Exhaust gas purifying catalyst

Abstract: An exhaust gas purifying catalyst is characterized in that at least one kind of catalyst metal is loaded on a layered porous silica or a layered porous silica-metal oxide. The exhaust gas purifying catalyst is used as an oxidation catalyst for purifying hydrocarbon and carbon monoxide, or a reduction catalyst for purifying nitrogen oxides (NO x ), which is suitable for purifying exhaust gases in automobiles. An exhaust gas purifying apparatus includes the above exhaust gas purifying catalyst and an absorbent for trapping hydrocarbon components, in which aromatic HC such as trimethylbenzene and the like are effectively trapped.

Description: Field of the Invention The present invention relates to an exhaust gas purifying catalyst for purifying hydrocarbon, carbon monoxide or nitrogen oxides (NO x ) contained in exhaust gases exhausted from an internal combustion engines of automobiles and the like. Description of the Related Art Conventionally, inorganic porous body such as alumina or zeolite is mainly used as a support of an exhaust gas purifying catalyst for automobiles. Japanese Laid-Open Patent Publication No. 201648/1987 (Patent Abstracts of Japan 62 C 477) discloses various kinds of supports such as alumina, silica, titania and alumina-silica. Japanese Laid-Open Patent Publication No. 147153/1980 (Patent Abstracts of Japan 71 C 42) discloses A-type zeolite, X-type zeolite and mordenite-system zeolite. Japanese Laid-Open Patent Publication No. 4220/1989 (Patent Abstracts of Japan 24 C 589) discloses crystalline zeolite. Japanese Laid-Open Patent Publication No. 63552/1990 (Patent Abstracts of Japan 109 C 721) discloses composite oxides comprising titanium, nitrogen and zirconia. Japanese Laid-Open Patent Publication No. 245850/1989 (Patent Abstracts of Japan 124 C 669) discloses an aggregate comprising ceramic fibers. The above inorganic porous bodies have wide specific surface, acidity and heat resistance at high temperature, so they are suitable for catalytic supports. These supports are used as conventional exhaust gas purifying catalysts in such a manner that a noble metal such as platinum or rhodium is loaded on these supports. So-called cold HC is the problem, for it is included in the exhaust gas at low temperature immediately after the engine is ignited and it is hard to be purified by catalysts. To solve this problem, there is proposed an exhaust gas purifying apparatus such as cold HC purifying system and the like which use adsorbent such as zeolite for temporarily trapping cold HC (Japanese Patent Laid-Open No. 2-75327/1990 (US-A-4 985 210) and Japanese Patent Application No. 3-49658/1991 (Patent Abstracts of Japan 44 C 832)). However, the above-described conventional exhaust gas purifying catalysts have poor catalytic activity. So, they are required to improve catalytic activity in order to purify exhaust gases in diesel engines. In the case of the above-mentioned exhaust gas purifying apparatus, hydrocarbon components, which are trapped by zeolite as the adsorbent, are limited to have relatively small molecules. In this apparatus, it is difficult to efficiently trap bulky aromatic HC such as trimethylbenzene which causes troubles in some countries as the material having the high capacity of forming ozone. This may be related to the small pore diameters for trapping in zeolite. Zeolite has the low heat resistance, so it is hard to directly be provided in the exhaust gas system of an internal combustion engines. Therefore, zeolite should be provided in the system with a bypass or the like. As mentioned above, in the conventional evaporated fuel absorbing apparatus and the hydrocarbon trapping apparatus of the exhaust gas purifying apparatus, there are various problems caused by the insufficient specific surfaces of adsorbents for trapping hydrocarbon components, small pore diameters for trapping and the low heat resistance. DE-A-3 928 760 discloses an exhaust gas purifying apparatus comprising an adsorbent and a catalyst, said adsorbent being a zeolite provided on the upstream side of the catalyst. USP No. 4,774,213 discloses a catalyst for decreasing the content of nitrogen oxide in flue gases. The catalyst comprises an active constituent in form of a combination of a compound of iron and of an acid alumino silicate that has a layered structure, said iron being inserted e.g. by impregnation. EP-A-0 472 144 is directed to a method for producing synthetic Magadiite, which might be used as catalyst component, adsorbent or catalytical active agents. EP-A-0 284 278 discloses a hydrocracking catalyst which is a layered silicate containing interspathic polymeric silica and interspathic polymeric oxides of one or more metals, said catalyst optionally comprises a catalytic element such as Pd. SUMMARY OF THE INVENTION It is an object of the present invention to provide an exhaust gas purifying catalyst having excellent catalytic activity which is used as an oxidation catalyst for purifying hydrocarbon and carbon monoxide, or a reduction catalyst for purifying nitrogen oxides (NO x ), and which is suitable for purifying exhaust gases in automobiles. It is another object of the present invention to provide a hydrocarbon trapping apparatus, an evaporated fuel adsorbing apparatus and an exhaust gas purifying apparatus without the above-mentioned problems. Extensive researches have been made for achieving the above objects, and they have invented the following exhaust gas purifying catalyst in which a layered porous silica or a layered porous silica-metal oxide is used as a support as specified in claim 1. The exhaust gas purifying catalyst according to the present invention comprises at least one kind of catalyst metal which is loaded on a layered porous silica or a layered porous silica-metal oxide as specified in claim 1. As shown in the chemical formula 1, the layered porous silica or the layered porous silica-metal oxide has the structure that the skeleton comprises SiO 2 or SiO 2 metal composite oxide. As shown in Figure 2, the layered porous silica or the layered porous silica-metal oxide has the basic structure that a plural of planar sheets 10 are piled up each other. As shown in Figure 1, each of these sheets 10 are curved, and one sheet 10 is partially connected to the other sheet 10 to form a three-dimensional skeleton. Among these layers, there are plural of pores 2 whose diameter is in the range of 1 to 6 nm (10 to 60 angstroms). M is metal element except Si. The layered porous silica is used in the forms of spherical particles, prismatic particles or the like. Considering to secure the gas permeability of its filling part and the contacting area of gas, the dimensions of particles are preferably as follows: the diameter of spherical particle falls in the range of 0.1 to 10mm; the diameter of prismatic particle falls in the range of 0.1 to 5mm and the length of prismatic particle falls in the range of 1 to 30mm. The layered porous silica may also be used by being loaded on a support comprising appropriate material and having a certain configuration (such as an opening three dimensions ped). The specific surface (surface area) of the above layered porous silica is in the range of 1000 to 1500m 2 /g. As shown in Figure 1, the exhaust gas purifying catalyst according to the present invention has the structure that a fine particle of catalyst metal 3 is loaded on the inner portion of the pore 2 of a layered porous silica 1 or a layered porous silica-metal oxide 1. The loaded amount of the catalyst metal is desirably not less than 0.03% by weight against the layered porous silica. When the loaded amount of the catalyst metal is less than 0.03% by weight, no catalytic action occurs. The catalyst metals include noble metals, transition metals and rare earth metals. Among these, noble metals are preferable. Especially, platinum is the most preferable. Since the layered porous silica and platinum or the layered porous silica-metal oxide and platinum show high affinity, platinum is widely dispersed and loaded. Furthermore, sintering of platinum particles at high temperature is prevented. The layered porous silica is manufactured by the following manner. At first, crystalline layered silicate such as kanemite is heated and agitated in alkyl trimethyl ammonium aqueous solution to generate a layered crystal. Then, an organic substance is introduced into the layers of the layered crystal by means of ion exchange reaction to form an interlayered bridge of SiO 2 . This is referred to as an interlayered extension process. After that, the above layered crystal is filtered, dried and calcined at the temperature of 700°C to obtain the layered porous silica. The layered porous silica-metal oxide is manufactured by the following manner. At first, crystalline layered silicate is heated and agitated in alkyl trimethyl ammonium aqueous solution. Then, it is filtered and contacted with metallic salt other than silicon. This is referred to as a metal addition process. After that, it is calcined at high temperature to obtain the layered porous silica-metal oxide. Crystalline layered silicate for forming a layered porous silica is represented by crystalline layered sodium silicate containing sodium ion between silicon tetrahedral layers. Crystalline layered sodium silicate include kanemite (NaHSi 2 O 5 · 3H 2 O), sodium subsilicate (Na 2 Si 2 O 5 ), macatite (Na 2 Si 4 O 5 ·5H 2 O), airaite (Na 2 Si 8 O 17 ·xH 2 O), magadiite (Na 2 Si 14 O 23 ·xH 2 O), kenyaite (Na 2 Si 20 O 41 ·xH 2 O) and so on. However, crystalline layered sodium silicate is not limited to the above substance. Since the above crystalline layered silicate contains no structural water, it is different from clay mineral. Hydroxyl group of silanols is used for forming interlayered bridge formation of SiO 2 by means of condensation in the interlayered extension process. So, the pore structure of the crystalline layered silicate is not deteriorated at high temperature. Concerning kanemite which is one kind of crystalline layered silicate, layered crystal comprises single silicon tetrahedral layer, so the surface area per unit weight is wide, and the monolayer structure cannot be deteriorated under the calcination treatment at high temeprature. When the layered porous silica or the layered porous silica-metal oxide is formed by using kanemite, the specific area becomes wide, and catalytic ability improves. When kanemite is used for forming the layered porous silica or the layered porous silica-metal oxide, the upper layer is partially connected with the lower layer while maintaining the monolayer structure, and the non-connected portion has pores comprising organic substance. Namely, the layered porous silica or the layered porous silica-metal oxide has porous structure having honey-comb shaped cross section. The above pore diameter is depended on the size of organic substance which is used in the process for forming the layered porous silica or the layered porous silica-metal oxide. However, when the pore diameter is less than 1 nm (10 angstroms) which is the same size of zeolite, it has no effect on the forming. When the pore diameter is more than 10 nm (100 angstroms), the corresponding organic substance is a few, and validity is less. The distribution of the pore diameter can be within the uniformly narrow ranges, and it can be within the wide ranges of 1 to 4 nm (10 to 40 angstroms). Interlayered bridge formation of SiO 2 is formed in such a manner that concentration occurs between two hydroxyl groups which are connected to silicon of two silicon tetrahedral layers opposed each other in the interlayered extension process. The layered porous silica-metal oxide has acidity. The acidity is generated when metallic atom is connected to a part of silicon which constitutes the silicon tetrahedral layer by way of oxygen. Therefore, the acidity functions as Lewis acid. Furthermore, the acidity functions as Brønsted acid when water is added to the acidity to discharge proton. In both cases, the acidity exhibits catalytic activity. Metallic atoms which has the acidity include aluminum, zirconium, gallium, beryllium, magnesium, yttrium, lanthanum, tin, lead and the like. The structural analysis of the layered porous silica are shown as follows. Concerning one sample in which cetyl trimethyl ammonium chloride is used as an organic substance, the peak corresponding to 3,8 nm (38 angstrom) is observed by powder X-ray diffraction (See Figure 3). Since the peak corresponds to the layer distance, the layered porous silica has the layered structure having the layer space of 3,8 nm (38 angstroms). Concerning 29 Si-MAS·NMR, kanemite which is used as raw material shows the peak corresponding to Q 3 of Si (representing the condition that one of four oxygen atoms is free). On the other hand, the layered porous silica shows the peak corresponding to Q 4 of Si (representing the condition that none of four oxygen atoms is free) (See Figure 4). As shown in Figure 4, while kanemite has no layer bonding, the layered porous silica has layer bonding and three-dimensional network. When the distribution of the pore diameter of the layered porous silica is shown by the measurement of nitrogen adsorption isotherm, the distribution is within the narrow ranges around 3 nm (30 angstroms) (See Figure 5). The method for forming the layered porous silica or the layered porous silica-metal oxide is described as follows. The organic substance is introduced into silicon tetrahedral layers in the interlayered extension process, and cation of organic substance reacts with sodium ion to make ion exchange reaction. Since crystalline layered sodium silicate such as kanemite has no lubricating ability with water, it is different from clay mineral and it is hard to cause interlayered extension. However, it is possible to make interlayered extension by means of introducing organic substance for ion exchange reaction. There is no limit to kinds of cation of organic substance. But, organic onium ion, especially, alkyl ammonium ion is preferable since it is excellent in easy sample preparation and ion exchanging ability. Molecular size and molecular weight of the organic substance directly regulate the degree of interlayered extension, namely, the pore diameter of the layered porous silica or the layered porous silica-metal oxide. So, the pore diameter is freely decided by optimum selection of molecular size and molecular weight. Concerning the distribution of the pore diameter, it can be set within uniformly narrow ranges when single kind of organic substance is used. When plenty kinds of organic substances having different molecular size and different molecular weight are used together, the distribution of the pore diameter can be set within wide ranges. There is also no limit to kinds and usage of metallic salt in the metal addition process. The layered crystal of SiO 4 tetrahedra can be immersed into the metallic salt solution, and the powder of the layered crystal of SiO 4 tetrahedra can be mixed and contacted with the powder of the metallic salt. When the metallic salt solution is used, it is preferable that the layered crystal of SiO 4 tetrahedra is dried after immersing in order to improve the efficiency of the calcination process. In the calcination process, it is desirable that calcination is normally performed at the temperature of 500 to 800°C for hours. When the calcination temperature is too high, the structure of the layered porous silica is likely to be deteriorated. On the other hand, when the calcination temperature is too low, the structure of the layered porous silica is not fully fixed. There is no limit to calcination condition, so the layered porous silica can be calcined in the air. Furthermore, it also can be calcined in the atmosphere including oxygen or ozone in order to improve decomposition of organic substance. The catalyst metal such as platinum is loaded on the above layered porous silica or the above layered porous silica-metal oxide. The method for loading the catalyst metal is performed in such a manner that the layered porous silica or the layered porous silica-metal oxide is immersed into the solution of the catalyst metal compound to vaporize moisture, and to be calcined, for example, at the temperature of 350°C. An exhaust gas purifying apparatus according to the present invention is provided in an exhaust system of an internal combustion engine, and it comprises an installation portion of an exhaust gas purifying catalyst and an installation portion of adsorbent for trapping hydrocarbon components as specified in claim 2. The above-described layered porous silica or the above-described layered porous silica-metal oxide is used as the adsorbent as specified in claim 2. The above-mentioned internal combustion engine may be represented by a gasoline engine or diesel engine, but it is not limited to these engines. The exhaust gas system of internal combustion engine indicates totally from an exhaust manifold to the tip of an exhaust port of an exhaust pipe. The portion of providing exhaust gas purifying apparatus is not limited. Exhaust gas purifying catalyst should at least be the catalyst which has the activity for purifying HC in exhaust gas. So, for example, so called oxidation catalyst or three way catalyst is used as exhaust gas purifying catalyst. The kind and use of the catalyst or the kind of activated metal which is loaded by the catalyst are not limited. Activated metal may be selected from Pt (platinum), Pd (palladium), Pt-Pd, Pt-Rh (rhodium), Pd-Rh, Pt-V 2 O 5 (vanadium oxide) and the like. The arrangements of the providing portion of adsorbent in the exhaust system and the providing portion of the exhaust gas purifying catalyst reside in the following two patterns. In one pattern, the former is provided at the upstream side and in the other pattern, the latter is provided at the upstream and the downstream side of the former (refer to Figures 8 to 10). The providing portion of adsorbent can reside in the exhaust system or also can reside in the bypass provided in the exhaust system. The adsorbent is at least one of the above-mentioned layered porous silica and layered porous silica-metal oxide. Both of the above-mentioned layered porous silica may be combined to be used as the adsorbent or other kinds of adsorbents having a high heat resistance may also be used together. The use of these adsorbents is not limited but the examples include a pellet form and the form in which they are coated on support such as cordierite, metal honeycomb and the like. The specific surface of the layered porous silica or the layered porous silica-metal oxide is 2 to 7.5 times as large as the conventional catalyst support such as alumina (having the specific surface of 200 to 300m 2 /g). So, it is possible to load much amount of catalyst metal high-dispersively. Concerning catalytic reaction, the more the active spot is, the faster the reaction speed is, and the higher the activity is. Therefore, when the catalyst metal which functions as active spot is highly dispersed, the number of active spot increases and the activity becomes high. The exhaust gas purifying catalyst according to the present invention has plenty of fine pores being 1 to 6 nm (10 to 60 angstroms) on its support. Since the pore diameter is slightly larger than the particle diameter of hydrocarbon (being 0.5 to 1.5 nm (5 to 15 angstroms)), hydrocarbon having low concentration in exhaust gases can be effectively trapped to be contacted with oxygen or NO x . The conventional layered porous silica such as zeolite has small pore diameter being less than 1 nm (10 angstroms), so hydrocarbon cannot be trapped. Or even if hydrocarbon can be trapped, catalytic activity cannot be fully generated since hydrocarbon cannot be dispersed into the inner side of the pore. However, in the catalyst according to the present invention, the pore diameter is enough large for hydrocarbon to be dispersed into the inner side of the pore to be effectively reacted on the catalyst metal. In the exhaust gas purifying catalyst according to the present invention, since particles of catalyst metal loaded on the inner side of multiple of pores are encircled with pore wall, sintering is not likely to occur, and excellent heat resistance can be obtained. For a few minutes immediately after the ignition of the internal combustion engine, so called cold HC including unburned gasoline vapor is generated. On the other hand, the catalyst is in the state being not warmed up yet, so the ability for purifying exhaust gas is not sufficiently exercised. Accordingly, cold HC is hardly purified. The above-mentioned cold HC is adsorbed and stocked by the layered porous silica or the layered porous silica-metal oxide as the adsorbent, so the cold HC is not exhausted in the atmosphere. Aromatic HC such as trimethylbenzene and the like which are not effectively trapped by the conventional zeolite and the like can be smoothly trapped. After that, the condition in which the exhausting temperature rises and the ability of the catalyst for purifying HC is obtained, the HC which was adsorbed and stocked by the above-mentioned adsorbent is purged as the temperature rises and purified by the above-mentioned catalyst. The adsorbent is in superior in heat resistance so it is not necessarily provided in bypass and also can be provided at the high temperature portion (for example, the most upstream portion) of the exhaust gas system. Namely, the providing portion is selected more freely. In the exhaust gas purifying catalyst according to the present invention, the catalyst metal is high-dispersively loaded on the wide surface area of the support. Furthermore, since the exhaust gas purifying catalyst has plenty of pores having the appropriate diameter, hydrocarbon can be effectively trapped. Therefore, hydrocarbon can be reacted with oxygen or NO x at low temperature so that the exhaust gas purifying catalyst shows excellent catalytic activity. Furthermore, in the exhaust gas purifying catalyst, particles of catalyst metal which are highly dispersed are encircled with pore wall, so the catalytic activity can be maintained at high temperature without sintering, and the catalyst has excellent heat resistance. The exhaust gas purifying catalyst according to the present invention can be used as an oxidation catalyst in which hydrocarbon, soluble organic fraction (SOF) and carbon monoxide contained in exhaust gases in diesel engines can be oxidized at low temperature, a catalyst for purifying NO x in which NO x contained in exhaust gases in diesel engines can be selectively reduced by hydrocarbon having low concentration, and a catalyst for purifying NO x by which NO x can be selectively reduced by hydrocarbon having low concentration in the oxidation atmosphere in lean-burn engines in order to improve fuel consumption. In the exhaust gas purifying apparatus according to the present invention, so called cold HC are effectively purified. Especially aromatic HC such as trimethylbenzene and the like are effectively trapped. Also the adsorbent is superior in heat resistance so the deterioration owing to heat is little and the providing portion can be selected more freely. BRIEF DESCRIPTION OF THE DRAWINGS A more complete appreciation of the present invention and many of its advantages will be readily obtained as the same becomes better understood by reference to the following detailed description when considered in connection with the accompanying drawings and detailed specification, all of which forms a part of the disclosure: Figure 1 is an enlarged view for showing the main portion of the exhaust gas purifying catalyst according to the present invention. Figure 2 is a view for showing the layered porous silica which is used as the exhaust gas purifying catalyst. Figure 3 is a graph for showing the result of the powder X-ray diffraction of the layered porous silica. Figure 4 is a graph for showing the result of the measurement of 29 Si-MAS·NMR of the layered porous silica. Figure 5 is a graph for showing the measurement of the distribution of pores in the layered porous silica, zeolite (ZSM-5) and amorphous silica-alumina (JRC-SAL2). Figure 6 is a graph comparing the ratios of adsorbing each of HC components included in the engine exhaust gases in the Fifth Preferred Embodiment. Figure 7 is a layout drawing of layered porous silica in the converter in the reference example of the Sixth Preferred Embodiment. Figure 8 is a layout drawing of layered porous silica and the catalyst in the converter in the Sixth Preferred Embodiment. Figure 9 is a layout drawing of layered porous silica and the catalyst in the converter in the Sixth Preferred Embodiment. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Having generally described the present invention, a further understanding can be obtained by reference to the specific preferred embodiments which are provided herein for purposes of illustration only and are not intended to limit the scope of the appended claims. The Preferred Embodiments according to the present invention will be hereinafter described with reference to Figures 1 through 9. First Preferred Embodiment (Formation of a layered porous silica) 3870g of powder sodium silicate (SiO 2 /Na 2 O = 2.00) was calcined at the temperature of 700°C in an electric furnace for six hours to obtain 3000g of δ-Na 2 Si 2 O 5 crystal. The whole amount of the obtained crystal was immersed into 30 liters of water, and it was agitated for 3 hours. After that, the solid amount was filtered to obtain kanemite which contains 100wt% by weight of water. 3000g (dried amount) of the obtained kanemite was dispersed into 60 liters of 0.1N hexadecyl trimethyl ammonium chloride aqueous solution, and 2N HCl aqueous solution was added to prepare the solution being 8.5pH. After that, the prepared solution was agitated for 3 hours at the temperature of 70°C. Then, the solid amount was filtered, and the remaining substance was washed and filtered with 120 liters of water for five times. The obtained sample was dried, and after that, it was calcined at the temperature of 700°C for six hours under the air to obtain a layered porous silica. The specific surface of the above layered porous silica was 1100m 2 /g which is measured by the nitrogen adsorption method. The distribution of the pore diameter was also measured by the nitrogen adsorption method to show the result that the distribution of the pore diameter was within the ranges of about 3 nm (30 angstroms). (Formation of catalyst loaded with platinum) The predetermined amount of dinitro diamine platinum (Pt-P salt) was diluted with water, and the predetermined amount of the dried layered porous silica was immersed into the diluted solution. Then, the solution was heated and agitated at the temperature of 100 to 120°C on a hot stall to vaporize moisture. After that, the obtained sample was dried at the temperature of 100°C in a drier, and it was calcined at 350°C, thereby obtaining 0.08% by weight of catalyst. The obtained catalyst was molded by powder-pressed molding, and it was formed into the granule having 6 to 10 mesh by pulverized classification. Second Preferred Embodiment The Second Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 1.67% by weight of catalyst. Third Preferred Embodiment The Third Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 2.50% by weight of catalyst. Fourth Preferred Embodiment The Fourth Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 4.17% by weight of catalyst. Fifth Preferred Embodiment The Fifth Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 6.73% by weight of catalyst. Sixth Preferred Embodiment The Sixth Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 8.33% by weight of catalyst. Seventh Preferred Embodiment The Seventh Preferred Embodiment employed the same compositions as described in the First Preferred Embodiment except that tetraamine dihydro platinum was used instead of dinitro diamine platinum (Pt-P salt), thereby obtaining 1.67% by weight of catalyst. Comparative Example 1 The Comparative Example 1 employed the same compositions as described in the Second Preferred Embodiment except that γ-alumina was used instead of the dried layered porous silica, thereby obtaining 1.67% by weight of catalyst. Comparative Example 2 The Comparative Example 2 employed the same compositions as described in the Fourth Preferred Embodiment except that γ-alumina was used instead of the dried layered porous silica, thereby obtaining 4.17% by weight of catalyst. Comparative Example 3 The Comparative Example 3 employed the same compositions as described in the Sixth Preferred Embodiment except that γ-alumina was used instead of the dried layered porous silica, thereby obtaining 8.33% by weight of catalyst. Comparative Example 4 The Comparative Example 4 employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 0.02% by weight of catalyst. Comparative Example 5 The Comparative Example 5 employed the same compositions as described in the First Preferred Embodiment, thereby obtaining 0.01% by weight of catalyst. Loaded Amount (wt%) Platinum Compound Embodiments 1 0.08 dinitro diamine platinum 2 1.67 dinitro diamine platinum 3 2.50 dinitro diamine platinum 4 4.17 dinitro diamine platinum 5 6.73 dinitro diamine platinum 6 8.33 dinitro diamine platinum 7 1.67 tetraamine dihydro platinum Comparative Examples 1 1.67 dinitro diamine platinum 2 4.17 dinitro diamine platinum 3 8.33 dinitro diamine platinum 4 0.02 dinitro diamine platinum 5 0.01 dinitro diamine platinum Table 1 shows the loaded amount and the kinds of platinum. (Evaluation) 7cc of each catalyst was filled into a reaction tube made of quarts having the diameter of 32mm (inner diameter being 29mm). Then, the catalyst was heated to the predetermined temperature, and a model gas containing HC was introduced into the reaction tube. HC concentration in the gas flown out from the reaction tube was measured, and HC invert ratio was calculated by the ratio of HC concentration between outflow gas and inflow gas. After that, each of the catalyst was evaluated at the temperature in which 50% of HC can be inverted. C 6 H 14 and C 10 H 22 are used as HC, and the composition of the model gas is shown in Table 2. Composition of C 6 H 14 System Model Gas Composition of C 10 H 22 System Model Gas Kinds Concentration Kinds Concentration C 6 H 14 500ppm C 10 H 22 200ppm O 2 5% O 2 10% N 2 Balance N 2 Balance Table 3 shows the result of oxidation decomposition ability of C 6 H 14 and C 10 H 22 about each catalyst. Concerning the catalyst in the Preferred Embodiment 2, it is possible that C 6 H 14 and C 10 H 22 can be oxidized and decomposed at lower temperature than that of the catalyst in the Comparative Example 1. Concerning the catalyst in the Preferred Embodiment 4, it is possible that C 6 H 14 and C 10 H 22 can be oxidized and decomposed at lower temperature than that of the catalyst in the Comparative Example 2. Concerning the catalyst in the Preferred Embodiment 6, it is possible that C 6 H 14 and C 10 H 22 can be oxidized and decomposed at lower temperature than that of the catalyst in the Comparative Example 3. Namely, the catalyst in which platinum is loaded on the layered porous silica has higher catalytic activity as compared with the catalyst in which platinum is loaded on γ-alumina. Loaded Amount (wt%) Temperature for inverting 50% of HC (°C) C 6 H 14 C 10 H 22 Embodiments 1 0.08 238 209 2 1.67 190 168 3 2.50 182 146 4 4.17 146 127 5 6.73 133 118 6 8.33 121 112 Comparative Examples 1 1.67 208 181 2 4.17 196 176 3 8.33 190 168 4 0.02 368 359 5 0.01 more than 500 Concerning the catalysts in the Preferred Embodiments 2, 7 and the Comparative Example 1, ability for purifying NO x contained in exhaust gases in 2-liter diesel engines was examined. 10cc of each catalyst was filled with a reaction tube made of stainless steel. After that, a part of exhaust gases in diesel engines was introduced into the reaction tube. Then, the ability for purifying NO x is evaluated by measuring HC concentration and NO x concentration in outflow gas and inflow gas. Propylene as a reductant was introduced into the reaction tube, and the concentration of total HC of inflow gas was prepared to be 500 to 5000ppm (by methane conversion). The concentration of NO x contained in inflow gas is 250ppm. The space velocity is about 30000h -1 . Table 4 shows the maximum NO x purification ratio and the maximum temperature for purifying NO x when HC concentration is 500, 1000, 3000 and 5000ppm. Concerning the catalysts in the Preferred Embodiments 2 and 7 in which platinum is loaded on the layered porous silica, NO x can be purified at higher ratio and at lower temperature than that of the catalyst in the Comparative Example 1 in which platinum is loaded on γ-alumina. Catalysts HC Concentration Maximum NO x Purification Ratio Maximum Temperature for Purifying NO x Embodiment 2 500ppm 14.6% (240°C) 1000ppm 29.4% (220°C) 3000ppm 50.0% (220°C) 5000ppm 49.6% (200°C) Embodiment 7 500ppm 20.0% (220°C) 1000ppm 31.2% (220°C) 3000ppm 46.0% (240°C) 5000ppm 49.2% (220°C) Comparative Example 1 500ppm 17.1% (240°C) 1000ppm 34.0% (240°C) 3000ppm 42.6% (240°C) 5000ppm 40.5% (240°C) Concerning the catalysts in the Preferred Embodiments 2, 7 and the Comparative Example 1, the ability for purifying NO x was evaluated about the model gas which corresponds to the gas having the air fuel ratio of 18 and which is suitable for exhaust gas in lean-burn engines. Each catalyst is formed into the granule having 0.3 to 0.7mm, and it is filled with a reaction vessel made of quarts. Then, the ability for purifying NO x is evaluated by measuring the concentration of outflow gas and inflow gas. The space velocity is about 33000h -1 . Table 5 shows NO x purification ratio at the early stage of each catalyst, and NO x purification ratio after five-hour treatment in the model gas which corresponds to the gas having the air fuel ratio of 18 and which includes 10% of aqueous vapor at the temperature of 700°C and 800°C. Catalysts Maximum NO x Purification Ratio Maximum Temperature for Purifying NO x Early Stage 700°C x 5hr 800°C x 5hr Embodiment 2 24 (230°C) 24 (250°C) 23 (250°C) Embodiment 7 30 (220°C) 28 (250°C) 25 (250°C) Com. Ex. 1 23 (230°C) 22 (240°C) The catalysts in the Preferred Embodiments 2 and 7 in which platinum is loaded on the layered porous silica have higher NO x purification ratio and more excellent heat resistance than that of the catalyst in the Comparative Example 1 in which platinum is loaded on γ-alumina. Eighth Preferred Embodiment By using the layered porous silica which was synthesized from kanemite, various kinds of HC components in the exhaust gases of the engine were absorbed and the rates of absorbing each of HC components were measured. For the comparison, the same measurement was conducted on zeolite (ZSM-5). The result is shown in Figure 6. The above-mentioned measurement was conducted under the following conditions: after the engine was started, exhaust gas was introduced into the converter for one minute under the condition in which engine rotational speed is 1200rpm and the first idle condition in which negative pressure is 250mmHg. Inside the converter, absorbents of above-mentioned layered porous silica or zeolites are filled. In Figure 6, HC adsorbing rates show the adsorbing percentage of HC components (100%), which are included in the above-mentioned exhaust gas, by the above-mentioned adsorbents. The axis of abscissa in Figure 7 shows the HC components such as methane, ethane, toluene and O-xylene, which are included in the above-mentioned exhaust gases. As shown in Figure 6, excluding the part of HC whose molecular weight is relatively low such as ethane and isobutane, HC components whose molecular weight is relatively high such as isopentane, benzene, toluene and O-xylene show higher adsorbing rate in the above-mentioned layered porous silica. Also as shown in Figure 6, the above-mentioned layered porous silica has larger adsorbing capacity especially concerning HC whose carbon atom number is more than 6 and bulky aromatic hydrocarbon. Figures 7 to 9 show the arrangements of layered porous silica (the same arrangement is applied to layered porous silica-metal oxide and the followings are also applied to it) in the converter for purifying exhaust gas. Figure 7 shows the referential example in which only the above-mentioned layered porous silica 95 is filled in the converter 8 to trap HC in the exhaust gas 91. Figure 8 shows the embodiment in which the layered porous silica 95 is provided at the upstream side of the converter 9 and three way catalyst 97 is provided at the downstream side of the converter 9. In this case, at the time of cold starting of the engine, HC components are adsorbed by the layered porous silica 95 and when the temperature of the exhaust gas rises (the time of warming up) this HC can be purged and purified by the three way catalyst 97. Figure 9 shows the embodiment in which the layered porous silica 95 is disposed at the middle portion in the converter 9 and the first catalyst 971 is disposed at the upstream side of the converter 9 and the second catalyst 972 is disposed at the downstream side of it. In this case, the first catalyst 971 is warmed up earlier compared with the second catalyst 972, so the initial purifying rate of HC is high and the burden of adsorbing by the layered porous silica 95 can be reduced. Having now fully described the invention, it will be apparent to one of ordinary skill in the art that many changes and modifications can be made thereto.

Claims: An exhaust gas purifying catalyst comprising a support of a layered porous silica (1) or a layered porous silica-metal oxide (1) that comprises a plurality of silica sheets (10), the sheets (10) being curved and partially connected to each other to form a three-dimensional structure having a plurality of pores (2) in the diameter range of from 1 to 6 nm (10 to 60 Å), having a surface area in the range of from 1,100 to 1,500 m 2 /g and having at least one catalyst metal (3) selected from the group consisting of noble metals, transition metals and rare earth metals, wherein said catalyst metal (3) is loaded on said support. An exhaust gas purifying apparatus which is provided in an exhaust system of an internal combustion engine, comprising an exhaust gas purifying catalyst (97), an adsorbent (95) for trapping hydrocarbon components, the adsorbent (95) disposed upstream with respect to the exhaust gas purifying catalyst (97) in a flow of an exhaust gas and comprising a layered porous silica (1) or a layered porous silica-metal oxide (1) that comprises a plurality of silica sheets (10), the sheets (10) being curved and partially connected to each other to form a three-dimensional structure having a plurality of pores (2) in the diameter range of from 1 to 6 nm (10 to 60 Å), and having a surface area in the range of from 1,100 to 1,500 m 2 /g.

Inventors: BANNO KOUJI, FUKUMOTO KAZUHIRO, FUKUSHIMA YOSHIAKI, HAYASHI KIYOTAKA, INAGAKI SHINJI, KURODA KAZUYUKI, MATSUURA SHINJI, NAGAMI TETSUO, OGAI MASAHIKO, OGURA YOSHITSUGU, OHTA TAKASHI, OKADA AKANE, SAKAKIBARA YUJI, TAKADA YASUO, YAMADA YUKIMURA, BANNO, KOUJI, FUKUMOTO, KAZUHIRO, FUKUSHIMA, YOSHIAKI, HAYASHI, KIYOTAKA, INAGAKI, SHINJI, KURODA, KAZUYUKI, MATSUURA, SHINJI, NAGAMI, TETSUO, OGAI, MASAHIKO, OGURA, YOSHITSUGU, OHTA, TAKASHI, OKADA, AKANE, SAKAKIBARA, YUJI, TAKADA, YASUO, YAMADA, YUKIMURA, Banno, Kouji, c/o Kabushiki Kaisha Toyota, Fukumoto, Kazuhiro, c/o Kabushiki Kaisha Toyota, Fukushima, Yoshiaki, c/o Kabushiki Kaisha Toyota, Hayashi, Kiyotaka, c/o Cataler Ind. Co., Ltd., Inagaki, Shinji, c/o Kabushiki Kaisha Toyota, Matsuura, Shinji, c/o Cataler Ind. Co., Ltd., Ohta, Takashi, c/o Kabushiki Kaisha Toyota, Okada, Akane, c/o Kabushiki Kaisha Toyota, Sakakibara, Yuji, c/o Kabushiki Kaisha Toyota, Takada, Yasuo, c/o Kabushiki Kaisha Toyota, YAMADA, YUKIMURA, C/O CATALER IND. CO., LTD.
Applicants: TOYOTA MOTOR CO LTD, TOYOTA JIDOSHA KABUSHIKI KAISHA
Application year: 1993
Main classification: B01J29
IPC codes: B01D53, B01J21, B01J29