Patent Application
20080269046
This application claims priority under 35 USC 119 to Japanese Patent Applications No. 2007-118105 filed on Apr. 27, 2007, and No. 2008-048163 file on Feb. 28, 2008, the entire contents of which are incorporated herein by reference.
(a) Field of the Invention
This invention relates to exhaust gas purification catalysts for converting exhaust gas from engines and methods for manufacturing such an exhaust gas purification catalyst.
(b) Description of Related Art
Exhaust gas purification catalysts for converting exhaust gas from engines employ an oxygen storage component having oxygen storage/release capacity, such as ceria or a cerium-zirconium mixed oxide (composite oxide). When such an oxygen storage component is used for a three-way catalyst, it acts to expand the air-fuel ratio window (A/F window) of the catalyst, whereby hydrocarbons (HC), carbon monoxide (CO) and nitrogen oxides (NOx) can be converted even if the A/F ratio of exhaust gas deviates from the stoichiometric A/F ratio. Meanwhile, when such an oxygen storage component is used for an oxidation catalyst for a lean-burn diesel engine, it releases stored oxygen as active oxygen to enhance the catalyst performance.
Cerium-zirconium mixed oxides (Ce—Zr mixed oxides) are known to have higher thermal resistance than ceria but lower thermal resistance than alumina that is another material for an exhaust gas purification catalyst. “Having low thermal resistance” means that when the material is exposed to gas having a high temperature, for example, about 1000° C. for a long time, its crystal structure changes, its specific surface area reduces or its particles agglomerate.
A solution to this problem is disclosed in Published Japanese Patent Applications Nos. 2000-271480 and 2005-224792. This solution is to add one or more rare earth metals other than Ce to a Ce—Zr mixed oxide, make a composite of alumina substantially indissoluble in ceria and the Ce—Zr-based mixed oxide and then post-carry one or more catalytic metals on the composite.
Alternatively, Published Japanese Patent Application No. H10-182155 discloses another solution in which an alkaline solution is added to a solution containing salts of a catalytic metal, aluminium (Al), Ce and Zr to coprecipitate these metal components and the obtained coprecipitate is dried and calcined to produce a mixed oxide containing the catalytic metal.
Meanwhile, Published Japanese Patent Application No. 2000-300989 discloses a technique that aqueous ammonia is added to a solution containing salts of Ce, Zr and palladium (Pd) to coprecipitate these metal components and the obtained coprecipitate is dried and calcined to produce a catalytically active substance, and additionally that powder of the catalytically active substance and alumina are loaded into deionized water and wet ground into a slurry and the obtained slurry is coated on a honeycomb support to form an exhaust gas purification catalyst.
In the catalysts disclosed in Published Japanese Patent Applications Nos. 2000-271480 and 2005-224792, since a catalytic metal is post-carried on the surface of the composite containing alumina, ceria and zirconia, a problem arises that the catalytic metal is sintered when exposed to high-temperature exhaust gas. In contrast, since in the catalyst disclosed in Published Japanese Patent Application No. H10-182155 a catalytic metal is coprecipitated with Al, Ce and Zr, the catalytic metal is chemically compounded into the obtained mixed oxide, which makes the catalytic metal hard to sinter.
However, the Inventor's closer inspection on the mixed oxide disclosed in Published Japanese Patent Application No. H10-182155 has revealed that if Pd disclosed in Published Japanese Patent Application No. 2000-300989 is employed as a catalytic metal for the mixed oxide, Pd exists on the surface of a Ce—Zr-based mixed oxide but not on the alumina surface (i.e., Pd fully dissolves in alumina and is not exposed at the alumina surface).
Therefore, Pd contained in alumina cannot effectively act as a catalyst. Hence, part of Pd is wasted and alumina simply acts to restrain agglomeration of Ce—Zr mixed oxide particles and cannot be effectively used as a support material for carrying Pd thereon.
An object of the present invention is that an exhaust gas purification catalyst containing an oxygen storage component containing Ce and Zr, alumina and a catalytic metal Pd enhances the thermal resistance of the oxygen storage component by the action of alumina, effectively uses the alumina as a support material for Pd and effectively uses Pd for exhaust gas conversion, particularly for oxidation of HC and CO.
A solution taken in the present invention to attain the above object is to employ a metal oxide composite in which alumina and an oxygen storage component are made into a composite, chemically compound part of Pd as a catalytic metal into the oxygen storage component to expose it at the surface of the oxygen storage component and post-carry the rest of Pd on the surfaces of alumina and the oxygen storage component.
Specifically, an aspect of the invention is directed to an exhaust gas purification catalyst including a catalyst layer that is formed on a support and contains an oxygen storage component containing Ce and Zr, alumina and a catalytic metal. In the exhaust gas purification catalyst, a plurality of primary particles of the oxygen storage component and a plurality of primary particles of the alumina agglomerate to form each of metal oxide composite particles, and the catalytic metal includes Pd doped in the oxygen storage component particles to constitute each of the oxygen storage component particles with Ce and Zr and exposed at the surfaces of the oxygen storage component particles and Pd adhered to the surfaces of the oxygen storage component particles and the surfaces of the alumina particles.
Pd is conventionally known to be useful as an oxidation catalyst and, particularly, oxidized Pd exhibits high oxidative catalytic function. However, when the air-fuel ratio of exhaust gas becomes fuel-rich, the oxygen concentration required for oxidation of HC and CO decreases and oxidized Pd is reduced to Pd metal, whereby the oxidative catalytic function of Pd tends to deteriorate.
One of significant points of the present invention is that even when the air-fuel ratio becomes fuel-rich, oxygen released from the oxygen storage component allows Pd to easily keep its oxidized form exhibiting high oxidative catalytic function. As a result, the HC and CO conversion performance at rich air-fuel ratios enhances. In other words, for three-way catalysts, their A/F window can be expanded to the fuel-rich side.
Another significant point is that since the oxygen storage component is doped with Pd, it enhances the oxygen storage/release capacity.
However, when Pd is doped in the oxygen storage component, the amount of Pd exposed at the surfaces of the oxygen storage component particles is small. Particularly when a mixture of coprecipitated Ce—Zr—Pd hydroxide and aluminium hydroxide is calcined to form metal oxide composite particles each composed of an agglomerate of oxygen storage component primary particles and alumina primary particles, Pd dissolves in alumina and, therefore, the amount of Pd exposed at the surfaces of the oxygen storage component particles is small. In such a case, Pd cannot be effectively used for exhaust gas conversion, particularly for oxidation of HC and CO.
In this respect, what is important in the invention is that not all of Pd is doped in the oxygen storage component particles but part of Pd is doped therein and the rest is adhered to the surfaces of the oxygen storage component particles and alumina particles. Thus, alumina can be effectively used as a support material for Pd, and Pd carried on the oxygen storage component and Pd carried on alumina can effectively enhance the exhaust gas conversion performance.
Furthermore, in each metal oxide composite particle, alumina particles serve as steric hindrances to restrain sintering of oxygen storage component particles. Furthermore, since Pd particles exposed at the surface of each oxygen storage component particle are integrated with the oxygen storage component particle by doping thereinto, sintering of the Pd particles can also be restrained.
The oxygen storage component particles containing Ce and Zr may be doped with one or more trivalent rare earth metals other than Ce, such as lanthanum (La), yttrium (Y) or neodymium (Nd), in addition to Pd. In such a case, the amount of doped rare earth metal is sufficient if it is 0.6% to 4.0% by mole, both inclusive, with respect to the total amount of the metal oxide composite particles excluding Pd.
The Pd doping ratio of the amount of Pd doped in the oxygen storage component particles to the sum of the amount of Pd doped in the oxygen storage component particles and the amount of Pd adhered to the surfaces of the oxygen storage component particles and the surfaces of the alumina particles is preferably 1% to 60% by mass, both inclusive.
Specifically, not all of Pd doped in each oxygen storage component particle is exposed at the surface of the particle but only part of Pd doped therein is exposed at the surface thereof. Therefore, in order to provide Pd exposed at the surfaces of the oxygen storage component particles to effectively act as a catalytic metal, the above Pd doping ratio is preferably not less than 1% by mass. Furthermore, there is a limit to enhancing the oxygen storage/release capacity of the oxygen storage component by increasing the amount of doped Pd and excessively doped Pd is wasted. In addition, as the Pd doping ratio increases, the amount of Pd carried on the surfaces of the oxygen storage component particles and alumina particles accordingly becomes smaller. Therefore, in order to effectively enhance the exhaust gas conversion performance by the action of Pd carried on the oxygen storage component and Pd carried on the alumina, the above Pd doping ratio is preferably not more than 60% by mass. More preferably, the upper limit of the Pd doping ratio is 50% by mass. Still more preferably, the Pd doping ratio is 5% to 40% by mass, both inclusive.
The metal oxide composite particles preferably have a (Ce+Zr)/Al molar ratio of 0.08 to 0.97 both inclusive.
If, like this, the proportion of alumina in the metal oxide composite particles is large, alumina particles can be effectively used as steric hindrances, which is advantageous in restraining sintering of oxygen storage component particles.
In a preferred embodiment, the exhaust gas purification catalyst further includes, in addition to the catalyst layer containing the metal oxide composite particles, a catalyst layer containing Rh and formed over the support and the catalyst layer containing the metal oxide composite particles is disposed in a lower layer closer to the surface of the support than the catalyst layer containing Rh.
Rh effectively acts to reduce NOx in exhaust gas but is likely to be alloyed by reaction with Pd and thereby deteriorates the catalytic activity. Furthermore, Rh, unlike Pd, exhibits high NOx reductive conversion performance when in metallic form (when reduced) than when oxidized. However, when Pd advantageous in oxidized form and Rh advantageous in metallic form are close to each other, both the catalytic metals interact with each other to make their electronic states unstable and thereby deteriorate the catalytic activity.
To cope with this, since in this preferred embodiment Pd and Rh are contained in different catalyst layers, this prevents deterioration of catalytic activity due to interaction between both the catalytic metals and makes it easy for both the catalytic metals to keep their advantageous electronic states. Furthermore, Pd easily deteriorates and is likely to be poisoned with sulfur and phosphorus. However, since in this preferred embodiment Pd is contained in the lower catalyst layer, the upper catalyst layer containing Rh protects Pd to reduce heat deterioration and poisoning of Pd.
The catalyst layer containing Rh preferably further contains Pt. Pt, like Rh, exhibits an excellent catalytic activity when in metallic form. Therefore, Pt is contained in the catalyst layer different from the catalyst layer containing Pd, i.e., in the catalyst layer containing Rh. In this case, since both of Pt and Rh exhibit excellent catalytic activity when in metallic form, they are less likely to cause an unfavorable interaction.
A preferable method for manufacturing the exhaust gas purification catalyst containing the Pd-carried oxygen storage component particles includes the steps of: calcining a mixture of coprecipitated Ce—Zr—Pd hydroxide and aluminium hydroxide to prepare metal oxide composite particles each composed of an agglomerate of a plurality of primary particles of the oxygen storage component containing Ce, Zr and Pd and a plurality of primary particles of alumina so that at least part of Pd is exposed at the surfaces of the primary particles of the oxygen storage component; and bringing the metal oxide composite particles into contact with a solution of Pd to adhere Pd to the surfaces of the oxygen storage component particles and the surfaces of the alumina particles.
Thus, a catalyst material can be obtained in which a plurality of primary particles of the oxygen storage component and a plurality of primary particles of alumina agglomerate to form each of metal oxide composite particles, part of Pd is doped in the oxygen storage component particles to constitute each of the oxygen storage component particles with Ce and Zr, the rest of Pd is adhered to the surfaces of the oxygen storage component particles and the alumina particles and part of the doped Pd is exposed at the surfaces of the oxygen storage component particles.
The coprecipitated Ce—Zr—Pd hydroxide can be obtained by adding a basic solution to a mixed solution of Ce, Zr and Pd salts while stirring the mixed solution. If aqueous ammonia is used as the basic solution, it is difficult to produce a palladium hydroxide. Therefore, preferred examples of the basic solution include NaOH, KOH, Na2CO3 and K2CO3.
The coprecipitated Ce—Zr—Pd hydroxide and the aluminium hydroxide may be separately prepared and then mixed. However, if aqueous ammonia is first added to a solution of an Al salt to obtain a precipitate of aluminium hydroxide and, then, a basic solution, such as NaOH or KOH, and a mixed solution of Ce, Zr and Pd salts are concurrently added to the solution including the precipitated aluminium hydroxide to produce a coprecipitated hydroxide as a precursor of the oxygen storage component, this provides a mixture in which the coprecipitated hydroxide and the aluminium hydroxide are well mixed.
Alternatively, also by adding a basic solution, such as NaOH or KOH, to the solution including the precipitated aluminium hydroxide and then adding a mixed solution of Ce, Zr and Pd salts to produce a coprecipitated hydroxide as a precursor of the oxygen storage component, a mixture in which the coprecipitated hydroxide and the aluminium hydroxide are well mixed can be obtained.
When NaOH aqueous solution is added to a solution of an Al salt to obtain a precipitate of aluminium hydroxide, a mixed solution of Ce, Zr and Pd salts may be first added to the solution including the precipitated aluminium hydroxide and then a basic solution, such as NaOH or KOH, added. Alternatively, a mixed solution of Ce, Zr and Pd salts and a basic solution, such as NaOH or KOH, may be concurrently added to the solution the precipitated aluminium hydroxide.
The adhesion of Pd to the surfaces of the oxygen storage component particles and the alumina particles may be implemented by evaporation to dryness or by impregnating metal oxide composite powder with Pd solution and then drying and calcining it.
In doping one or more trivalent rare earth metals other than Ce into the oxygen storage component, a mixed solution of salts of Ce, Zr, Pd and the trivalent rare earth metals other than Ce can be prepared.
Hereinafter, preferred embodiments of the invention will be described with reference to the drawings. Note that the following description of the preferred embodiments is merely illustrative in nature and is not intended to limit the scope, applications and use of the invention.
NaOH aqueous solution is added as a basic solution to the solution including the produced precipitate and respective aqueous solutions of a Ce salt, a Zr salt and a Pd salt are then added to and mixed with the above solution. If needed, one or more kinds of solutions of other trivalent rare earth metal salts, such as La, Y and Nd, are added to and mixed with the above solution. Thus, hydroxides of Ce, Zr and Pd (and, if needed, one or more of other trivalent rare earth metals, such as La, Y and Nd) are coprecipitated, thereby obtaining a mixture of the coprecipitate and aluminium hydroxide. In producing the coprecipitate, the mixed solution is preferably set at a temperature ranging from room temperature to about 80° C. and the pH of the solution after addition of the basic solution is preferably set at 9 to 12.
The obtained precipitate mixture is rinsed in water several times and then dried and calcined. The drying is preferably carried out at a temperature from about 150° C. to about 250° C. for a few to a dozen hours and the calcination is preferably carried out at a temperature from about 450° C. to about 600° C. for a few to a dozen hours. The product thus obtained is powder of a metal oxide composite composed of agglomerates of primary particles of an oxygen storage component containing Ce and Zr, doped with Pd and having at least part of the doped Pd exposed at the particle surfaces and primary particles of alumina.
Next, an aqueous solution of a Pd salt is added to the metal oxide composite powder and then evaporated to dryness (whereby Pd is post-carried on the metal oxide composite). Thus, Pd is adhered to the surfaces of the oxygen storage component particles and the surfaces of the alumina particles. Then, the dried residue is ground into catalyst powder (as an exhaust gas purification catalyst material).
Thereafter, the catalyst powder is wash-coated on a honeycomb support. Specifically, a slurry is prepared by blending the catalyst powder with a binder and water. If needed, during the blending, alumina or any other oxide powder and/or any other catalyst powder are added to the slurry. Then, a honeycomb support is immersed into the slurry and picked up therefrom, excess slurry adhering to the support surface is removed, and the support is dried and calcined, thereby obtaining an exhaust gas purification catalyst (honeycomb catalyst) in which a catalyst layer is formed on the honeycomb support. The drying is preferably carried out at a temperature from about 150° C. to about 200° C. for a few hours and the calcination is preferably carried out at a temperature from about 450° C. to about 600° C. for a few hours.
In forming a plurality of catalyst layers in stratified form on the honeycomb support, a plurality of kinds of catalytic powders are wash-coated in appropriate order on the honeycomb support.
This embodiment relates to an exhaust gas purification catalyst prepared using only the catalyst material shown in
A honeycomb catalyst according to an example of this embodiment was prepared by the exhaust gas purification catalyst manufacturing method shown in
The calcination of the slurry applied to the honeycomb support was carried out at 500° C. for two hours. The amount of metal oxide composite powder carried per L of the honeycomb support was 80 g. Therefore, the total amount of Pd carried on the support, including the amount of doped Pd and the amount of post-carried Pd, was 0.4 g/L. Used as a binder was a Zr binder. The amount of binder used was 8.9 g/L.
Respective aqueous solutions of source salts of the above six kinds were mixed with each other and NaOH solution was added to the mixed solution to coprecipitate all metal hydroxides. The water rinsing, drying and calcination of the coprecipitate were carried out under the same conditions as in preparation of the metal oxide composite particles of the above Inventive Example. The obtained mixed oxide particles were carried on a honeycomb support under the same conditions as in Inventive Example. The composition of the obtained mixed oxide particle was a CeO2/ZrO2/La2O3/Y2O3/Al2O3 mass ratio of 11.0:8.0:1.0:0.4:79.6 (% by mass), and the amount of doped Pd in the mixed oxide particle was 0.5% by mass. The amount of Pd post-carried on the mixed oxide by evaporation to dryness was zero. The amount of mixed oxide powder carried per L of the honeycomb support was 80 g, the total amount of Pd carried on the support was 0.4 g/L and the amount of binder was 8.9 g/L.
The honeycomb catalysts of the above Inventive Example and Comparative Example were heat-aged in an air atmosphere at 1000° C. for 24 hours, then set in a model exhaust gas flow reactor, then preconditioned and then measured in terms of light-off temperature T50 (° C.). The preconditioning was carried out by increasing the temperature of a model exhaust gas having an A/F ratio of 14.7 (see Table 1) at a rate of 30° C. per minute from a room temperature while allowing the model exhaust gas to flow through the catalyst at a space velocity of 120000/h and then keeping the model exhaust gas at 600° C. for 20 minutes.
The model exhaust gas for light-off performance evaluation had an A/F ratio of 14.7±0.9. Specifically, a mainstream gas was allowed to flow constantly at an A/F ratio of 14.7 and a specified amount of gas for changing the A/F ratio was added in pulses at a rate of 1 Hz, so that the A/F ratio was forcedly oscillated within the range of ±0.9. The respective gas compositions at A/F ratios of 14.7, 13.8 and 15.6 are shown in Table 1. The space velocity SV was set at 60000/h and the rate of temperature increase was set at 30° C./min.
T50 (° C.) is the gas temperature at the catalyst entrance when the concentration of each exhaust gas component (HC, CO and NOx) detected downstream of the catalyst reaches half of that of the corresponding exhaust gas component flowing into the catalyst (when the conversion efficiency reaches 50%) after the temperature of the model exhaust gas is increased, and indicates the low-temperature catalytic conversion performance of the catalyst. The measurement results are shown in Table 2.
The catalyst of Inventive Example was a dozen degrees Celsius lower in light-off temperatures T50 for all of HC, CO and NOx than the catalyst of Comparative Example. Now, the reasons for this are considered with reference to
Therefore, it can be said that one of reasons why the light-off performance of the catalyst of Comparative Example was lower than that of the catalyst of Inventive Example is that substantially no Pd existed on alumina surface, that is, the dispersibility of Pd was low, or the amount of Pd effectively acting as a catalytic metal was small, or alumina did not effectively act as a support material for the catalytic metal. In yet other words, it can be said that in the catalyst of Inventive Example alumina was effectively used as a support material for Pd to highly disperse Pd on alumina surface and thereby enhance the light-off performance.
—Ratio of Pd Doping into Oxygen Storage Component Particle—
According to the manufacturing method shown in
Furthermore, it can be seen from
Sample 5 having a ratio of Pd doping of 100% by mass exhibited substantially the same light-off performance as Comparative Example in Table 2. Therefore, although in this experiment no difference was exhibited in light-off performance between the case where Al hydroxide was coprecipitated with the other metal hydroxides, such as Ce and Zr, and the case where Al hydroxide was precipitated earlier than the other metal hydroxides, it is believed from the results of
Since in
Table 4 shows that both of Sample 2 having a small Al content and Sample 8 having a large Al content exhibited good light-off performance. The (Ce+Zr)/Al molar ratio in Sample 2 was 8/100 and the (Ce+Zr)/Al molar ratio in Sample 8 was 97/100. Therefore, it can be seen that metal oxide composite particles having a (Ce+Zr)/Al molar ratio of 0.08 to 0.97 both inclusive exhibits a good light-off performance. The amount of rare earth metal (the total amount of La and Y) is sufficient if it is 0.6% to 4.0% by mole, both inclusive, with respect to the total amount of metal oxide composite particles excluding Pd.
This embodiment relates to an exhaust gas purification catalyst prepared using a combination of the catalyst material shown in
A catalytic coating (monolayer) in which the following Materials A to E and a binder were mixed together was formed on a honeycomb support:
Here, the unit “g/L” indicates the amount of component carried per L of the honeycomb support. The composition of the “composite catalyst material” excluding Pd was a CeO2/ZrO2/La2O3/Y2O3/Al2O3 mass ratio of 11.0:8.0:1.0:0.4:79.6 (% by mass). “Alumina” is La-alumina containing 4% by mass of La2O3. The composition of the “Zr—Ce—Nd mixed oxide” was a ZrO2/CeO2/Nd2O3 mass ratio of 80:10:10 (% by mass). The number in parentheses of “Material A(10)” indicates the ratio of Pd doping. An evaporation-to-dryness method was used to carry catalytic metals on metal oxides for Materials B, D and E. These points apply also to the following other Inventive Examples and Comparative Examples.
A catalytic coating of bilayer structure including the following lower layer (containing Pd as a catalytic metal) and upper layer (containing Rh as a catalytic metal) was formed on a honeycomb support:
“lumina with no catalytic metal carried thereon”, serving as Material F, is La—alumina containing 4% by mass of La2O3 (the same applies below).
A catalytic coating of bilayer structure including the following lower layer (containing Rh as a catalytic metal) and upper layer (containing Pd as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of bilayer structure including the following lower layer (containing Pd as a catalytic metal) and upper layer (containing Rh and Pt as catalytic metals) was formed on a honeycomb support:
A catalytic coating of bilayer structure including the following lower layer (containing Pd and Pt as catalytic metals) and upper layer (containing Rh and Pt as catalytic metals) was formed on a honeycomb support:
An evaporation-to-dryness method was used to carry Pt on cerium oxide for Material G.
A catalytic coating of bilayer structure including the following lower layer (containing Pd as a catalytic metal) and upper layer (containing Rh and Pd as catalytic metals) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pd as a catalytic metal), middle layer (containing Pt as a catalytic metal) and upper layer (containing Rh as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pt as a catalytic metal), middle layer (containing Pd as a catalytic metal) and upper layer (containing Rh as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pd as a catalytic metal), middle layer (containing Rh as a catalytic metal) and upper layer (containing Pd as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pd as a catalytic metal), middle layer (containing Rh and Pt as catalytic metals) and upper layer (containing Pd as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pd and Pt as catalytic metals), middle layer (containing Rh as a catalytic metal) and upper layer (containing Pd as a catalytic metal) was formed on a honeycomb support:
A catalytic coating of three-layer structure including the following lower layer (containing Pd as a catalytic metal), middle layer (containing Rh as a catalytic metal) and upper layer (containing Pd and Pt as catalytic metals) was formed on a honeycomb support:
Comparative Examples 1 to 12 used Material A(O) having a ratio of Pd doping of 0% (i.e., Material A in which all of Pd was post-carried), instead of their respective corresponding Materials A in Inventive Examples 1 to 12.
The catalysts of Inventive Examples 1 to 12 and Comparative Examples 1 to 12 were aged. Specifically, each catalyst was joined to the exhaust pipe of a 2 L gasoline engine and then aged by repeating the following cycle for 50 hours at a temperature of 900° C. at the entrance of the catalyst: flowing of exhaust gas with a stoichiometric air-fuel ratio for 60 seconds; flowing of exhaust gas with a lean air-fuel ratio for 10 seconds; and flowing of exhaust gas with a rich air-fuel ratio for 30 seconds. The volume of honeycomb support of each catalyst was 1 L.
Sample catalysts in a columnar shape having a diameter of 25 mm and a height of 50 mm were cut out of their respective aged catalysts and then measured in terms of light-off temperature T50 (° C.) with a model exhaust gas flow reactor. Like the previously described Evaluation of Light-Off Performance, the A/F ratio of the model exhaust gas was 14.7±0.9, the space velocity SV was set at 60000/h and the rate of temperature increase was set at 30° C./min. The measurement results are shown in Tables 5 and 6 and
The measurement results show that the catalysts of Inventive Examples 1 to 12 exhibited lower light-off temperatures than those of corresponding Comparative Examples 1 to 12.
The catalyst of Inventive Example 2 has a structure in which Pd-based catalyst materials (Materials A and B) are in the lower layer and an Rh-based catalyst material is in the upper layer, and exhibited a lower light-off temperature than Inventive Example 3 having an inverted structure. The reason for this is believed to be due to an effect of the upper layer (the Rh-based catalyst material) restraining heat deterioration of Pd-based catalyst materials due to aging.
The catalyst of Inventive Example 9 has a three-layer structure in which one of the Pd-based catalyst materials in Inventive Example 2 (Material A) is located over an Rh-based catalyst layer (Materials D and F), and exhibited a higher light-off temperature than Inventive Example 2. Part of the reason for this is believed to be due to heat deterioration of the Pd-based catalyst material (Material A) in the upper layer.
Although both of Inventive Examples 7 and 8 have a three-layer structure, they are different from each other in that the former contains Pd-based catalyst materials (Materials A and B) in the lower layer but the latter in the middle layer. Comparison between both of Inventive Examples 7 and 8 shows that the former exhibited a lower light-off temperature than the latter. Part of the reason for this is believed to be that the Pd-based catalyst materials in Inventive Example 7 were less likely to be deteriorated by heat than those in Inventive Example 8.
Although both of Inventive Examples 9 and 10 have a three-layer structure, the latter is different from the former in that the middle layer containing an Rh-based catalyst material (Material D) further contains a Pt-based catalyst material (Material E). Comparison between both of Inventive Examples 9 and 10 shows that the latter exhibited a lower light-off temperature than the former. This is believed to be due to an effect of the Pt-based catalyst material and to mean that even if a mixture of Pt-based catalyst material and Rh-based catalyst material is contained in the same layer, there arises no unfavorable interaction between them.
Although both of Inventive Examples 10 and 12 have a three-layer structure, they are different from each other in that the former contains a Pt-based catalyst material (Material E) in the middle layer containing an Rh-based catalyst material (Material D) but the latter contains it in the upper layer containing a Pd-based catalyst material (Material A). Comparison between both of Inventive Examples 10 and 12 shows that the latter exhibited a higher light-off temperature than the former. The reason for this is believed to be that the Pt-based catalyst material (Material E) had no mutual adverse effect on the Rh-based catalyst material (Material D) but had a mutual adverse effect on the Pd-based catalyst material (Material A).
| Number | Date | Country | Kind |
|---|---|---|---|
| 2007-118105 | Apr 2007 | JP | national |
| 2008-048163 | Feb 2008 | JP | national |
