NOx CATALYST AND METHOD OF USING THE SAME

Abstract: A NOx abatement composition comprises a NOx abatement catalyst and a NOx sorbent material which are dispersed in proximity to, but segregated from, each other on a common refractory carrier member (10). The NOx sorbent material comprises a basic oxygenated metal compound and optionally further comprises ceria. The NOx abatement catalyst contains a catalytic metal component including a platinum metal catalytic component. The catalytic metal component is segregated from the NOx sorbent material, which may be one or more of metal oxides, metal carbonates, metal hydroxides and mixed metal oxides. At least the catalytic metal component and the NOx sorbent material must be on, or comprise separate, particles; the particles may either be admixed or may be disposed in separate layers (20a, 20b) on the carrier member (10). A NOx abatement method employs the composition and includes periodically adjusting the gas being treated between lean and stoichiometric/rich operating cycles.

Description: NO,CATALYSTANDMETHODOFUSINGTHESAME BACKGROUND OF THE INVENTION Field of The Invention The present invention is broadly concerned with NO χ abatement, especially with NO χ abatement in the exhaust gas of lean-burn internal combustion engines. More spe- cifically, the present invention is concerned with a novel composition comprising a combination of a NO χ trap (sor¬ bent material) and a NO χ abatement catalyst, and to a method of using the same. Related Art It is well-known in the art to utilize catalyst com¬ positions, such as those commonly referred to as three-way conversion catalysts ("T C catalysts") to treat the ex¬ haust gases of internal combustion engines. Such cata- lysts have been found to successfully promote both the oxidation of unburned hydrocarbons ("HC") and carbon mon¬ oxide ("CO") and the reduction of nitrogen oxides ("NO χ ") in the exhaust gas, provided that the engine is operated at or close to stoichiometric air/fuel conditions. How- ever, many present day engines, especially gasoline-fueled engines used for passenger automobiles and the like, are designed to operate under lean conditions at least part of the time as a fuel economy measure. That is, the ratio of air to fuel in the combustion mixture supplied to the en- gine is maintained above the stoichiometric ratio so that the resulting exhaust gases are "lean", i.e., the exhaust gases are relatively high in oxygen content and relatively low in reductants content, e.g., HC, CO and/or hydrogen. Although lean burn engines provide enhanced fuel economy, they have the disadvantage that conventional TWC catalysts cannot adequately abate the NO χ component of pollutants in the gas stream. The art has devoted some effort to developing catalysts specifically designed to treat the exhaust of lean burn engines. One such effort is described in the publication Environmental Catalysis For A Better World And Life, Proceedings of the 1st World Congress at Pisa, Italy, May 1-5, 1995, published by the Societa Chimica Italiana of Rome, Italy. At pages 45-48 of the publication, there is an article entitled "The New Concept 3-Way Catalyst For Automotive Lean-Burn Engine Storage and Reduction Catalyst", by Takahashi et al (below referred to as "the Takahashi et al paper"). This article discloses the preparation of catalysts by impregnating precious metals, mainly platinum, and various alkaline and alkaline earth metal oxides, mainly barium oxide, and rare earth oxides on supports, mainly alumina. These catalysts were employed for NO χ purification of actual and simulated exhaust gases. At page 47 of the article, there is both shown graphically in Figure 5 and discussed in paragraph 3.1.1., "NO χ Storage Mechanism", the concept of employing NO χ storage compounds in conjunction with the catalytic (platinum) component, with both the NO χ storage compounds and the catalytic component dispersed on a common support material. It is stated that "When precious metals were separated from the NO χ storage compounds on these cata¬ lysts, the NO χ storage amount drastically decreased." Paragraph 3.1.1. therefore teaches that the NO χ storage compound and the platinum catalyst should be intimately admixed by being disposed on the same increment of, e.g., alumina, support as described in the catalyst preparation procedure described in paragraph 2 (page 45) and illu¬ strated in Figure 5. In paragraph 3.1, page 46, testing of the catalysts is described as being carried out with simulated exhaust gases alternately under oxidizing and reducing conditions. The conclusion is drawn on the last sentence on page 46, that N0 χ was stored in the catalyst under oxidizing con- ditions and that the stored N0 χ was then reduced to nitro¬ gen under stoichiometric and reducing conditions. SAE paper 950809 published by the Society of Automo¬ tive Engineers, Inc., Warrendale, Pennsylvania, and en- titled Development of New Concept Three-Way Catalyst for Automotive Lean-Burn Engines, by Naoto Miyoshi et al, was delivered at the International Congress and Exposition, Detroit, Michigan, February 27-March 2, 1995. This paper, referred to below as "the SAE paper", which has authors in common with the above-mentioned Takahashi et al paper, contains a disclosure which is substantially the same as, but is more detailed than, that of the Takahashi et al paper. At page 123 of the SAE paper a correlation between basicity of the elements used as N0 χ storage material and NO χ storage capacity is discussed as is NO χ adsorption by complex oxides such as YBa 2 Cu 3 0y and CuO-BaO. The discus¬ sion of mixed oxides is made with reference to items 6 and 7 of the references cited at the end of the SAE paper. The references are "Uptake of NO gas by YBa 2 Cu 3 0y" by K. Tabata et al, Chem. Lett., 1988, pp. 799-802 and "NO re¬ moval by adsorption into BaO-CuO binary oxides" by M. Machida et al, J. Chem. Soc. Chem. Commum. 1990, pp. 1165-1166. At page 125 of the SAE paper, there is a com- parison of two catalysts. One catalyst comprises (a) noble metal impregnated on one increment of alumina and the NO χ storage component impregnated on alumina, and the other catalyst comprises (b) both noble metal and the storage component impregnated on the same increment of alumina. The SAE paper states that catalyst (a) stored a very small amount of NO χ as compared to catalyst (b) and concludes that the "storage amount increases when the noble metal is in the proximity of the storage component". U.S. Patent 5,202,300, "Catalyst For Purification of Exhaust Gas", issued on April 13, 1993, to . Funabiki et al, discloses a catalyst composition comprising a refrac¬ tory support having deposited thereon an active layer con¬ taining a palladium and rhodium catalytic metal component dispersed on alumina, a cerium compound, a strontium com- pound, and a zirconium compound. (See the Abstract.) This patent discloses the preparation of the catalyst by im¬ pregnating alumina particles with palladium and rhodium and then combining the impregnated alumina with compounds such as cerium nitrate, strontium acetate hemi-hydrate and zirconyl acetate together with acetic acid and deionized water in a ball mill, and crushing and mixing the mixture to provide a slurry which is applied to a monolithic, cyl- indrical cordierite carrier. See columns 3-5 of the Funa- biki et al Patent, especially Example 1 which discloses that the strontium compound is solubilized in the acidi¬ fied water and impregnated into the alumina support parti¬ cles together with the palladium and rhodium catalytic me- tal components. Example 1 as Funabiki et al, like the Takahashi et al and SAE papers referred to above, impreg¬ nates both the alkaline earth metal compound (a strontium compound in the case of Funabiki et al) , and the palladium and rhodium catalytic metal components into the same in- crement of (alumina) support material. However, Example 2 of Funabiki et al substitutes strontium hydroxide for the strontium acetate and the limited solubility of strontium hydroxide suggests that it remains in bulk form in the finished product, admixed with the palladium and rhodium- impregnated alumina. SUMMARY OF THE INVENTION Generally, the present invention provides a composi¬ tion containing a NO χ sorbent material and a NO χ abatement catalyst, the latter including one or more catalytic metal components essentially including a platinum catalytic metal component. The abatement catalyst may optionally include one or more other platinum group metal components. The composition is characterized by the catalytic metal components being segregated from the NO χ sorbent material at least to the extent that the catalytic metal components and the NO χ sorbent material are not dispersed on the same increment of support material. Preferably, the NO χ sor¬ bent material is a bulk material and it is substantially free of any catalytic metal components dispersed thereon. Inasmuch as ceria is not effective for NO χ abatement it is not considered to be a catalytic metal component and in certain embodiments of the invention ceria may optionally be combined with the NO χ sorbent material. Specifically, in accordance with the present inven¬ tion there is provided a composition for NO χ abatement in a gas stream, the composition comprising a NO χ abatement catalyst and a NO χ sorbent material disposed in proximity to each other on a common refractory carrier member. The NO χ abatement catalyst comprises a catalytic metal compo¬ nent comprised of a platinum catalytic metal component. The catalytic metal component is dispersed on a first re- fractory support material, e.g., alumina. The NO χ sorbent material comprises at least one basic oxygenated metal compound, e.g., strontium oxide or strontium hydroxide, which is segregated from the platinum group metal cata¬ lytic component, at least to the following extent. When the NO χ sorbent material is dispersed on a refractory sup¬ port material, the catalytic metal component and the NO sorbent material are not dispersed on the same increment of refractory support material. When the NO χ sorbent material is present in bulk form, the catalytic metal component is not impregnated into the bulk N0 χ sorbent material. In one aspect of the invention the catalytic metal component further comprises at least one other platinum group metal catalytic component in addition to the plati- num catalytic metal component. In another aspect of the invention, the NO χ sorbent material is selected from the group consisting of one or more of metal oxides, metal carbonates, metal hydroxides and mixed metal oxides. Optionally, the NO χ sorbent ma- terial may further comprise ceria, e.g., bulk ceria. Yet another aspect of the invention provides that the N0 χ sorbent material comprises a mixed metal oxide sel¬ ected from the group consisting of one or more of barium strontium tungstate, barium strontium niobate, strontium titanate, barium zirconate, barium silicate and barium strontium titanate. In another aspect of the invention, the NO χ sorbent material is selected from the group consisting of one or more of metal oxides, metal hydroxides, metal carbonates, and mixed metal oxides, wherein the metals of the metal oxides, metal hydroxides and metal carbonates and at least one of the metals of the mixed metal oxides are selected from the group consisting of lithium, sodium, potassium, rubidium, cesium, magnesium, calcium, strontium and bari¬ um. One aspect of the present invention provides that the N0 χ abatement catalyst is admixed with the N0 χ sorbent ma- terial; another aspect of the invention provides that the N0 χ abatement catalyst is disposed as a first discrete layer on the refractory carrier member and the NO χ sorbent material is disposed as a second discrete layer on the refractory carrier member. Yet another aspect of the in- vention provides that the first discrete layer (the NO χ abatement catalyst) comprises an underlayer disposed on the carrier member and the second discrete layer (the NO χ sorbent material) comprises an overlayer superposed on the underlayer. In any case, the discrete layers may be in direct contact one with the other or an intervening layer, e.g, alumina, may be interposed between the two discrete layers. Still other aspects of the present invention provide one or more of the following features: the N0 χ abatement catalyst may comprise, in addition to the platinum cata¬ lytic metal component, one or more other platinum group metal catalytic components; the refractory support materi¬ al may comprise a refractory metal oxide; and the NO χ sor¬ bent material may comprise a metal oxide selected from the group consisting of oxides of one or more of magnesium, calcium, strontium and barium. Yet another aspect of the invention provides that the refractory carrier, e.g, made of cordierite, comprises a body having a plurality of gas flow passages extending therethrough, the passages being defined by passage walls, and the NO χ abatement catalyst and the N0 χ sorbent mate¬ rial, e.g., the first and second layers, are disposed on the passage walls. Still another aspect of the invention provides that the refractory carrier comprises a body of carrier beads retained within a gas-permeable container. In such case, the NO χ abatement catalyst and the N0 χ sorbent material, e.g., the first and second layer may be arranged so that the first layer is disposed on one increment of carrier beads and the second layer is disposed on a second incre¬ ment of carrier beads, with the first and second incre¬ ments of carrier beads admixed within the container. Alternatively, the first and second layers may be disposed on the same increment of carrier beads or the N0 χ abate¬ ment catalyst and the N0 χ sorbent material may also be mixed on the same increment of carrier beads. In accordance with the method aspect of the present invention there is provided a method of N0 χ abatement com¬ prising contacting a gas stream containing NO χ with a NO abatement composition as defined above. The method in¬ cludes periodically adjusting the composition of the gas stream between lean and stoichiometric/rich conditions to thereby provide alternating lean operating condition per¬ iods and stoichiometric/rich operating condition periods, and maintaining NO χ abatement conditions during the stoi¬ chiometric/rich operating condition periods, whereby dur¬ ing the lean operating periods the NO χ abatement catalyst promotes sorption of NO χ by the NO χ sorbent material and during the rich operating periods the NO χ abatement cata¬ lyst promotes reduction of NO χ to nitrogen. As used herein and in the claims, the following terms, whether used in singular or plural form, have the indicated meanings. Reference herein and in the claims to the NO χ abate¬ ment catalyst and the NO χ sorbent material being "in proximity to each other on a common refractory carrier member" means that the N0 V abatement catalyst and the NO„ sorbent material are either admixed with each other, or disposed in respective superposed layers, on the same car¬ rier member. When a component, such as ceria or the N0 χ sorbent material, is described as a "bulk" component, this means that the component is present as solid particles thereof. These particles are usually very fine, on the order of at least 90 percent of the particles being from about 5 to 15 microns in diameter. The term "bulk" is intended to dis¬ tinguish from the situation in which a component is "dis¬ persed" on a refractory support material by being impreg¬ nated into the support material from a solution or other liquid dispersion of the component. For example, it is well-known in the art to stabilize activated alumina (pre¬ dominantly γ-alumina), which is used as a refractory sup¬ port material, against thermal degradation in TWC and oth¬ er catalyst compositions by impregnating the particles of alumina with the solution of a soluble cerium compound such as a solution of cerium nitrate. After impregnation, the alumina particles are dried and calcined in air to convert the impregnated cerium nitrate to ceria. The re¬ sultant ceria is thus "dispersed" onto and, to a greater or lesser extent, within a surface layer of the solid par- tides of the alumina. The dispersed ceria is not present in bulk form, because bulk ceria comprises fine, solid particles of ceria. Reference to components which are not being dispersed on "the same increment" or "increments" of refractory sup- port material simply means that the components are not dispersed on the same particles of refractory support ma¬ terials. For example, consider a situation in which a catalytic metal component is dispersed onto one batch of alumina particles and a NO χ sorbent material is dispersed onto a second, different batch of alumina particles. This situation would result in the catalytic metal component and the N0 χ sorbent material being dispersed on "different increments" of alumina. This situation differs from that described, for example, in the aforementioned Funabiki et al U.S. Patent 5,202,300 wherein, following the procedure of Example 1 thereof, the palladium and rhodium catalytic metal components are dispersed onto alumina particles and thereafter a strontium compound (as well as other com- pounds) are dispersed onto the same alumina particles onto which the palladium and rhodium catalytic components are dispersed. In that case, the platinum/rhodium and stron¬ tium compounds are dispersed onto the same increment of alumina. Reference to a "catalytic metal component" means a catalytic metal, such as a platinum group metal, whether the metal is present as the element, or alloy or a com¬ pound, e.g., an oxide, and which is effective to catalyze NO χ abatement in a gas stream. The term "platinum group metals" means and includes platinum, rhodium, palladium, ruthenium, iridium and os¬ mium. The term "washcoat" has its usual meaning in the art of a thin, adherent coating of a catalytic or other mate¬ rial applied to a refractory carrier material such as a honeycomb-type carrier member, and which is porous to per¬ mit the passage therethrough of the gas stream being treated. The term "stoichiometric/rich" is used with reference to the condition of the gas stream being treated and re¬ fers collectively to the stoichiometric and rich operating conditions of the gas stream. The term "gas stream" means a stream of gaseous con- stituents, such as the exhaust of an internal combustion engine, which may contain entrained non-gaseous components such as liquid droplets, solid particulates and the like. The term "mixed metal oxide" means bimetallic or multi-metallic oxygen compounds, such as Ba 2 SrW0 6 , which are true compounds and is not intended to embrace mere mixtures of two or more individual metal oxides such as a mixture of SrO and BaO. BRIEF DESCRIPTION OF THE DRAWINGS Figure 1 is a perspective view of a catalyst/trap composition comprising a honeycomb-type refractory carrier member in accordance with one embodiment of the present invention; Figure IA is a partial cross-sectional view enlarged relative to Figure 1 and taken along a plane parallel to the end faces of the carrier of Figure 1; Figure IB is a view enlarged relative to Figure IA of one of the gas flow passages shown in Figure IA; Figure IC is a cross-sectional schematic partial view of a carrier body comprising a gas-permeable container within which are disposed a plurality of carrier beads in accordance with one embodiment of the present invention; and Figures 2-12 show various graphs plotting test data comprising (except for Figure 2A) N0 χ removal versus the gas stream temperature at the inlet to the composition being tested, for certain embodiments of the present in- vention and for certain comparative compositions; Figure 2A plots N0 χ removal versus time. DETAILED DESCRIPTION OF THE INVENTION AND SPECIFIC EMBODIMENTS THEREOF Contrary to some teachings of the prior art, for ex¬ ample, the discussion in the above-mentioned Takahashi et al and SAE papers, it has surprisingly been found that an exceedingly effective and durable composition for the abatement of N0 χ in a gas stream is provided by a composi- tion comprising a N0 χ sorbent material and one or more catalytic metal components, essentially including a plati¬ num catalytic metal component, in which the N0 χ sorbent material is in proximity to but segregated from the cata¬ lytic metal component or components. In one embodiment of the invention, both the catalytic metal component or com¬ ponents and the N0 χ sorbent material or materials are dispersed onto different respective increments or batches of support material, such as activated alumina. In this embodiment, the N0 χ sorbent material is dispersed onto a first batch of refractory support material to provide a "supported N0 χ abatement material" and the catalytic metal component is dispersed onto a second batch of refractory support material. Ceria, either in dispersed or bulk for , is often used as an oxygen-storage component of three-way conversion catalysts and therefore may be a component of the NO χ abatement catalyst, although the NO x abatement catalyst will in such case necessarily also contain other catalytic metal components effective for NO abatement. In another embodiment of the invention which is pre¬ ferred because it is believed that it provides enhanced NO X v sorption and release characteristics, the NOX v sorbent material is provided in bulk form, i.e., as discrete fine particles of the N0 χ sorbent material, to provide a "bulk N0 χ sorbent material". In this embodiment, the composi¬ tion comprises refractory support material such as parti¬ cles of activated alumina impregnated with the catalytic metal component, and particles of the N0 χ sorbent materi¬ al, i.e., in bulk form. Whichever of the two above-described embodiments of the present invention is employed, either embodiment may be employed as a mixture of the N0 χ abatement catalyst and NO χ sorbent material or as discrete layers of the NO χ abatement catalyst and NO χ sorbent material. The requi¬ site segregation of the abatement catalyst and sorbent material is attained in a mixture of the NO χ abatement catalyst with either the supported NO χ sorbent material or bulk N0 χ sorbent material because in both cases the cata¬ lytic metal component is supported on particles of support material which do not also support NO χ sorbent material and the N0 χ sorbent material does not support any cata¬ lytic metal component. Of course, when the NO χ sorbent material, whether supported or bulk, is disposed in a dis¬ crete layer separate from a second discrete layer of NO χ abatement catalyst, a still higher degree of segregation is attained. The degree of segregation may be further en¬ hanced by disposing an intermediate washcoat layer between the layers of abatement catalyst and support material. However, it has been found that an excessive degree of segregation of the (1) NO χ abatement catalyst and (2) the N0 χ sorbent material, such as that attained by depositing (1) and (2) on respective, separate carrier members dis¬ persed in series gas flow, yielded very poor results. The segregated components (1) and (2) are therefore, in ac¬ cordance with the present invention, disposed on a common carrier member in proximity to each other. In a specific embodiment, the composition of the pre¬ sent invention may comprise a refractory carrier member such as a honeycomb-type member comprising a unitary body made of a suitable material such as cordierite and having a plurality of fine, parallel gas flow passages extending therethrough from an inlet face to an outlet face of the member. The walls defining these fine gas flow passages may be coated in a manner well-known in the art with a washcoat comprising either a mixture of fine particles of the N0 χ abatement catalyst and N0 χ sorbent material, or the walls may be coated with a respective discrete layer of NO χ abatement catalyst and a respective discrete layer of NO χ sorbent material. The NO χ abatement catalyst is preferably disposed as a first or underlayer on the car- rier with the N0 χ sorbent material being disposed as a second overlayer superposed on the underlayer. Optional¬ ly, the two layers may be separated by an intermediate layer, such as an intermediate layer of one or more of alumina, zirconia, ceria, titania or other suitable re- fractory metal oxide. Alternatively, the two layers may be in "direct contact" with each other, by which is meant that there is no intervening layer of another material be¬ tween the respective catalyst and sorbent material layers. Figure 1 shows generally at 10 a refractory carrier member of generally cylindrical shape having a cylindrical outer surface 12, one end face 14 and an opposite end face, not visible in Figure 1, which is identical to end face 14. The junction of outer surface 12 with the oppo¬ site end face at its peripheral edge portion is indicated at 14' in Figure 1. Carrier member 10 has a plurality of fine, parallel gas flow passages 16 formed therein, better seen in enlarged Figure IA. Gas flow passages 16 are formed by walls 18 and extend through carrier 10 from end face 14 to the opposite end face thereof, the passages 16 being unobstructed so as to permit the flow of a fluid, e.g., a gas stream, longitudinally through carrier 10 via gas flow passages 16 thereof. As will be seen from Fig- ures IA and IB walls 18 are so dimensioned and configured that gas flow passages 16 have a substantially regular polygonal shape, substantially square in the illustrated embodiment, but with rounded corners in accordance with U.S. Patent 4,335,023, issued June 15, 1982 to J.C. Dett- ling et al. A layer 20, which in the art and sometimes below is referred to as a "washcoat", is adhered to the walls 18 and, as shown in Figure IB, may be comprised of a single layer comprising a mixture of N0 χ abatement cata¬ lyst and N0 χ sorbent material. Alternatively, as illu- strated in Figure IB, layer or washcoat 20 may comprise a first discrete layer or underlayer 20a and a second dis¬ crete layer or overlayer 20b superposed over first layer 20a. The first layer or washcoat 20a preferably is com¬ prised of the NO χ abatement catalyst and the second layer or washcoat 20b is preferably comprised of the NO χ sorbent material and is superposed over layer 20a. However, the arrangement of the layers may be reversed, with the first layer 20a comprised of the N0 χ sorbent material and the second layer 20b comprised of the NO χ abatement catalyst. For purposes of illustration, the thickness of layers 20, 20a and 20b are exaggerated in Figures IA and IB. As shown in Figures 1-1B, the honeycomb-type carrier members include void spaces provided by the gas-flow pas¬ sages, and the cross-sectional area of these passages and the thickness of the walls defining the passages will vary from one type of carrier member to another. Similarly, the weight of washcoat applied to such carriers will vary from case to case. Consequently, in describing the quan¬ tity of washcoat or catalytic metal component or other component of the composition, it is convenient to use units of weight of component per unit volume of catalyst carrier. Therefore, the units grams per cubic inch ("g/in 3 ") and grams per cubic foot ("g/ft 3 ") are used herein to mean the weight of a component per volume of the carrier member, including the volume of void spaces of the carrier member. The density of gas flow passages per unit surface area of the end faces of the carrier member is expressed herein as the number of cells (passages) per square inch, or "cpsi". Generally, the NO χ sorbent material comprises at least one basic oxygenated metal compound and, as indi- cated above, may either be dispersed onto a refractory support material such as activated alumina, or may be present in bulk form, i.e., as fine particles of the basic oxygenated metal compound. As used herein and in the claims, an "oxygenated metal compound" means a compound of metal and oxygen which may or may not contain other ele¬ ments. For example, the basic oxygenated metal compound may comprise one or more of a metal oxide, a metal carbon¬ ate, a metal hydroxide or a mixed metal oxide. The metal of such compounds (at least one of the metals in the case of the mixed oxides) is preferably selected from the group consisting of one or more of lithium, sodium, potassium, rubidium, cesium, magnesium, calcium, strontium and bari¬ um. Strontium oxide has been found to be an especially useful NO χ sorbent material. The NO χ sorbent material will be present in an amount calculated to provide ade¬ quate sorption for the intended use. A typical quantity of the basic metal oxygenated compound will be from about 0.05 to 3 g/in 3 . The NO χ sorbent material may optionally include a sulfur compound sorbent such as ceria, either as bulk ceria or as ceria dispersed into the particles of NO χ sorbent material. In the latter case, the NO χ sorbent material may be impregnated with a solution of a soluble cerium salt such as cerium nitrate and then dried and heated in air to convert the cerium nitrate to cerium ox¬ ide (ceria). It has been found that when present in eith¬ er bulk or dispersed form, ceria facilitates coating the carrier member with a washcoat of the NO χ sorbent material and also protects the basic oxygenated metal compounds comprising the NO χ sorbent material from poisoning by sulfur oxides which may be present in the gas stream being treated as the sulfur oxides are preferentially sorbed on the ceria. The NO χ sorbent material may thus advanta¬ geously contain ceria in a weight ratio of ceria to NO sorbent material of from about 0.1 to 100:1. Typically, ceria may be present in the composition in the amount of from about 0.05 to 1.0 g/in 3 , as Ce0 2 . The N0 χ sorbent material may also contain a binder such as alumina to en¬ hance adherence of the NO χ sorbent material to the carrier member. The N0 χ abatement catalyst may comprise any catalyst which will catalyze the reduction of NO χ in the presence of a suitable reductant, usually hydrocarbons or CO in the case of treating the exhaust from an internal combustion gasoline engine. Without intending to be bound by any particular theory, it is believed that the platinum cata¬ lytic metal component of the NO χ abatement catalyst of the present invention serves a number of functions, including promoting the sorption of N0 χ by the N0 χ sorbent material during lean phase operation. In addition to catalyzing reduction of NO χ during rich phase operation the platinum catalytic metal component is also believed to catalyze some N0 χ reduction during at least a part of the lean phase operation. The N0 χ abatement catalyst may comprise a suitable catalyst containing a platinum catalytic metal component and, optionally, one or more other platinum group metal catalytic components. Typically, these will include one or more of rhodium and palladium although other platinum group metal components may also be employed. A suitable NO χ abatement catalyst for utilization in accordance with the present invention is a conventional TWC catalyst which usually comprises one or more platinum group metal compo¬ nents including a platinum component dispersed on a re¬ fractory support. The refractory support is typically a refractory metal oxide such as activated alumina. TWC catalysts may also include a so-called oxygen storage com¬ ponent which may comprise bulk ceria or a base metal oxide such as an oxide of nickel, iron, manganese or copper. The art is replete with well-known TWC compositions. In a typical composition of the present invention, the amount of platinum group metal present will be from about 5 to 150, preferably from about 20 to 80 g/ft 3 . Of that amount, platinum will typically comprise from about 4 to 125 g/ft 3 , preferably from about 17 to 67 g/ft 3 . A typical method of manufacturing a catalyst composi¬ tion in accordance with the present invention is to pro¬ vide the NO χ abatement catalyst as a first coating or lay¬ er on the walls of the gas flow passages of a suitable re¬ fractory carrier member such as a cordierite honeycomb carrier. This may be accomplished, as is well-known in the art, by impregnating fine particulate activated alu¬ mina with one or more catalytic metal components such as platinum or platinum and rhodium, drying and calcining the impregnated activated alumina particles and forming an aqueous slurry of these particles together with particles of bulk ceria. (As used herein, the term "activated alu¬ mina" has its usual meaning in the art of a relatively high surface area alumina, as compared, e.g., to α-alu- mina (alpha), comprising predominantly γ-alumina (gamma) although other phases such as h-alumina (eta) may also be present. ) The activated alumina may have initially been thermally stabilized, as is well-known in the art, by im¬ pregnating it with, for example, a solution of a soluble salt of barium, lanthanum, rare earth metal or other known stabilizer precursor, and calcining the impregnated acti¬ vated alumina to form a stabilizing metal oxide dispersed onto the alumina. Base metal catalysts may also have been impregnated into the activated alumina, for example, by impregnating a solution of nickel nitrate into the alumina particles and calcining to provide nickel oxide dispersed in the alumina particles. The carrier member may then be immersed into the slurry of impregnated activated alumina and excess slurry removed to provide a thin coating of the slurry on the walls of the gas flow passages of the carrier. The coated carrier is then dried and calcined to provide an adherent coating of the N0 χ abatement catalyst to the walls of the passages thereof. The carrier may then be immersed into a slurry of fine particles of a basic oxygenated metal com¬ pound, for example, in an aqueous slurry of fine particles of bulk strontium oxide, and a second or overlayer coating of a NO χ sorbent material is thus deposited over the first or underlayer of N0 χ abatement catalyst. The member is then dried and calcined to provide a finished catalyst composition in accordance with one embodiment of the pres¬ ent invention. Alternatively, the alumina particles impregnated with the catalytic component may be mixed with bulk or support¬ ed particles of the NO χ sorbent material in an aqueous slurry, and this mixed slurry of NO χ abatement catalyst particles and NO χ sorbent material particles may be ap¬ plied as a coating to the walls of the gas flow passages of the carrier member. In another embodiment of the present invention, the refractory carrier member may comprise a body of beads, pellets or particles (collectively referred to as "carrier beads") made of a suitable refractory material such as γ-alumina, coated with the N0 χ abatement catalyst and the NO χ sorbent material. A body of such carrier beads may be contained within a suitable perforated container which permits the passage of the exhaust gas therethrough. Fig¬ ure IC shows such an embodiment of the invention in which the carrier member 10' comprises a perforated metal con¬ tainer 11 enclosed on all sides by walls 22 within which is formed a regular pattern of perforations 22a. The in¬ terior of the container 11 is packed with a plurality of carrier beads 24 on which are disposed the N0 χ abatement catalyst and NO χ sorbent material. The member 10' illus¬ trated in Figure IC would be, as well-known to those skilled in the art, contained within a structure (not shown) designed to direct the flow of the gas stream being treated through member 10', as indicated in Figure IC by the unnumbered arrows. In one embodiment of the inven¬ tion, a proportion, e.g., approximately one-half, of the carrier beads 24 may have the NO χ abatement catalyst coated thereon and the remainder may have the NO χ sorbent material coated thereon. The two different increments of carrier beads 24 are thoroughly admixed so that the NO abatement catalyst and NO χ sorbent material are more or less uniformly distributed throughout the interior of the container 11. In another embodiment, the same increment of carrier beads may be coated with both the NO χ abatement catalyst and the N0 χ sorbent material, preferably in dis¬ crete respective layers thereof, and most preferably with the layer of NO χ sorbent material superposed over the layer of N0 χ abatement catalyst. Without wishing to be bound by any particular theory of operation, it is believed that when the gas stream, e.g., engine exhaust, to be treated is lean, NO χ contained in the gas stream is sorbed onto the NO χ sorbent material, thereby removing the sorbed NO χ from the stream discharged to the atmosphere. The platinum catalytic component is believed to promote such sorption. This lean sorption occurs during a lean operating period which is terminated by rendering the gas stream rich, as may be accomplished by decreasing the air-to-fuel ratio of the combustible mixture fed to the engine generating the exhaust, or by directly introducing a suitable reductant such as hydro¬ carbons into the exhaust gas stream. The hydrocarbons or other suitable reductant in the gas stream will displace the sorbed NO χ from the NO χ sorbent material, and the dis¬ placed NO χ contacts the NO χ abatement catalyst in the presence of the reductant and otherwise under conditions (a suitable elevated temperature) such that the N0 χ is re¬ duced. Some or all of the N0 χ may be reduced to nitrogen or to nitrogen and N 2 0. In accordance with the method aspect of the present invention, the exhaust gas is alternately adjusted between lean and stoichiometric/rich operating conditions so as to provide alternating lean operating periods and stoichio¬ metric/rich operating periods. It will be understood that the gas stream, e.g., exhaust, being treated may be selec¬ tively rendered lean or stoichiometric/rich either by ad- justing the air-to-fuel ratio fed to the engine generating the exhaust or by periodically injecting a reductant into the gas stream upstream of the catalyst. For example, the composition of the present invention is well-suited to treat the exhaust of diesel engines which continuously run lean. In such case, in order to establish a stoichiomet¬ ric/rich operating period, a suitable reductant, such as diesel fuel, may be sprayed into the exhaust immediately upstream of the catalyst composition of the present in¬ vention. Such diesel fuel introduction will be carried out periodically so as to alternate lean and stoichiomet¬ ric/rich periods of the exhaust. Even if the overall con¬ dition of the exhaust (or other gas stream) being treated is lean, stoichiometric/rich local conditions may be peri¬ odically imposed at and within the catalyst composition. During the lean operating periods NO χ is sorbed by the N0 χ sorbent material and such sorption may take place at temperatures of from about 150°C to about 600°C. The sorbed N0 χ is desorbed during stoichiometric/rich oper¬ ating periods and/or high temperature periods. The reduc- tion of N0 χ during the stoichiometric/rich operating peri¬ od is promoted by contact of the reactants with the NO abatement catalyst under NO χ abatement conditions, typi¬ cally at temperatures of from about 200°C to about 800°C. For gasoline, a stoichiometric air-to-fuel weight ratio ("A/F") is 14.6. Lambda (λ) is usually used to symbolize the ratio of the actual A/F to the stoichiometric A/F. Therefore, λ = 1 is a stoichiometric A/F, λ > 1 is lean and λ < 1 is rich. Gasoline-fueled engine lean operation is usually at λ = about 1.03 to 1.30. The following examples illustrate the preparation and testing of specific embodiments of the invention. It will be noted that the platinum group metal catalytic compo- nents are segregated from the NO χ sorbent materials, in accordance with the teachings of the present invention. The following test procedure was employed. Test Procedure A Catalysts were tested as follows. A feed stream com¬ prising 250 ppm NO, 333 ppm propylene (equivalent to 1000 ppm C 1 ), 10% steam, 10% 0 2 , 50 ppm S0 2 and balance nitro¬ gen, giving a C 1 to NO χ ratio of 4 to 1, was flowed through the catalyst, which had previously been heated in air to 100°C, at a space velocity of 25,000/h. The tem¬ perature was then ramped up at a rate of 10°C/minute up to a temperature of 600°C and the exit gases were tested for NO χ content. In the Figures showing plots of N0 χ removal versus temperature, the amount of N0 χ removal is the net of (1) N0 χ converted to innocuous gases (N 2 and N 2 0) and sorbed by the NO χ sorbent material, less (2) NO χ desorbed from the NO χ sorbent material. The amount of NO χ removal is expressed as a percentage of the total N0 χ present in the inlet gas. A negative percentage indicates a net release of N0 χ from the sorbent material into the gas stream. Example 1 A. Eleven grams of a soluble platinum salt contain¬ ing 18.2% Pt by weight was dissolved in 55 ml of deionized water. The resulting platinum salt solution was used to impregnate 100 g of γ-alumina having a BET (Brunnauer- Emmett-Teller) surface area of 150 square meters per gram (m 2 /g). The platinum salt solution was added with contin¬ uous mixing to give an impregnated alumina containing 2% by weight Pt (dry basis). The sample was ball milled about 30 minutes following which five grams of acetic acid was added into the mix to fix the Pt onto the alumina sur- face. The mixture was then slurried with deionized water to make a slurry of 45% solids and the slurry was further milled in a ball mill to a particle size of 90% of the particles being less than 10 microns in diameter. The re- sulting slip is designated Slip A. B. Slip A was coated onto a cylindrical cordierite carrier member measuring 1.5 inches in diameter by 3.0 inches in length and containing 400 cells per square inch ("cpsi"). The coated carrier member was then dried at 100°C and calcined at 550°C for two hours to give a wash¬ coat weight of the calcined catalyst of 2 g/in 3 and a Pt loading of 70 g/ft 3 . The resulting catalyst member pro¬ vided a comparative platinum-containing abatement catalyst and was designated Catalyst C-l. Example 2 A. A 250 g quantity of the same type of alumina as used in Part A of Example 1 was thoroughly mixed with 750 g of strontium oxide (SrO) powder, i.e., bulk SrO. The SrO-Al 2 0 3 mixture was slowly added to 2000 g of deionized water with mixing. The mixture was kept in an ice bath to prevent the added deionized water from boiling, and mixing was continued to bring the Sr0-Al 2 0 3 mixture to room tem- perature. Then 150 g of acetic acid (5% based on slurry weight) was added to the mixture followed by 150 g of Nyacol Al-20 alumina binder (5.1% based on dry solids weight). Mixing was continued for an additional 15 min¬ utes. The resulting slurry was placed in a ball mill jar and ball milled overnight to a particle size of 90% of particles less than 10 micron. The solids level was ad¬ justed with deionized water to 36% solids. The resulting sorbent material (or trap) slurry is designated Slip T-l. B. The catalyst member C-l of Example 1 was coated with Slip T-l obtained in Part A of this Example 2. The coated member was then dried at 100°C and calcined at 550°C for 2 hours to provide a washcoat overlayer of 1 g/in 3 superposed over the Pt/Al 2 0 3 layer(now an underlay¬ er) of Catalyst C-l. The resulting composition provided an embodiment of the present invention comprising a bulk strontium oxide sorption material overlayer superposed over a platinum-containing abatement catalyst underlayer and was designated Catalyst E-l. C. A conventional, commercially available three-way catalyst has a precious metal loading of 70 g/ft 3 com¬ prised of Pt and Rh in a weight ratio of 5 to 1 Pt:Rh. The catalytic precious metals are dispersed on activated alumina and the catalyst has a washcoat loading (alumina plus Pt and Rh) of 2 g/in 3 . The catalyst had been dried and calcined at 450°C. The slurry T-l obtained in Part A of this Example 2 was coated over the TWC catalyst to pro¬ vide, after drying at 100°C and calcining at 550°C for 2 hours, an sorbent material overlayer washcoat of 1 g/in 3 superposed over the Pt/Rh/Al 2 0 3 underlayer. The resulting composition provided an embodiment of the present inven¬ tion comprising a bulk strontium oxide sorbent material overlayer superposed on an underlayer comprising a plat- inum and rhodium-containing TWC catalyst, and was desig¬ nated Catalyst E-2. D. The results of testing Catalysts C-l, E-l, and E-2 under Test Procedure A are compared in Figure 2, which shows that comparative Catalyst C-l does not show any NO sorption and shows some NO χ conversion with a maximum NO reduction at a temperature of about 200°C of the gas stream at the inlet to the test catalyst. (All the tem¬ peratures shown in Figures 2-12 (including Figure 2A) are temperatures of the test gas stream at the inlet to the catalyst member being tested. Reference in this and the following examples to the temperatures at which the events of N0 χ sorption and release occur are to such gas stream inlet temperatures, sometimes referred to simply as "inlet temperature(s)". ) In contrast to the very poor perfor- mance of comparative Catalyst C-l, Catalyst E-l and Cata¬ lyst E-2 comprising embodiments of the present invention showed reduction of N0 χ at an inlet temperature of about 200°C with 20% N0 χ sorption at inlet temperatures between 100 and 150°C, as well as high sorption efficiency in the inlet temperature range of 250 to 400°C. The maximum NO sorption was about 60% at an inlet temperature of 300°C. At inlet temperatures greater than 400°C, NO χ was released as indicated by the negative N0 χ peak between 400 and 550°C. Comparison of Catalyst C-l (Pt/Al 2 0 3 ) with Cata¬ lyst E-l (SrO coated over Pt/Al 2 0 3 ) and E-2 (SrO coated over a TWC catalyst) clearly shows the increase in NO sorption capacity of the SrO coated Catalysts E-l and E-2 as compared to the comparative Catalyst C-l. E. Catalyst E-l was tested in accordance with Test Procedure B which comprises cycling the composition of the feed in a laboratory reactor between (1) rich and (2) lean. The test gas contained 250 ppm NO, 333 ppm C,H (1000 ppm Cl), 50 ppm S0 2 , and 2% steam and was flowed through the catalysts at a space velocity of 25,000/hr while varying the oxygen concentration in the feed from zero (rich conditions) to 10% (lean conditions). The test was performed on a cylindrical cordierite carrier member having 400 cpsi measuring 3/4 inch in diameter and 1 inch in length but otherwise identical to Catalyst E-l and so this Example is also designated Catalyst E-l. The cycle was repeated for two cycles at inlet temperatures of 370 - 390°C and one cycle at inlet temperatures of 470 - 500°C. The results are presented in Figure 2A which shows that at lean conditions and at catalyst inlet temperatures of 370 - 390°C and 470 - 500°C, the N0 χ was sorbed during the lean cycles. After about 10 minutes, the conditions were changed from lean to rich by replacing the 0 2 flow with N 2 and keeping the space velocity fixed. The moment the feed turned rich, a portion of the sorbed NO χ was released as NO χ and a significant amount was reduced to innocuous gases. Example 3 The quantity of 204 g of Sr(N0 3 ) 2 was dissolved in 226 ml of deionized water and the resulting solution was added to 500 g of γ-alumina powder. The thus-impregnated powder was dried at 100°C and calcined at 550°C for 2 hours and allowed to cool. The quantity of 200 g of the SrO impregnated alumina was slurried in 226 ml of deion¬ ized water with 10 g of acetic acid and the mixture was ball milled to a particle size of 90% less than 10 mi- crons. The resulting SrO/Al 2 0 3 slurry was coated onto a sample of Catalyst C-l of Example 1. The coated catalyst was then dried at 100°C and calcined at 550°C for 2 hours to provide an overlayer of 1 g/in 3 . The resulting compo- sition provided an embodiment of the present invention comprising a dispersed (not bulk) SrO sorption material overlayer superposed on an underlayer of Catalyst C-l and was designated Catalyst E-3. Catalyst E-3 was tested in accordance with Test Procedure A and the results are given in Figure 3, which shows that NO χ removal was attained with a peak at an inlet temperature of about 240°C and a release of desorbed NO χ at an inlet temperature of about 420°C. Example 4 The quantity 198 g of Sr(OH) 2 was mixed with 25 g of the same type of alumina as used in Example 1 as a binder and then slurried with 100 ml of deionized water and ball milled to a particle size of 90% of the particles having a diameter of less than 10 microns. The slurry was then coated onto a sample of Catalyst C-l of Example 1. The Sr(OH) 3 and Al 2 0 3 slurry was coated over the Pt/Al 2 0 3 un¬ derlayer of Catalyst C-l. The sample was then dried at 100°C and calcined at 550°C for 2 hours to provide an overlayer of 0.7 g/in 3 . The resulting catalyst provided an embodiment of the present invention comprising a bulk strontium hydroxide sorption material layer superposed on a platinum-containing abatement catalyst, and was desig¬ nated Catalyst E-4. Catalyst E-4 was tested according to Test Procedure A and the results are given in Figure 4. It is clear from the results, which show a removal peak for N0 χ at an inlet temperature of about 280°C that the provision of an over¬ layer Sr(0H) 2 on the Pt/Al 2 0 3 underlayer results in a high NO sorption and reduction capacity. Example 5 Two hundred grams of a slurry of 35% solids of SrO powder in deionized water was mixed with 70 g of CeO powder and deionized water was added to make a 40% solids slurry. The resulting mixture was added to 300 ml of de¬ ionized water and ball milled for 24 hours to provide a particle size of 90% of the particles being less than 10 microns in diameter. This slurry was coated over a sample of Catalyst C-l of Example 1. The coated catalyst was then dried at 100°C and calcined at 550°C for 2 hours to provide an overlayer washcoat loading of 1.3 g/in 3 super¬ posed over the Pt/Al 2 0 3 underlayer of Catalyst C-l. The resulting composition provided an embodiment of the pres¬ ent invention comprising an sorbent material overlayer of a mixture of striontium oxide and bulk ceria superposed on a platinum-containing abatement catalyst and was desig¬ nated Catalyst E-5. Catalyst E-5 was tested using the same gas feed and flow as in Test Procedure A except that the propylene was not included, i.e., no hydrocarbon was included in the feed. The results are given in Figure 5. It is clear from the results that this material showed excellent NO removal, peaking at inlet temperatures of about 180°C and 400°C. NO χ desorption starts at an inlet temperature of about 480°C. Example 6 (Comparative) A soluble platinum salt was added to a ball mill con¬ taining Slip T-l from Part A of Example 2 (Slip T-l con- tains 75 weight % SrO and 25 weight % Al 2 0 3 ) to give 2% by weight Pt dispersed on Slip T-l. This provided 70g/ft 3 Pt in the finished catalyst. The sample was ball milled about thirty minutes, 5% by weight (based on the weight of the slurry) acetic acid was added and the slip was further ball milled to a particle size of 90% of the particles having a diameter of less than 10 microns. The resulting slip was coated onto 400 cpsi cordierite carrier members measuring 0.75 inches in length and 1.0 inches in diame- ter, dried and calcined at 550°C for 2 hours to give 2 g/in 3 of washcoat loading. The resulting comparative sam¬ ple provided a platinum catalytic component dispersed onto the bulk strontium oxide sorbent material, i.e., the plat- inum group metal catalytic component was not segregated from the sorbent material. The resulting comparative catalyst was designated Catalyst C-2. Catalyst testing results using Test Procedure A on comparative Catalyst C-2 and Catalyst E-l of the present invention are shown in Figure 6. It is clear from these results that impregnation of Pt on bulk Sro (as suggested by the Takahashi et al and SAE papers described above) does not give the superior NO χ trapping and reduction per¬ formance which is obtained with Catalyst E-l. In fact, less than 10% NO χ removal is observed over Catalyst C-2 at inlet temperatures of from about 150 - 600°C, indicating that mixing of the catalytic and trapping functions by supporting the platinum catalytic metal component on the strontium oxide sorption material results in very poor efficiency for NO χ removal. Example 7 (Comparative) Activated alumina having a BET surface area of about 150 g/m 2 was impregnated with an aqueous solution of strontium nitrate. The impregnated powder sample was dried at 120°C overnight and then calcined by heating from ambient temperature to 600°C over a two-hour period and then held at 600°C for an additional four hours to provide alumina containing 20% by weight (calcined basis) SrO. An aqueous slip of 35% solids was made from the resulting NO sorbent material powder by adding the powder to deionized water to which sufficient platinum was added using an aqueous solution of a soluble platinum salt to provide 2% by weight Pt in the calcined product. Samples were pre- pared by coating 400 cpsi cordierite carrier members to give 2 g/in 3 of washcoat loading after calcination at 550°C for 2 hours (i.e., 70 g/ft 3 Pt) . The resulting com¬ parative catalyst had the platinum catalytic metal compo- nent impregnated onto the same (alumina) support particles onto which the dispersed strontium oxide (via calcination of strontium nitrate) sorbent material was dispersed. Thus, the catalytic metal component, in this case a plat- inum catalytic metal component, was not segregated from the NO χ sorbent material as required by the present in¬ vention. This comparative catalyst was designated Cata¬ lyst C-3. Catalyst testing results using Test Procedure A were carried out on comparative Catalyst C-3, along with Cata¬ lyst E-l of the present invention and the results are shown in Figure 7. Catalyst E-l is seen to remove NO over a broad inlet temperature range of from about 150 - 400°C with NO χ release above this temperature, whereas Catalyst C-3 shows only minor, less than 15%, NO χ removal at an inlet temperature range of from about 150 - 300°C and correspondingly much lower NO χ release at higher tem¬ peratures. Thus, as also shown in Example 6, failure to segregate the platinum catalytic metal component and the strontium oxide NO χ sorbent material component in the manner required by the teachings of the present invention, in this case by supporting both species on the same Al 2 0 3 particles, results in poor N0 χ removal efficiency. As noted elsewhere herein, this is contrary to the teachings of the Takahashi et al and SAE papers noted above. Example 8 A. Mixed E-l Seventy-five ml of Slip A of Part A of Example 1 di- luted with deioninzed water to 37.2% solids, and 45.3 ml of Slip T-l of Part A of Example 2 diluted with deionized water to 30.8% solids were thoroughly mixed together. The resulting slip was used to coat 400 cpsi cordierite carri¬ er members to give 3 g/in 3 of washcoat loading after cal- cination at 550°C for 2 hours to provide a catalyst having 70 g/ft 3 Pt. The result is a "mixed" version of Catalyst E-l in which the NO v abatement catalyst and the NO„ sorp- tion material are not in discrete layers but are mixed in a single layer. The resulting sample is designated Cata¬ lyst E-1M, the "M" standing for mixed. B. Reverse E-l Slip T-l of Part A of Example 2 was coated as an un¬ derlayer on 400 cpsi cordierite carrier members to give 1 g/in 3 washcoat after calcination at 550°C for 2 hours. These carrier members were then further coated with 2 g/in 3 of Slip I as an overlayer containing 70 g/ft 3 of platinum and further calcined at 550°C for 2 hours. The result is a version of Catalyst E-l in which the layers are reversed relative to Catalyst E-l, i.e., the NO χ sor¬ bent material is the underlayer and the NO χ abatement catalyst is the overlayer. The resulting sample is desig- nated Catalyst E-1R, the "R" standing for reversed. Figure 8 shows the results of testing Catalysts E-l, E-1M and E-1R using Test Procedure A. Clearly from these results a layered structure with the N0 χ trapping compo¬ nent on the overlayer and the N0 χ abatement catalyst on the underlayer is preferred. It must be noted however that adequate NO χ trapping and conversion is observed with the other two materials as well. Nonetheless, it is pre¬ ferred to have the NO χ sorbent material and the NO χ abate¬ ment catalyst disposed in the layered structure exempli- fied by Catalyst E-l, wherein the N0 χ abatement catalyst is the underlayer. Example 9 A comparative material was made containing only the NO χ sorbent material, as follows. Slip T-l of Part A of Example 2 was coated onto a 400 cpsi cordierite carrier member which was then calcined at 550°C for 2 hours to give a 1 g/in 3 washcoat. The resulting comparative was designated Catalyst C-4. In Figure 9, N0 χ removal over Catalyst E-l and com¬ parative Catalyst C-4 is compared using test conditions similar to those used in Test Procedure A except that no reductant is present. Because of the absence of hydrocar- bons (or other reductant) in the feed gas, the NO χ remov¬ als shown in this Figure result from NO χ trapping alone, there being no NO X v conversion, i.e., reduction of NOX„ by** a reductant. Clearly from these results it is shown that the platinum group metal catalytic component in the under¬ layer of Catalyst E-l, plays a role in promoting NO χ sorp¬ tion by the N0 χ sorbent material, i.e., strontium oxide in this case. Very little N0 χ removal by comparative Cata¬ lyst C-4 is observed, i.e., less than 5% above an inlet temperature of 150°C, whereas the data for Catalyst E-l show two NO χ removal peaks at inlet temperatures of about 150°C and about 360°C, each with over 30% NO χ removal. At higher inlet temperatures, about 400 - 575°C, a corre¬ spondingly large N0 χ desorption peak is shown for Catalyst E-l. Example 10 A calcined cordierite catalyst core, 400 cpsi, had a washcoat of 2 g/in 3 deposited from Slip A of Part A of Ex- ample 1 as an underlayer. An overlayer of 1 g/in 3 was ap¬ plied using a slip prepared with 150 g Ba 2 Sr0 6 , 50 g Al 2 0 3 , 31 g A-20 Nalco alumina binder (20% solids) and 180 g of deionized water. The resulting layered material was calcined to 550°C for 2 hours. The resulting catalyst is designated Catalyst E-10. Catalyst E-10 was tested according to Test Procedure A for activity for NO χ reduction and trapping and the test results are given in Figure 10. Clearly this material is active for both NO χ conversion and sorption over a fairly broad inlet temperature range of 100 - 400°C and releases NO χ above an inlet temperature of about 400°C. Example 11 Lean/Rich Testing Catalysts E-l and E-10 were tested in an alternating rich/lean environment under the following conditions at the data point temperatures shown in Figures IIA and llB. Thus, the data plotted in Figure llA were developed at inlet temperatures ranging from 200°C to 450°C at 50°C intervals and the data plotted in Figure llB were devel¬ oped at inlet temperatures of from 150°C to 500°C at 50°C intervals. Space Velocity = 25,000/h The inlet temperature was held steady for one-half hour at each of the temperatures shown in Figures llA (200 - 450°C, at 50°C intervals) and 11B (150 - 500°C, at 50°C intervals) . Composition of Inlet Gas NO = 250 ppm H 2 0 ■= 10% CO = 1,000 ppm C 3 H 6 - 16.7 ppm S0 2 = 50 ppm H 2 -= 330 ppm 0 2 = 0.07% (rich modes) <—> 6.0% (lean modes) The frequency of cycling between lean and rich modes was 60 seconds in each mode. Preconditioning of the test catalysts was carried out for about 30 minutes by subject- ing the catalysts to the 60-second lean and rich periods at each test temperature. The results obtained for lean/- rich testing of preconditioned Catalysts E-l and E-10, are plotted in, respectively. Figures IIA and 11B. In these Figures the vertical lengths of the bars represent the range of NO χ sorption observed during the lean pulses. The percentage of NO χ removal at the start of a lean cycle is shown by the top of each vertical bar in Figures llA and llB, and the percentage of NO χ removal at the end of each lean cycle is shown by the bottom of each vertical bar. The cyclic way in which the test was run ensures that during rich operating periods the catalyst was cleaned of stored N0 χ so that NO χ sorption could occur again in the next lean operating period. Clearly, both Catalyst E-l and Catalyst E-10 demonstrated the ability to sorb N0 χ over a broad temperature range for an extended period of time with alternating periods of rich and lean operation. Example 12 A. A catalyst sample was prepared identically to Cata¬ lyst C-l of Part B of Example 1, the sole difference being that the washcoat loading of the calcined catalyst was 1.67 g/in 3 . B. An alumina slurry made of activated alumina was ball milled to 90% of the particles being less than 10 microns in diameter using 5% acetic acid in the slurry. The slur¬ ry contained 35% solids based on dried weight. The alumi¬ na was then coated over the catalyst obtained in Part A of this Example 12. The catalyst was then dried at 100°C and calcined at 550°C for 2 hours to provide 0.6 g/in 3 of an alumina washcoat layer in the calcined sample. C. The calcined catalyst obtained from Part B of this Example 12 was then coated with Slip T-l from Part A of Example 2. The coated catalyst was then dried and calcin- ed at 550°C for 2 hours to give a N0 χ sorbent material overlayer of 0.7 g/in 3 . The total washcoat loading of the resulting three-layered catalyst was 3 g/in 3 , having a NO χ abatement catalyst underlayer of platinum dispersed on alumina, an intermediate layer of alumina, and an over- layer of NO χ sorbent material comprised of bulk strontium oxide and bulk alumina. This catalyst was designated Catalyst E-12. Catalyst E-12 was tested according to Test Procedure A. The results are plotted in Figure 12 and clearly show that even with an intermediate layer separating the NO χ sorbent material overlayer from the N0 χ abatement catalyst underlayer, catalyst E-12 demonstrated good efficiency of sorbing and converting NO χ . Note the high NO χ removal at inlet temperatures from about 275°C to 350°C. Sorbed NO χ was released at temperatures greater than 375°C. While the invention has been described in detail with respect to specific embodiments thereof, it will be appre¬ ciated that numerous variations to the specific embodi¬ ments may well occur to those skilled in the art upon a reading and understanding of the foregoing and it is in¬ tended to embrace such variations within the scope of the appended claims.

Claims: THE CLAIMS What is claimed is: 1. A composition for NO χ abatement in a gas stream, the composition comprising a NO χ abatement catalyst and a NO χ sorbent material disposed in proximity to each other on a common refractory carrier member; the NO χ abatement catalyst comprising a catalytic metal component comprised of a platinum catalytic metal component, the catalytic metal component being dispersed on a first refractory catalyst support material; and the NO χ sorbent material comprising at least one basic oxygenated metal compound which is segregated from the catalytic metal component at least to the extent that (a) when the NO χ sorbent material is dispersed on a re¬ fractory support material, the catalytic metal component and the NO χ sorbent material are not dispersed on the same increment of refractory support material, and (b) when the N0 χ sorbent material is in bulk form, the catalytic metal component is not impregnated into the bulk NO χ sorbent material. 2. The composition of claim 1 wherein the NO χ sor¬ bent material is selected from the group consisting of one or more of metal oxides, metal carbonates, metal hydrox¬ ides and mixed metal oxides. 3. The composition of claim 1 or claim 2 wherein the NO χ sorbent material further comprises ceria. 4. The composition of claim 1 or claim 2 wherein the NO χ sorbent material further comprises bulk ceria. 5. The composition of claim 1 or claim 2 wherein the catalytic metal component further comprises at least one other catalytic metal component in addition to the plati¬ num catalytic metal component. 6. The composition of claim 1 or claim 2 wherein the catalytic metal component further comprises at least one other platinum group metal catalytic component in addition to the platinum catalytic metal component. 7. The composition of claim 1 wherein the NO χ sor¬ bent material comprises a mixed metal oxide selected from the group consisting of one or more of barium strontium tungstate, barium strontium niobate, strontium titanate, barium zirconate, barium silicate and barium strontium ti¬ tanate. 8. The composition of claim 1 wherein the NO χ sor¬ bent material is selected from the group consisting of one or more of metal oxides, metal hydroxides, metal carbon¬ ates, and mixed metal oxides, wherein the metals of the metal oxides, metal hydroxides and metal carbonates and at least one of the metals of the mixed metal oxides are sel¬ ected from the group consisting of one or more of lithium, sodium, potassium, rubidium, cesium, magnesium, calcium, strontium and barium. 9. The composition of claim 1 wherein the refractory support material comprises a refractory metal oxide, and the NO χ sorbent material is selected from the group con¬ sisting of one or more of oxides and hydroxides of one or more of magnesium, calcium, strontium and barium. 10. The composition of claim 1 or claim 2 wherein the NO χ abatement catalyst is admixed with the NO χ sorbent material. 11. The composition of claim 1 or claim 2 wherein the N0 χ abatement catalyst is disposed as a first discrete layer on the refractory carrier member and the NO sorbent material is disposed as a second discrete layer on the refractory carrier member. 12. The composition of claim 11 wherein the first discrete layer comprises an underlayer disposed on the carrier member and the second discrete layer comprises an overlayer superposed on the underlayer. 13. The composition of claim 11 wherein the first discrete layer and the second discrete layer are in direct contact one with the other. 14. The composition of claim 11 wherein the first discrete layer and the second discrete layer are separated by an intervening layer of material. 15. The composition of claim 11 wherein the refrac¬ tory carrier comprises a body having a plurality of gas flow passages extending therethrough, the passages being defined by passage walls, and the first and second layers are disposed on the passage walls. 16. The composition of claim 11 wherein the refrac¬ tory carrier comprises a body of carrier beads retained within a gas-permeable container. 17. The composition of claim 16 wherein the first layer is disposed on one increment of carrier beads and the second layer is disposed on a second increment of car¬ rier beads, and the first and second increments of carrier beads are admixed within the container. 18. The composition of claim 16 wherein the first and second layers are disposed on the same increment of carri¬ er beads. 19. The composition of claim 1 wherein the NO sor¬ bent material comprises strontium oxide. 20. A composition for NO χ abatement in a gas stream comprising: a refractory carrier member comprising a body having a plurality of gas flow passages extending there¬ through, the passages being defined by passage walls; a NO χ abatement catalyst comprising a catalytic metal component comprised of a platinum catalytic metal component, the catalytic metal component being dispersed on a refractory metal oxide support, the abatement cata¬ lyst being disposed on the passage walls as a first dis¬ crete layer; and a N0 χ sorbent material comprising a bulk oxide selected from the group consisting of one or more of ox¬ ides of magnesium, calcium, strontium and barium, the NO χ sorbent material being disposed on the passage walls as a second discrete layer. 21. The composition of claim 20 wherein the NO χ abatement catalyst further comprises at least one other platinum group metal component to the platinum catalytic metal compound. 22. The composition of claim 20 or claim 21 wherein the first discrete layer comprises an underlayer disposed on the carrier member and the second discrete layer com¬ prises an overlayer superposed on the underlayer. 23. The composition of claim 20 wherein the NO sor¬ bent material further comprises ceria. 24. The composition of claim 20 or claim 21 wherein the N0 χ sorbent material comprises bulk strontium oxide. 25. The composition of claim 20 or claim 21 wherein the N0 χ sorbent material comprises bulk strontium hydrox¬ ide. 26. A method of NO χ abatement comprising contacting a gas stream containing NO χ with a N0 χ abatement composi¬ tion, the composition comprising a NO χ abatement catalyst and a NO χ sorbent material disposed in proximity to each other on a commmon refractory carrier member, (i) the NO χ abatement catalyst comprising a catalytic metal component comprised of a platinum catalytic metal component and, op¬ tionally, at least one other platinum group metal catalyt¬ ic component, the catalytic metal component being dispers¬ ed on a first refractory metal oxide support, (ii) the NO sorbent material optionally being a bulk material and com¬ prising at least one material selected from the group con¬ sisting of basic oxygenated metal compounds and, optional¬ ly, further comprising ceria, and (iii) wherein the NO χ sorbent material is segregated from the catalytic metal component, at least to the extent that (a) when the NO χ sorbent material is dispersed on a refractory support ma¬ terial, the catalytic metal component and the NO χ sorbent material are not dispersed on the same increment of re¬ fractory support material, and (b) when the NO χ sorbent material comprises a bulk material, the catalytic metal component is not impregnated into the bulk NO χ sorbent material; the method including periodically adjusting the composition of the gas stream between lean and stoichio¬ metric/rich conditions to thereby provide alternating lean operating condition periods and stoichiometric/rich oper¬ ating condition periods, and maintaining NO χ abatement conditions during the stoichiometric/rich operating con¬ dition periods, whereby during the lean operating periods NO χ is sorbed by the NO χ sorption material and during the stoichiometric/rich operating periods the NO χ abatement catalyst promotes the reduction of NO χ . 27. The method of claim 26 wherein the NO χ sorbent material comprises a mixed metal oxide selected from the group consisting of one or more of barium strontium tung¬ state, barium strontium niobate, strontium titanate, bari- um zirconate, barium silicate and barium strontium titan¬ ate. 28. The method of claim 26 wherein the N0 χ sorbent material is selected from the group consisting of one or more metal oxides, metal carbonates, metal hydroxides and mixed metal oxides, wherein the metals of the metal ox¬ ides, metal carbonates, metal hydroxides and at least one of the metals of mixed metal oxides are selected from the group consisting of one or more of lithium, sodium, potas¬ sium, rubidium, osmium, magnesium, calcium, strontium and barium. 29. The method of claim 26 wherein the N0 χ abatement catalyst further comprises at least one other platinum group metal catalytic component and the N0 χ sorbent mate¬ rial is selected from the group consisting of one or more of oxides of magnesium, calcium, strontium and barium. 30. The method of claim 26 wherein the N0 χ sorbent material comprises strontium oxide. 31. The method of claim 26 wherein the NO χ abatement catalyst is disposed as a first discrete layer on the re¬ fractory carrier member and the N0 χ sorbent material is disposed as a second discrete layer on the carrier member. 32. The method of claim 31 wherein the first discrete layer comprises an underlayer disposed on the carrier mem¬ ber and the second discrete layer comprises an overlayer superposed on the underlayer.

Inventors: DEEBA MICHEL, FARRAUTO ROBERT J, FEELEY JENNIFER S, DEEBA, MICHEL, FARRAUTO, ROBERT, J., FEELEY, JENNIFER, S.
Applicants: ENGELHARD CORP, ENGELHARD CORPORATION
Application year: 1996
Main classification: B01D53
IPC codes: B01D53, B01J23