preferably, the stabilizer can be selected from one kind or two or more kinds of metals selected from the group consisting of strontium and barium.

[0038] The OSC material may be a material having an oxygen storage capacity (OSC). For example, the OSC material may include cerium compound particles, zirconium compound particles, and ceria-zirconia particles.(Production method of present catalyst composition)

[0039] The carrier A comprising the zirconium phosphate, the catalytically active component (a), water, and other raw materials as needed are mixed and stirred with each other to obtain a slurry, whereas the carrier B consisting of one or more of the inorganic oxide porous materials, the catalytically active component (b), water, and other raw materials as needed are mixed and stirred with each other to obtain a slurry. Thereafter, both slurries are mixed with each and dried as needed, whereby it is possible to obtain the present catalyst composition.<Present catalyst>

[0040] Next, a catalyst for exhaust gas purification (hereinafter, referred to as a "present catalyst") will be described, which can be prepared using the present catalyst composition.

[0041] The present catalyst can be prepared in such a manner that the present catalyst composition is supported on a substrate.

[0042] In addition, the present catalyst can be prepared in such a manner that the present catalyst composition is formed into a pellet shape.

[0043] As a specific configuration example of the present catalyst, for example, the present catalyst may include a catalyst provided with a catalyst layer which is formed through processes of preparing a slurry by mixing the present catalyst composition with water and other components, stirring the mixed present catalyst composition using a ball mill, and applying the slurry on a substrate by a wash coat.

[0044] In addition, another example of the present catalyst may include a catalyst provided with a catalyst layer which is formed on the surface of the substrate through processes of preparing a slurry by mixing the present catalyst composition with water and other components and stirring the mixed present catalyst composition using a ball mill, immersing the substrate into the slurry, and then pulling up the immersed substrate to calcine it.

[0045] However, the method of producing the present catalyst can employ all of the known methods as a part of the processes, and is not limited to the above examples.(Substrate)

[0046] Examples of the substrate material used in the present catalyst may include refractory materials such as ceramics or metal materials.

[0047] Examples of the ceramic substrate material may include a refractory ceramic material, for example, cordierite, cordierite-alpha alumina, silicon nitride, zircon mullite, spodumene, alumina-silica magnesia, zircon silicate, sillimanite, magnesium silicate, zircon, petalite, alpha alumina, and alumino-silicates.

[0048] Examples of the metal substrate material may include a refractory metal, for example, other suitable corrosion-resistant alloys based on stainless steel or iron.

[0049] The shape of the substrate may include a honeycomb shape, a pellet shape, or a spherical shape.

[0050] The honeycomb material may generally use, for example, a cordierite material such as the ceramics in many cases. In addition, the honeycomb material may use the honeycomb formed of a metal material such as ferritic stainless steel.

[0051] In the case of using the substrate of the honeycomb shape, for example, it is possible to use a monolithic substrate which has a plurality of minute gas flow passages, that is, channels parallel to each other inside the substrate so that fluid flows through the inside of the substrate. At this time, catalyst compositions may be coated on the inner wall surface of each channel of the monolithic substrate by the wash coat to form the catalyst layer.(Catalyst layer)

[0052] The catalyst layer may be stacked with one or two or more in a vertical direction, and another catalyst layer may be formed in a flowing direction of an exhaust gas.<Explanation of expressions>

[0053] In this specification, when the expression "X to Y" (X and Y are arbitrary numbers) is used, unless otherwise explicitly mentioned, the meaning of "X or greater but Y or less" is included and at the same time, the meaning of "preferably greater than X" or "preferably less than Y" is included.

[0054] In addition, the expression "X or greater" (X is an arbitrary number) or "Y or less" (Y is an arbitrary number) includes the intention of "it is preferable to be greater than X" or "it is preferable to be less than Y". Examples

[0055] Hereinafter, the invention will be further described in detail based on the following Examples and Comparative Examples.<Synthesis of zirconium phosphate (ZrP 2 O 7 )>

[0056] After zirconium oxynitrate dihydrate of 203.6 g was dissolved in deionized water, aqueous ammonia of 4 mol / L was slowly added dropwise to a solution charged with 85%-phosphate of 173.9 g to obtain a value of pH 8, and the obtained gel-like product was washed and filtered with deionized water and was then subjected to drying at 120°C through the night. After the drying, the product was calcined at 900°C for five hours in the air to obtain zirconium phosphate (ZrP 2 O 7 ).<Example 1>

[0057] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above and La-stabilized alumina (H 0max : 7.1) were individually made into a slurry by a wet grinding treatment. The specific surface area (BET) of the zirconium phosphate (ZrP 2 O 7 ) after the grinding was 6.7 m 2< / g (the specific surface area (BET) of zirconium phosphate (ZrP 2 O 7 ) used in the following Examples is also the same). The zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours. Meanwhile, the La-stabilized alumina was dispersed into the deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0058] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained the La-stabilized alumina of 21 parts by mass, and the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of the La-stabilized alumina.

[0059] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L to obtain a catalyst layer formed on the ceramic honeycomb substrate and the resultant was used as a honeycomb catalyst for activity evaluation.

[0060] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on the La-stabilized alumina.<Example 2>

[0061] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above and a ceria-zirconia composite oxide (CeO 2 -ZrO 2 ) were individually made into a slurry by a wet grinding treatment. The zirconium phosphate slurry was added with an Rh salt solution and was then stirred for two hours. Meanwhile, the ceria-zirconia composite oxide (CeO 2 -ZrO 2 ) was dispersed into deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0062] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained the ceria-zirconia composite oxide (CeO 2 -ZrO 2 ) of 21 parts by mass, and the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of the ceria-zirconia composite oxide (CeO 2 -ZrO 2 ).

[0063] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L to obtain a catalyst layer formed on the ceramic honeycomb substrate and the resultant was used as a honeycomb catalyst for activity evaluation.

[0064] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on the ceria-zirconia composite oxide (CeO 2 -ZrO 2 ).<Comparative Example 3>

[0065] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above was made into a slurry by a wet grinding treatment. The zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours. Meanwhile, CeO 2 was dispersed into deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0066] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained CeO 2 of 21 parts by mass, the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of CeO 2 .

[0067] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L and the resultant was used as a honeycomb catalyst for activity evaluation.

[0068] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on CeO 2 .<Reference Example 4>

[0069] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above was made into a slurry by a wet grinding treatment. The zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours. Meanwhile, ZrO 2 (H 0max : 9.3) was dispersed into deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0070] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained ZrO 2 of 21 parts by mass, and the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of ZrO 2 .

[0071] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L and the resultant was used as a honeycomb catalyst for activity evaluation.

[0072] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on ZrO 2 .<Example 5>

[0073] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above was made into a slurry by a wet grinding treatment. The zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours. Meanwhile, TiO 2 (H 0max : 4.3) was dispersed into deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0074] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained TiO 2 of 21 parts by mass, and the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of TiO 2 .

[0075] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L and the resultant was used as a honeycomb catalyst for activity evaluation.

[0076] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on TiO 2 .<Example 6>

[0077] The zirconium phosphate (ZrP 2 O 7 ) obtained as described above was made into a slurry by a wet grinding treatment. The zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours. Meanwhile, SiO 2 (H 0max : 3.3) was dispersed into deionized water to obtain a slurry, and the resulting slurry was added with a Pt salt solution and was then stirred for two hours. Thereafter, the stirred mixture was added to the Rh-containing zirconium phosphate slurry and was then stirred for one hour, and then a binder component was added thereto.

[0078] With respect to various components contained in the slurry, when the zirconium phosphate was set to be 73 parts by mass, the slurry contained SiO 2 of 21 parts by mass, and the binder of 6 parts by mass, Rh of 0.14 wt% with respect to the total mass of the zirconium phosphate, and Pt of 0.24 wt% with respect to the total mass of SiO 2 .

[0079] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L and the resultant was used as a honeycomb catalyst for activity evaluation.

[0080] In the catalyst layer, Rh of 0.10 g / L was supported on a carrier consisting of the zirconium phosphate and Pt of 0.05 g / L was supported on SiO 2 .<Comparative Example 1>

[0081] The zirconium phosphate (ZrP 2 O 7 ) and La-stabilized alumina obtained as described above were individually made into a slurry by a wet grinding treatment. After the zirconium phosphate slurry was added with a Rh salt solution and was then stirred for two hours, the stirred mixture was added with the La-stabilized alumina slurry and was then stirred for one hour, and then a binder component was added thereto.

[0082] Rh was set to contain 0.21 wt% with respect to the total mass of the zirconium phosphate.

[0083] The resulting slurry was dried and calcined in a state of being coated on a ceramic honeycomb substrate by 100 g / L and the resultant was used as a honeycomb catalyst for activity evaluation.

[0084] In the catalyst layer, Rh of 0.15 g / L was supported on a carrier consisting of the zirconium phosphate.<Evaluation method of catalyst performance>

[0085] A / F scanning evaluation of the honeycomb catalyst was performed in the following manner: a complete-combustion-simulated exhaust gas consisting of CO, CO 2 , C 3 H 6 , O 2 , NO, and H 2 O, the balance being N 2 was subjected to scanning until A / F was 15.0 to 15.3 (until CO and O 2 concentration was changed) and flowed through the ceramic honeycomb catalyst at an SV of 100,000 h -1< ; and an outlet gas component was measured at 400°C using a CO / HC / NO analyzer (MOTOR EXHAUST GAS ANALYZER MEXA9100 made by HORIBA Ltd.) to compare the performance of each Rh-supporting catalyst.

[0086] By the A / F scanning evaluation of the honeycomb catalyst, the performance comparison was performed on the catalyst after the simulated exhaust gas was used for a long period. With respect to endurance condition of the simulated exhaust gas, a catalyst was placed in an electric furnace maintained at 800°C, and to the furnace accommodating the catalyst, a gas mixture (for 20 s) of C 3 H 6 and CO or C 3 H 6 and O 2 (complete combustion ratio), and air (for 10 s) were alternately and periodically fed for 50 hours.

[0087] A purification rate (%) of NO x in an A / F sweep test of C 3 H 6 -CO-NO reaction for each catalyst was indicated in Table 1, a purification rate (%) of NO x in an A / F sweep test of C 3 H 6 -NO reaction for each catalyst was indicated in Table 2, and a purification rate (%) of NO x in an A / F sweep test of CO-NO reaction for each catalyst was indicated in Table 3.

[0088] In Tables 1 to 3, "Al 2 O 3 " indicates La-stabilized alumina, "MO x " indicates an inorganic oxide, and "ZPO" indicates zirconium phosphate (ZrP 2 O 7 ). [Table 1]Cat.A / F15.015.115.215.3Comparative Example 1Rh / ZPO+Al 2 O 3 47.634.325.617.3Rh / ZPO+Pt / MO x Example 1MO x =Al 2 O 3 (7.1)54.748.541.535.3Example 2MO x =CeO 2 -ZrO 2 50.040.234.227.9Comparative Example 3MO x =CeO 2 32.724.920.314.5Reference Example 4MO x =ZrO 2 (9.3)21.019.918.916.9Example 5MO x =TiO 2 (4.3)62.153.246.337.8Example 6MO x =SiO 2 (3.3)53.047.642.736.3* Numeric values in parenthesis indicate Hammett acidity functions. [Table 2] Cat.A / F15.015.115.215.3Comparative Example 1Rh / ZPO+Al 2 O 3 16.39.95.43.2Rh / ZPO+Pt / MO x Example 1MO x =Al 2 O 3 29.627.424.723.7Example 5MO x =TiO 2 34.029.024.621.4Example 6MO x =SiO 2 45.933.727.022.4 [Table 3] Cat.A / F15.015.115.215.3Comparative Example 1Rh / ZPO+Al 2 O 3 43.333.428.122.2Rh / ZPO+Pt / MO x Example 1MO x =Al 2 O 3 55.343.836.929.3Example 5MO x =TiO 2 66.254.747.739.6Example 6MO x =SiO 2 53.545.540.334.0 (Results of evaluation)

[0089] As seen from Table 1, purification performance for NO x was significantly improved under lean conditions in Example 1 compared with Comparative Example 1, and excellent purification performance for NO x was shown in an area of 15.0 ≤ A / F ≤ 15.3 when an Rh / zirconium phosphate was added with an Pt-supported inorganic oxide.

[0090] In Examples 1, 2, 5 and 6 in Table 1, the purification performance for NO x was reduced when a basic metal oxide having a value of Hammett acidity function higher than that of Al 2 O 3 was added. However, purification capability for NO x equal to or higher than that of Example 1 was shown when a metal oxide having a value of Hammett acidity function equal to or lower than that of Al 2 O 3 was added. In particular, higher purification performance for NO x was observed in a lean area of 15.0 ≤ A / F ≤ 15.3 in Example 5 compared with Comparative Example 1.

[0091] In C 3 H 6 -NO reaction in Table 2, the improvement in purification capability for NO x was observed in Examples 1, 5, and 6 compared with Comparative Example 1, and particularly, the same level of purification capability for NO x was shown in an area of A / F ≥ 15.2 regardless of kinds of metal oxides. This is considered because the effect of Pt is remarkable for the C 3 H 6 -NO reaction in a lean area of A / F ≥ 15.2.

[0092] In CO-NO reaction in Table 3, the improvement in purification capability for NO x was observed in Examples 1, 5, and 6 compared with Comparative Example 1. The purification capability for NO x was greatly varied depending on kinds of metal oxides, and particularly, the purification capability for NO x was significantly improved in Example 5.

[0093] From the above, it is considered that performance is specifically improved due to acceleration of the C 3 H 6 -NO reaction by addition of Pt and improvement of CO-NO reactivity by addition of TiO 2 in Example 5 in Table 1.

Claims

1. An exhaust gas purification catalyst composition comprising: a carrier A comprising a zirconium phosphate; a catalytically active component (a) supported on the carrier A; a carrier B comprising an inorganic oxide porous material; and a catalytically active component (b) supported on the carrier B, wherein the carrier B consists of one or more inorganic oxide porous materials selected from silica, ceria-zirconia, lanthana, alumina, and titania, the catalytically active component (b) supported on the carrier B is platinum (Pt), and the catalytically active component (a) comprises Rh.

2. The exhaust gas purification catalyst composition according to claim 1, wherein the oxide porous material in the carrier B has a Hammett acidity function H0max of -10 < H0max < 15.

3. The exhaust gas purification catalyst composition according to claim 1 or 2, wherein the catalytically active component (a) supported on the carrier A is Rh.

4. An exhaust gas purification catalyst having a structure in which the exhaust gas purification catalyst composition according to any one of claims 1 to 3 is supported on a substrate.

5. An exhaust gas purification catalyst having a structure in which the exhaust gas purification catalyst composition according to any one of claims 1 to 3 is formed into a pellet shape.