Use of oxygen in excess in fuel combustion gives high combustion efficiency and accordingly, specific fuel consumption, raw emissions, and the temperature of exhaust gases are low. An excess of air also lowers the temperature of exhaust gases since such excessive air is always accompanied by a corresponding amount of inert nitrogen diluting such exhaust gases. The temperatures of exhaust gases from diesel engine cars in city traffic range between 100 and 250°C, being even under 150°C for extended periods. While raw emissions are relatively low in comparison to cars using gasoline, an oxidation catalyst for e. g. diesel engine- driven passenger cars should work at said temperature range with respect to carbon monoxide and hydrocarbon conversion of above 60-80% to attain emission limits. Moreover, inefficient oxidation of hydrocarbons also increases particle amounts. Depending on the conditions in diesel exhaust gases, the conversion of nitrogen oxides is between 0 and 20% using a so-called four-way catalyst (CO, HC, NOx, particles). In diesel oxidation catalysts, Pt having the highest resistance to sulfur is normally used as the active metal. If possible, the catalysts are placed for heat recovery as close to the engine as possible (CC = Closed Coupled), and not under car bodies (UF = under Floor). Since catalysts at CC positions can't be too massive and the operation of the catalyst at low temperatures largely depends on the volume thereof, new diesel cars often have a small catalyst close to the engine and a larger one further there from.

Moreover, many industrial power plants and factories produce emissions (hydrocarbon, nitrogen, oxygen containing hydrocarbon, and sulfur compounds) that can be oxidized with a catalyst to less harmful substances. Said compounds can also contain other atoms such as halogens. For instance in many industrial processes, volatile organic compounds (VOC) are a major emission source (solvents, flue gases, sulfides, organic sulfides, ammonia, organic compounds with nitrogen). Oxidation catalysts in effluent gas conduits should work very efficiently already at low temperatures. Hydrocarbons and compounds of sulfur and nitrogen are converted to corresponding oxides.

Many oxide based catalysts have been developed, purely alumina, silica, or titania based catalysts containing metals of the Pt-group (Pt, Pd, Rh) being most conventional. For instance, an oxide mixture is made from stabilized TiO2 and Si- sol (US 5,580, 533), or from a mixture of TiO2, Si02, Al203, and Zr02 (EP 0694332). Experience has, however, shown that catalysts containing solely other active metals than Pt or Pd are not sufficiently stable under actual exhaust gas conditions. Typically in noble metal catalysts, several promoters are used for further lowering the light-off temperature and for stabilizing the catalyst against thermal or chemical deactivation. A support mixture containing ceria and another oxide (titania, zirconia, Ce-zirconia, silica, alumina-silica, or alpha-alumina) is said to be an active oxidation catalyst (WO 93/10885). Also Si (EP 0377290), Ti (JP 4087627), Si-Ti based (US 5,145, 825) catalysts with less accumulation of sulfates in comparison to alumina based catalysts were used in the eighties and nineties when sulfur levels were very high in diesel fuels. Al-Ce based catalysts resembling three-way catalysts are also widely used as oxidation catalysts (WO 9310886, US 4,782, 038). However, the light-off temperatures of any oxide based catalysts are not sufficient for the latest diesel engine cars producing very cold exhaust gases.

Especially the amount of hydrocarbons accumulating in particles is said to be reduced by using catalysts containing various acid zeolites such as faujacite, pentasil or mordenite, and comprising heavier transition elements as active metals (DE 0449931). Similarily, zeolite Y containing noble metals (EP0596552), La, Ce, or Ca (EP 0508 513) are used for lowering hydrocarbon loads in exhaust gases.

While hydrocarbons and CO are effectively oxidized, sulfate formation can be lowered by adding V, or La to a Pt based oxidation catalyst (EP 0734756).

Several references disclose examples of catalysts containing zeolites (EP 0499286), or oxides (EP 0498 325) for catalyzing NOx reduction under lean conditions. Active agents including Cu, Ce, Mn, Co, Ag, Ga, Zr, Cr, or Pd are added to said zeolites. The zeolites can further contain a promoter, such as a transition metal, like La. In practice, the service life of such zeolite based catalysts in the presence of SO2, and other catalyst poisons was usually too short, or the additional fuel injection they require was too high.

By assembling various deNOx catalysts containing Pt in series in the cascading order of an operation window, a wide NOx operation window can be obtained while hydrocarbons act as reducing agents (US 5,294, 421). With respect to support

materials, said operation window cascades for Pt catalysts in the following order: Ti20, Ce02, Zr02, Ai203, that is, Pt/A ! 203 has the lowest light-off temperature.

For four-way catalysts, the concept of catalysts containing zeolites that adsorb HC, and a deNOx catalyst containing mainly Pt, the nitrogen oxides being reduced by HC, is also utilized (WO 9639244). The HC adsorbent is said to desorb HC in the temperature range from 190 to 250 °C.

Prior art (WO 9401926) also describes a diesel oxidation catalyst with zeolite and a support containing ceria, zeolite, and platinum in addition to alumina. The zeolite can contain a metal of the Pt group. The role of the zeolite is to assist in hydrocarbon oxidation, adsorption and cracking. Another similar catalyst contains a metal of the Pt group in an oxide based support with V, Au, Fe and thermally stable ceria, and non-catalytic, porous zeolite as a promoter, for instance beta, pentasil, or mordenite (WO 97 00119) being suitable zeolites.

For lean conditions, prior art also describes an oxidation catalyst with noble metals containing zeolite and alumina, comprising a compound of Si, Ba, La or Zr as a stabilizer. The weight ratio of alumina to zeolite ranges between 9: 1 and 1 : 9 (Fl 98274). EP 0800856 describes a similar catalyst made from zeolite, a metal of Pt group, and a metal oxide, this metal oxide being Al silicate, alumina, or titania. In EP 0566878, a catalyst composed of aluminium oxide, titanium oxide, silica, and zeolite is produced in an alcoholic solution. In the catalyst of WO 9722404, an acid or basic zeolite (beta, mordenite, or pentasil) is also combined with an oxide based Pt catalyst.

A four-way catalyst (WO 9850151) is produced from an oxide based support containing noble metals, said support comprising two different zeolites, one of which contains a noble metal (Pt or Rh). First one of said zeolites was pentasil, mordenite, zeolite Y, or beta-zeolite without any noble metal. Pore size was at least 5 A, with a Si: AI ratio of more than 5. The other zeolite was ZSM-5 added with a noble metal.

Regular porous structures and sizes of zeolitic structures have been utilized for producing a catalyst where HCs with longer chains are sterically hindered from occupying the active site of the oxidation catalyst, thus lowering the total oxidation rate of reducing compounds while the amount of reducing agents remains sufficiently high for reducing nitrogen oxides (WO 0020400). Examples use Pt ferrierite (oxidation), and Ag-mordenite (deNOx) catalysts.

Zeolites are natural, or synthetic crystalline aluminosilicates with a regular porous structure, said porous structure, however, varying among different zeolite types.

This property can be utilized for producing shape specific catalysts where the molecules that can enter the pores are limited by the shape and size thereof.

Basic structural unit of zeolites, alumina tetrahedron, needs a positively charged monovalent (+1) cation to be electrically neutral. For this reason, cations normally attach to the aluminium site during ion exchange. After the production, the cation present in the zeolite is normally sodium, or hydrogen. Silicon tetrahedron is electrically neutral. However, using ion exchange methods, it is easy to exchange them for other cations endowing the zeolites with catalytic properties (Gates et al., Chemistry of Catalytic Processes, McGraw-Hill 1979). In ion exchange, cations are usually adsorbed by zeolites from aqueous solutions, followed by drying and calcinating under suitable conditions. Pore size, pore volume, and surface properties vary between different zeolites. The composition of the basic zeolite structure is commonly described by Si: Al2 molar ratio influencing not only the zeolite structure but also hydrophobicity/hydrophilicity, acidity, and stability under various circumstances, and the amount of the desired cation that can be incorporated to the zeolite by ion exchange. With hydrophobic zeolites having high Si: AI2 ratios, hydrocarbons can be removed from effluent gases at low temperatures. Typical zeolite types used in emission catalysts include ZSM-5 (MFI), mordenite (MOR), beta (BEA), Y (FAU), and ferrierite (FER). The zeolites used in modern catalysts are normally synthetic having above designations accompanied by names (above in parenthesis) describing the structure of the corresponding natural zeolite. The pore size of zeolites, and the molecular sizes of different hydrocarbons vary in the same range. For instance higher aromatic hydrocarbons must be cracked before they fit into the pores of ZSM-5. The pore size of ferrierite is so small that even many light hydrocarbons are too large for the pores thereof. Zeolite Y has a three-dimensional pore structure with clearly fine pores, comprising also large pores between the structure. The smallest molecules such as NO, CO, hydrogen and oxygen are, however, sufficiently small to enter into the pores of all above zeolites. Pore size and surface properties are also important for the production of the catalyst during the addition of the active components as various dissolved compounds by ion exchange or impregnation.

General disclosure of the invention The object of the invention is to provide an oxidation catalyst and NOx reduction catalyst for applications containing oxygen, and sulfur compounds in excess, said

catalyst being stable under operation conditions and having an operation temperature, which is as low as possible. For attaining said objects, the invention is characterized by features presented in the independent claims. Other claims describe some preferable embodiments of the invention.

Compared to normal oxidation catalysts, the catalyst of the invention has high activity with respect to the reduction of nitrogen oxides, that is, the catalyst acts as a four-way catalyst (CO, HC, NOx, PM). With superior oxidation catalysts, high conversion is obtained for hydrocarbons that are volatile in the catalyst under operation conditions. Under these circumstances, the total amount (mass) of particles for passenger cars can be lowered by 10-50% depending on the conditions in NEDC (New European Driving Cycle).

NH3 or compounds containing nitrogen (e. g. ammonium, amine and nitrous compounds, organic nitrogen compounds) react in the catalyst of the invention to produce for instance nitrogen and nitrogen oxides.

The catalyst of the invention can also be a part of a system, or a method for removing e. g. nitrogen oxides and particles. In addition to the catalyst of the invention, the system can also comprise for instance a catalyst for removing NOx (such as SCR catalyst, NOx adsorption catalyst/NOX decomposition catalyst), or a particle separator (particle filter, electrostatic separator, cyclone, etc. ).

According to an embodiment of the invention, the catalyst contains a first zeolite, Ce compound, Ce promoter selected from the group consisting of Zr, Ti, Nd, Mn, Co, Pr, Nd, and Pt and/or Rh and/or Pd and/or Ir as an active metal dispersed in the catalyst.

According to another embodiment of the invention, the catalyst contains a second zeolite, the structure, type and/or Sisal2 ratio thereof differing from that (those) of the first zeolite. According to another embodiment of the invention, the catalyst contains a third zeolite, the structure, type and/or SiAI2 ratio thereof differing from that (those) of the first and the second zeolites.

The invention is based on the combination of a catalyst material containing aluminium oxide with one or several zeolites as discrete particles, coarse cerium oxide or mixed Ce oxide, as well as finely or coarsely divided metal, for instance as an oxide. The finely divided metal is dispersed on the surface of the aluminium oxide and/or zeolite. One or several of the zeolites can be added with an active metal, normally Pt.

The invention can be used in mobile or stationary applications for exhaust, flue and effluent gases, the gaseous mixture containing oxygen constantly or on an average in excess. Any gaseous (for instance methane, propane), liquid (light or heavy fuel oil, diesel, gasoline) or solid fuel can be used for combustion. Effluent gases can contain e. g. hydrocarbons (VOC, solvent emissions, fumes) and compounds of sulfur (H2S, organic sulfides or mercaptans), nitrogen (NH3, organic nitrogen compounds), or halogens (organic Cl, F, Br, I compounds).

The concentration of the Ce compound is typically in the range of 0, 1-99%. It can preferably be 140% such as 5-20%, 10-30%.

The catalysts of the invention comprises at least one zeolite of the ZSM-5, Beta, Y, ferrierite and/or mordenite type. Mean Si: AI2 can preferably vary from 1 to 1000, such as preferably from 2 to 500. The zeolite can also contain titanium, e. g. TS-1.

According to an embodiment of the invention, one or several of the zeolites can be added with (for instance by ion exchange or impregnation) metals of the invention, such as preferably with Pt and/or Pd, Ir and/or Rh. The specific surface area of the zeolites is usually very high (more than 350 m2/g), and thus the total surface area of the catalyst can be increased therewith. The zeolite can be a synthetic or a corresponding natural Al silicate. According to an embodiment of the invention, at least one of the active metals Pt and/or Rh and/or Pd and/or I r is on the surface of the Ce compound.

According to an embodiment of the invention, in the combination of two or more zeolites, the Si: AI2 of at least one of the zeolites can be less than 55 and that of at least one of the other zeolites can be more than 55. For exhaust catalysts, hydrothermal stability of the zeolites used is as high as possible. The use of hydrophobic zeolites adsorbing hydrocarbons is advantageous for HC conversion and light-off of the catalyst. The zeolite with Si: A ! z < 55, is preferably added with Pt, preferably to a concentration of 0.05-3%, such as 0.1-1%. The zeolite with Si: AI2 ! 55, is preferably added with Pt, preferably to a concentration of 0.05-3%, such as 0. 1-3%. The zeolite is preferably added with Pt corresponding to the ion exchange ratio of 100% with respect to Al.

In the combination of two or more zeolites, at least one of the zeolites (Beta, Y) can comprise larger (>0.6 nm) pores, and at least another one of zeolites (ZSM-5, ferrierite) can comprise small or medium (< 0.6 nm) pores. Zeolites can also have both large and small pores (mordenite). The shape, structure and the art of the junctions of the channels can vary between the zeolites. According to an

embodiment of the invention, the mean diameter of the pores in the first zeolite is <0.6 nm and that of the second zeolite ! 0.6 nm.

In the combination of two or more zeolites, at least one of them (e. g. Beta) can desorb adsorbed hydrocarbons at high temperatures, and at least another one of zeolites (e. g. ZSM5) can desorb hydrocarbons at considerably lower temperatures in comparison thereto.

Instead of normal Al-Si-zeolites, also metal silicates containing in the zeolite structure, at Al site, another sufficiently stable metal such as Ti, Co, Ga, In, Co, Mn, Zn, Cu, Cr or Fe can be used. In this case the silicate raw material is free of aluminium, this being a substantial difference with respect to normal zeolites. A promoter described above can also be added to these metal silicates.

One of the zeolites can be added with catalytically active metal (e. g. Pt, Pd, Rh), or an oxide thereof, the other zeolite being present in the catalyst as such. One of the zeolites (e. g. Beta (300) or Y (80) ) can be added with Pt to a high concentration (> 1%), and the other zeolite (ZSM5 (33), ZSM5 (59), Beta (25), ferrierite (20) ) with Pt to a low concentration (< 1%). High concentration corresponds for instance to an ion exchange degree of above 100%, or the latter to an ion exchange degree of below 100%. In this way, HC-adsorption and light-off reaction can simultaneously be promoted by the zeolites in the catalyst.

For applications containing unsaturated hydrocarbons (such as methane, ethane, propane), one of the zeolites can be added with Pd and the other with Pt, or both of them can be impregnated into the final catalyst. This provides a catalyst having a high HC light-off, CO light-off, and stability as well as NOx conversion (CH4- SCR).

One or more of the zeolites can preferably be added with a first promoter by ion exchange for increasing HC adsorption capacity, HC adsorption stability (thermal and sulfur) during ageing, or change the desorption temperature of adsorbed HC.

For zeolites with very high desorption temperatures (Beta), the desorption temperature can be lowered by suitable promoters, thus causing the desorption in the light-off temperature range of the catalyst. Since the zeolites have a very high adsorption capacity, there is a risk for the zeolite pores to be filled with the intermediates of the hydrocarbon oxidation, thus reducing the advantage attained with the zeolites in the reactions. In this case, the first promoter in the zeolite

structure (e. g. Ce, Ti, Mn, Fe) immediately promotes the oxidation of hydrocarbons and CO to form water and carbon dioxide.

Pure aluminium oxide having a high surface area, optionally stabilized with metals presented in the invention by dispersing them in advance in the catalyst is used in the catalyst. The specific surface area of aluminium oxide is typically above 100 m2lg, preferably from 200 to 300 m2/g, and even more than 300 m2/g.

In the catalyst, the cerium oxide or a mixture of Ce and Ce promoter oxides is present in the support material as particles larger than 0.4 um, the mean particle size being preferably between 1 and 10 um. Thus, the hydrothermal stability and sulfur resistance of the catalyst, as well as HC and NOx conversions are substantially higher than for catalysts comprising cerium dispersed as small particles on the surface of alumina. It is added to the catalyst in the slurry step as a powder or from e. g. a sol onto the catalyst surface, thus producing large particles. The compound of Ce can be evenly distributed in the whole support, or it can be present in one of several superimposed layers. If cerium oxide is present as accumulated clusters, the noble metal, or the dispersing promoter metals can be adsorbed more readily into the pure aluminium oxide.

Mixed oxide of Ce is prepared before coating of the catalyst, for instance by precipitation, sol gel technique, or using other similar methods. For instance Mn, Ti, Zr, Pr, La, Co, Ni, Cu, Ca, Sr, Sc, Nb, Nd or Gd can be added to Ce as the Ce promoter. Moreover, said mixed oxide can be a tri-or multicomponent mixture consisting of said elements, such as Mn-Zr-Ce, Mn-Nb-Ce, Ti-Zr-Ce, Ti-Nb-Ce, Mn-Ti-Ce, Pr-Ti-Ce, Pr-Mn-Ce or Co-Mn-Ce. Such mixed oxides form known natural or synthetic crystal structures. Said mixed oxides can also contain At.

The first promoter is preferably present in the catalyst in highly dispersed state (dso < 0.4 um), for instance in metallic form, as an oxide, nitrate, carbonate, or as other similar compounds or mixtures thereof. It can be added to the aluminium oxide, or zeolite beforehand during the production, for instance by precipitation, impregnation, ion exchange, or sol gel technique. The first promoter can be present in the structure of alumina, or adsorbed on the surface thereof. The first promoter can be adsorbed to the Al site in the zeolite structure, or it can replace Al in zeolite (corresponding metal silicate). The first promoter can preferably be on the surface of the zeolites or within the structure thereof. The first promoter can either be evenly dispersed throughout the whole catalyst structure, on the second promoter, or also preferably on the Ce compound. The first promoter can also be

Ce, the catalyst thus containig Ce in two different forms, that is, as large particles and dispersed either evenly throughout the catalyst, or in one of the catalyst components. The first promoter can preferably be Sc, Ti, Cr, Mn, Fe, Co, Cu, La, Au, Ag, Ga, In and/or Ce.

According to an embodiment of the invention, the catalyst also comprises a second promoter. The second promoter is preferably Ti, V, Cr, Mn, Mo and/or W.

According to an embodiment of the invention, the particle size of the second promoter in the support is ! 0.4 pm. The second promoter forms in the catalyst support a respective major unitary phase, for instance as large (dso : 0.4 pm) metal, oxide, nitrate, carbonate, sulfate particles, or a mixture thereof. It is added to the catalyst in the slurry step as a powder, or e. g. from a sol onto the catalyst surface, thus producing large particles when the particle size in the sol is sufficient.

The second promoter can be evenly present in the whole support, or it can be incorporated in one of several superimposed layers. The dispersed first promoter and active metals can be partly or totally on the second promoter. The second promoter consists of compounds of Ti, V, Cr, Mn, Mo or W, or mixtures thereof.

According to an embodiment of the invention, the catalytically active metal is added to the catalyst, or to some starting materials thereof by using at least two different starting complexes in the impregnation solution and/or by using different impregnation methods.

According to an embodiment of the invention, the catalyst comprises two or more separate catalyst parts, respectively coated with catalysts of the invention, or parts thereof having different compositions or layer thicknesses. Preferably, the first catalyst part is added with Ce oxide and/or Ce promoter, whereas the second catalyst part is not added with with Ce oxide and/or Ce promoter. Preferably, the first catalyst part comprises the first promoter, and the second catalyst part comprises the second promoter. The first catalyst part preferably contains Pt, and the second catalyst part contains Rh, Pd and/or Ir. It is also possible to make a catalyst, the first and the third parts of which are identical, the second catalyst part being different with respect to the composition and/or structure. It is also possible to make a catalyst of the invention, the first and the third parts of which have identical structures but different compositions. The second catalyst part can be consistent with the first and/or the third part (s) with respect to structure or composition thereof.

The catalyst composition of the invention (support) is for instance coated by separate spraying on a smooth or corrugated open metal foil or surface.

Alternatively, the catalyst coatings are coated by dipping or immersion of a finished, usually a cell-like metallic or ceramic catalyst substrate into a catalyst slurry. Also a combination of these preparation procedures can be used in the production. Active metals and promoters are already added to the slurry, or the coated catalyst is impregnated therewith by post-impregnation from a solution comprising water or an organic solvent (e. g. ethanol) as the solvent. Promoters can be added to the catalyst from the impregnation solution containing an inorganic or organic precursor. Ti can be added to the catalyst e. g. as Ti sol or from a Ti butoxide solution. Components can be added to the catalyst of the invention also by gas or solid phase methods (e. g. CVD, ALE, mechanical mixing).

According to the application, the thickness can for instance be from 0.1 to 200 pm (0.1-200 g/m2), normally from 10 to 60 pm (10-60 g/m2).

According to an embodiment of the invention, the catalyst is coated on one or several catalytic substrates made from metallic, ceramic, metal oxide, SiC and/or Si nitride material (s). The catalyst coating of the invention can be pre-or post- coated on normal ceramic or metallic cells or substrates where shapes of cells, such as a square, a triangle, cell density (10-2000 cpsi, cells per square inch, a term familiar to those skilled in the art), or wall thicknesses (10-500 um), can vary widely according to the application. Very large channel sizes can be used in the catalyst (< 100 cpsi) if the effluent gas contains high amounts of particles or sulfur compounds. In applications containing low amounts of particles and sulfur, very small channel sizes can be used in the cell (such as > 500 cpsi). In diesel applications, a typical cell number is from 50 to 600 cpsi. The values of these variables can also vary within the cell, or in the next cells, this being advantageous due to efficient mixing, low presure drop, or mechanical strength.

The cell to be coated can also serve as a kind of a statical mixing structure either having mixing zones (for instance bents, flow obstacles, or throttlings) in separate channels, or the structure being made by superimposing corrugated, curved foils or plates in a manner where the directions of wave crests deviate from that of the incoming gas, the wave crests of the superimposed plates being, respective, oriented in different directions. In a conventional metal cell, the wave crests of corrugated foils are parallel with one another, and with the main flow direction.

According to an embodiment of the invention, the catalyst is coated on one or several cell-like, or porous structure (s). The channels thereof can be parallel with

the flow direction and/or have a different orientation. According to another embodiment of the invention, the catalyst is coated on one or several particle separating and/or mixing structure (s). According to an embodiment of the invention, the catalyst is combined with a particle trap, or filter made of ceramic, metallic, metal oxide, Si02, SiC and/or Si nitride material (s).

Mixing efficiency can be controlled by altering the angle between the wave crest and the main flow direction. With the mixing structure, mixing of the flow is provided in radial direction of the pipe. With the mixing structure, higher separation rates for particles compared to normal cell structures are obtained. Also, the structure to be coated can partly or totally consist of a metal mesh, sintered porous metal, fiber, or a particle trap.

The catalyst of the invention can also be coated on two or several of the described catalyst structures located in series or parallel in flow direction. Catalyst structures of different, or of same sizes can be incorporated into a single catalyst converter, or they can be present in separate converters connected by necessary piping. The compositions of the catalysts of the invention, noble metal loads thereof (e. g. Pt), cell numbers (geometrical surface areas), or structures can be identical or different.

Latest diesel engines are typically provided with a turbo, and thus the temperatures in exhaust pipes are low, and there is no space very close to the engine for large converters. For this reason, the catalyst coatings of the invention can also be assembled in forms divided into smaller structures where the exhaust gas temperature is maximized for initiating reactions in the catalyst. Therefore, it is preferable to use for instance one or several small catalyst cell (s) or other structures (metal fiber, mixer) upstream of the turbo (preturbo catalyst) or immediately downstream thereof (precatalyst). The catalyst coating can also be situated at any point of the pathway of the exhaust gas, on the walls of piping or constructions (wings of the turbo, outlets from cylinders or from the turbo).

If an oxidation catalyst is necessary for downstream processing in addition to a particle separator, said particle separator can also be coated with the catalyst coating of the invention. In this way, a very compact structure is obtained. The particle separator can be made of ceramic, metallic, metal oxide, carbide (e. g.

SiC), nitride material (SiH2), nitride or a mixture thereof. The structure can be a cell-like particle trap or a rod-like structure where the gas flows through the holes on the walls, the particles being retained in the inlet side of the separator, in flow

direction. Other particle separators include fiber-like, mesh-like, foamy or plate-like structures that can also be coated with the catalyst of the invention. In addition to particle separation, such structures can be used for cost reasons or due to low pressure drops caused by them.

According to an embodiment of the invention, the first part of the catalyst is coated with a first coating, and the second part is coated with a second coating having a different composition (4). In this case, the compounds of the invention are partitioned in an optimal manner between various surfaces, and thus they can't chemically interfere with one another in the production stage or during use. When several catalyst layers are superimposed by coating, there is often a risk for the layers, particularly for moist layers to be mixed in the production stage. The compositions are selected to endow one catalyst surface with high CO activity and the other with high HC activity. In the first and the second catalyst coatings, for instance a promoter metal 1 (e. g. Fe, Co), and promoter metal 2 (e. g. Ti, Mn) can be used, respectively. The first catalyst coating can contain Ce oxide and Ce promoter, the second coating being free of them. In smooth and corrugated foil, also various zeolites can be used. In the first and the second foils, zeolites with Si: AI2 equal to 55 or lower, and zeolites with Si: Aì2 higher than 55 can be used, respectively.

The light-off temperature of the catalyst can be lowered in comparison to a catalyst containing an equal amount of Pt per volume unit (e. g. 76 g Pt/cft) by using a higher Pt load in one of the foils (e. g. 115 g Ptlcft in smooth foil) and a lower Pt load in the other (e. g. 50 g Pt/cft).

Some of the catalysts of the invention are used successfully also in lean applications where the composition of the mixture is lean, X > 1, for an extended period, say 60 s, and momentarily rich or nearly stoichiometric X < 1,2, preferably ? < 1, for e. g. 2-5 s.. In this case, the aim is to obtain a higher NO,, conversion with only slightly increased fuel consumption. So-called normal NOx trap catalysts being deactivated by sulfur, and sulfur removal requiring a temperature of above 600-650 °C, the use thereof in diesel applications is almost impossible. For this reason in diesel applications, it is preferable to use under heterogeneous conditions catalysts containing no or only very low amounts of normal NOx trap compounds such as Ba, Sr, or K. The performance of the catalysts of the invention is good just at the temperatures of the exhaust gases, for instance during normal traffic cycles. The temperatures of the diesel exhaust gases being extremely low, a catalyst with an acceptable NOx performance should have a low light-off

temperature with respect to CO, hydrogen, and hydrocarbons for lean and rich applications. In this case, it is convenient to combine superior oxidation and NOx catalysts to operate under heterogeneous conditions. The performance during rich peaks can be improved by adding Rh to the catalyst besides Pt. The superior performance of the catalyst is based on the changes of oxidation states particularly in noble metals and in the Ce compound, and the second promoter.

The purpose of the enriched peaks is to reduce the catalyst surfaces, and moreover, reducing agents can also be adsorbed in the catalyst for further use during the lean phase. The reduction of the nitrogen oxides is then based on the accumulation thereof, and the mechanism of reduction can also be called NO decomposition on a catalyst surface that is at least somewhat reduced.

According to an embodiment of the invention, the catalyst can be composed of several coated superimposed layers, at least one of which is a layer of the invention. The catalyst of the invention can be coated with another layer of the invention, the upper, or the surface layer being free of active metal. This protective layer can prevent the fully active metal from leaving from the catalyst, protect lower layers against deactivation, promote adsorption of particles to the surface, and/or alter electrical properties (electrical conductivity, charging, etc. ) of the surface layer in comparison to the lower layer.

Preferably, the surface of the catalyst of the invention can intentionally be rough, thus promoting mass and heat transfer and/or particle removal/reactions.

Roughness is provided for instance with rough starting materials such as with 30- 100 pm fibers and/or coating methods. Roughness, support thickness and/or the number of catalytically active layers can preferably vary in axial direction of one or more of the catalysts.

Constructional embodiments of the invention are not limited in any way. According to an embodiment of the invention, the catalyst of the invention can be present in several structures assembled parallel or in series with respect to the flow direction.

Detailed description of the invention In the following, the invention is described in more detail with reference to Examples 1-11, and Figures 1-3.

Figures 1 a and 1 b are cross-sectional presentations of the catalyst of the invention.

Figure 2 shows the use of the catalyst of the invention for NOx conversion (on an average for 5 minutes) under heterogeneous, mainly lean conditions.

Figure 3 shows the effect of dividing and uniting the catalyst composition on the performance of the catalyst of the invention.

In the catalyst of the invention shown in Figures 1a and 1b, separated first catalyst part (1) and second catalyst part (2) are provided with an identical or different catalytic coating (3,4) consisting besides aluminium oxide and adhesives, also of the following chemical compound: first zeolite (5), second zeolite (6), third zeolite (7), Ce oxide or mixed Ce oxide (8), Ce promoter (9) forming with Ce oxide a mixed oxide or a mixture of oxides, finely divided first promoter (10), second promoter (11), and active metals (12). The first catalyst part can for instance be a flat metal foil, and the second catalyst part can be e. g. a corrugated metal foil, forming together a rolled cellular structure. Said catalyst parts can be combined to a unitary structure can before coating. The inventive, and the comparative catalysts were as shown in Table 1. They were prepared for laboratory testing by first making a slurry from powders, and dissolved starting materials, and water.

The slurry obtained was mixed and milled in a ball mill. The properties (grade, purity, particle size, any stabilizers) of the starting materials were varied in the experiments to obtain a coating that was as stable and even as possible, and to maximize the activity in subsequent laboratory testing. Part of the starting materials can be added after milled or during thereof, thus providing differences with respect to mixing of the starting materials, any dissolution, and particle size thereof. The catalysts mainly being based on aluminium oxide and zeolite, or anyway containing aluminium and silicon, Al or Si sols were used as adhesives.

By the addition of Ti sol to the catalyst, different kinds of Ti02, that is, first or second promoter according to the invention was obtained in the catalyst, depending on the size of the TiO2 particles in the sol. The surface area (BET) of the aluminium oxide used as the raw material was from 150 to 300 m2/g (preferably more than 200 m2/g), the particle size (d5o) being about 5-30 pm. In the catalysts, ZSM-5, Beta, and Y were used as the zeolites, the Si : Al2 thereof varying between 20 and 300, and specific surface areas being more than 350 m2/g. In this way, the catalysts are provided with a high surface area by these zeolites. Some zeolites were preimpregnated with Pt or other active components in advance by wet or dry method. The particle sizes of the employed pure Ce02, Ti02 (anatase, 70-150 m2lg), Mn oxides (MnO2, Mn304), or mixed oxides were between 1 and 30 pm. Pure Ce02 having a surface area of more than 250 m 2/g

was also used in the catalysts. In mixed oxides containing cerium the surface areas of starting materials varied in the range from 50 to 200 m2/g. Depending on the concentration, the components normally added to the slurry by impregnation (wet or dry impregnation), or in dissolved state formed particles (e. g. Ce, La, Mn, Co, Ti, Fe oxides and noble metals) having the size of about 1-100 nm distributed on the porous surface of the support. The highest particle sizes were thus provided by high concentrations, and by co-precipitating the metal oxides on the catalyst surface. The oxides present in the catalyst were also added to the slurry as corresponding sols (e. g. Ti, Ce, Al).

Smooth and corrugated metal foils were coated with the thus prepared slurry to a thickness of 50 pm, the samples were dried at about 110°C, and calcined for four hours at 550°C. In the wet impregnation method, the pores of the support are filled with a solution having a suitable concentration, thus retaining a desired amount of the compound in the sample. In dry impregnation, impregnating solution containing a desired amount of the active component is totally absorbed by the pores of the support. Most compounds formed corresponding oxides by calcination in static air.

The catalyst was impregnated with Pt by the so-called chemisorption method using a Pt ammin carbonate solution as the starting solution. Pt was thus dispersed as small particles on the catalyst surface. After impregnation, the catalyst was dried at about 80-300°C, and calcined (a mixture containing oxygen in excess such as air) and/or reduced with a rich mixture (containing e. g. hydrogen, CO, hydrocarbon, or exhaust gas, ? < 1). A cell-like sample was obtained by rolling together smooth and corrugated coated foils. In some of the samples, the foils were coated with two different superimposed catalyst layers.

After the preparation, the specific surface area of the active support in various samples was about 50-300 m2/g. The catalysts mostly containing alumina and zeolites having high surface areas, the specific surface area of the samples of the invention was usually above 200 m2/g. The amount of the support on the metal foil was about 40-60 m2/g.

Table 1 Cell-like catalysts used in activity testing No Code Pt Pt Note Zeo Zeo2 Ce Ce promoter Pro1 Pro2 Cell g/cf % 1: Zeo % % % % no. t typ 3 d50> Zr, Ti, Mn, ri, Mn, Ti, Mn, cpsi e/% type/0. 4 o, Pr, Nd. Fe, Co, D50>0. % pm d50<0.4 µm La, Au, 4 µm Ce, D5o<0. 4 nu 1 Al-Ce-Zr 210 3 Ref. - - 16.7 3.3-Zr - 800 Al-Ce- 10 3 19 14. 6. 4-Zr 800 ZSM5(3 3) Al-Ce- Co- 0. 3.3C 40 19 - 2.3-Co 4-La 800 ZSM5(3 6 e 3)-La Al- SM5(3 190 3 Ref. 19 - - - 4-La 800 3)-La Al- 5 ZSM5(3 40 0. Ref. 19--- 4-La 800 3)-La 6 Al-Ce- 8 130 2 19 - 4.0 2.3-Co 4-La 800 ISM5 (3 3)-La Al-Ce- 7 Zr- 240 3. 19 - 14.6 5.4-Zr 800 Beta 25 3 Al-Ce- 8 Si- 240 3. 19 - 20 - Si 800 ZSM5(3 2 3) Ref.. Al-Ce- 9 ZSM5(3 211 19 - 9 - - 800 3) 2 erse d Al-Ce- 10 Zr- 105 1. 15 - 10 - 3.5-La 400 Beta(25 8 )-La Al-Ce- 1. 11 105 Ref. - - 16.7 3.3-Zr - 400 Zr 8 Al-Ce- 12 Zr- 181 3 19 - 16.7 3.3-Zr - 400 ZSM5(3 3) 13 Al-Ce- 70 1 19-16. 7 3. 3-Zr 500 Zr-Y(80) Al-Ce- Zr- 14 Beta(15 70 1 19 - 16.7 3.3-Zr - 500 0) Al-Ce- 15 Zr- 70 1 7 - 16.7 3.3-Zr - 500 ZSM5(3 3) Al-Ce- 16 Zr-Ti- 70119- 16.7 3.3-Zr 2.9-Ti 300 ZSM5(3 3) Al-Ce- 17 Zr- 70 1 19 - 16.7 3.3-Zr - 500 ZSM5(2 80) Al-Ce- 70 1 19 - 16.7 3.3-Zr - 500 ZFM5(3 3) Al-Ce- 70 1 30 - 4.2 0. 8-Zr - 500 ZSM5 (3 3) Al-Ce- 20 1 45 - 4. 2 0. 8-Zr 500 ZSM5 (3 3) Al-Ce- 21 Zr- 70 1 75 - 4.2 0.8-Zr 500 ZSM5(3 3) Al-Ce- 70 1 19 - 16.7 3.3-Zr - 300 ZSM5(3 3) Al-Ce- Zr-20 23 ZSM5 (3 70 1 18 (3% 8. 4 1. 6-Zr 500 3) Pt/Bet Pt) a 300 Pt- Ai-Ce-addi- Zr-tion ZSM5(3 in 24 70 1 15 15 8.4 1.6-Zr - 500 3)- two Beta(30 way 0) s Al-Ce- Zr 15(3 25 ZSM5(3 70 1 15 % 8.4 1.6-Zr - 500 3)- Pt/Beta( Pt) 300)- Al-Ce- Zr- 15( 26 Pt/ZSM 70 1 3% 15 8.4 - 5 (33)- Pt) Beta (30 0) Al-Ce- Zr-addi- tison 27 in 15 15 8.4 1.6-Zr - 500 Beta(30 way s Al-Ce- Zr- 5 + ZSM5(5 0. 3% 5 28 0)- 406PtY(3% 10(3% 8.4 1.6-Zr- 200 Beta(30 Pt) 0)- Pt/Y(80 Al-Ce- 3% 10 29 ZSM5(3 70 1 Pt/B 10 (3% 8. 4 1. 6-Zr 1.4-Fe 500 eta Pt) Pt/Beta( 300)-Fe Al-Ce- 2% 19 30 Zr- 70 1 Ce/B - (2% 16.7 3. 3-Zr 0. 4-Ce 500 Ce/Beta eta Ce) (300) Al-Ce- 31 Zr- 2% 19 70 1 - (2% 16.7 3.3-Zr 0.4-Ce 500 Ce/Y(80 Ce/Y ) Ce) -Ce-Zr- 32 ZSM5 (3 70 1 19-16. 7 3.3-Zr 1.8-Ti 500 3)-Ti AI-Ce- Zr- 1.8-Ti. 33 70 1 19 - 16.7 3.3-Zr 500 ZSM5(3 2.8-Fe 3)-Ti-Fe Al-Ce- Zr- ZSM5 (3 10 34 3)-70 1 10 (3% 8.4 1. 6-Zr 1.8-Ti. 500 Pt/Beta (Pt).-e 300)-Ti- Fe At-Ce-1. 8-Ti Zr- 35 ZSM5 (3 70 1 10 10 8.4 1.6-Zr 500 3)- Pt/Beta ( 300)-Ti Al-Ce-1. 8-Ti Zr- ZSM5 (3 36 3)-70 1 10 10 8. 4 1. 6-Zr 1. 4-Fe 500 Pt/Beta ( 300)-Ti- Fe Al-Ce- 20-Ti ZSM5 (3 37 3)-70 1 10 10 10 - 500 Beta (30 0)-Ti Al-Ce- 10-Ti ZSM5 (3 38 3)- 70 1 10 10 10 500 Beta (30 0)-Ti Al-Ce- Mn3 O4 39 Zr- 3. 12. 1.7- 174 surfa - 10.9 2.2-Zr 800 ZSM5 (3 1 ce 5 Mn3O4 3)-Mn layer Al-Ce- Zr- 12. 5.5- 70 1 2+Al - 10.6 2.1-Zr 400 ZSM5(3 1 MnO2 surfa 3)-Mn ce layer MnO Al-Ce- 2+Ce Zr-0. O2 12.5. 5Mn 41 62 10. 9 2. 2-Zr 3.7-Ce 400 ZSM5 (3 8 surfa 5 02 3) -Mn ce layer 42 Ai-Ce 145 3 Ref. - - 28 - - - 800 A Pt/CeZr 8. 4/1 43 Fe/Eta 70 1 10 10 1.6-Zr 0.1-Fe - 500 (22)- %Pt ZSM5(5 0) Al-Ce- Zr- 44 Fe/Beta 70 1 10 10 8.4 1.6-Zr 0.1-Fe 10 Ti 500 (22)- Y(80)-Ti Al-Ce- Pr- 45 ZSM5(3 70 1 10 10 7.6 2.4-Pr 3)- Beta(30 0)

Pt: % by weight as metal, others: % by weight as oxides in the support. Ce: as oxide or mixed oxide, Ce promoter: dispersed on the surface of Ce or forms a mixed Ce oxide, Pro1 = first promoter, dispersed e. g. as an oxide or metal particles of less than 0.4 pm in alumina, zeolite, or evenly throughout the whole support, Pro2 = second promoter, e. g. as an oxide, the particle size being more than 0.4 um, ref = comparative catalyst. As common in the art, Pt concentration is shown in g/cft (grams per cubic feet, factor 0.0283168 to obtain g/m3). As common in the art, cell number is in cpsi = cells per square inch (factor 0.155 to obtain cells/cm3).

The activities of the catalysts were tested under laboratory conditions by simulating the exhaust gases from diesel fuel engines, mainly operating with lean mixtures. Propene was used for simulating hydrocarbons present in exhaust gases. Stability under actual conditions being a problem, the activities of the samples were normally measured only after hydrothermal ageing thereof (10% water in the air, space velocity about 4000 h 1 in the sample) at 600-700 °C for 20 hours. The best samples stable in hydrothermally demanding actual exhaust gases were thus selected. The composition at the inlet of the laboratory reactor was controlled by computer-aided mass flow controlling devices, the composition being analyzed by continuously operating NOx, CO, HC, and °2 analyzers. The conditions for the activity measurements carried out with laboratory equipment were as follows: Table 2 Gas compositions used for laboratory simulation COMPOUND DIE1 DIE2 DIE3 NO, PPM 300 1000 200 C3H6, PPM 900 500 160 CO, % 900 500 500 H2, PPM 300 0 0 O2, % 8 15 12 H20, % 10 10 6 C02, % 10 10 6 SO2, PPM 0 0/25 0 N2 BALANCE BALANCE BALANCE SPACE 50,000 50,000 50, 000 VELOCITY, H' Space velocity (SV) = flow rate of the exhaust gas I volume of the catalyst cell Table 3 Results from the activity testing for the inventive and comparative catalysts, after hydrothermal ageing (700 °C/20 h) Cat Code Pt Test mixture Too, °C Tgo, max No g/cft CO °C NOx HC conv. % 1 AI-Ce-Zr 210 DIE1 176 220 80 2 Al-Ce-Zr-ASM5 (33) 210 DIE1 158 218 63 3 Al-Ce-Co-ZSM5 (33)-La 40 DIE1 203 260 33 4 Al-ZSM5 (33) -La 190 DIE1 180 230 68 5 Ai-ZSM5 (33)-La 40 DIE1 197 260 43 6 Al-Ce-Co-ZSM5 (33) -La 130 DIE1 165 235 63 7 Al-Ce-Zr-Beta (25) 240 DIE1 154 200 76 8 Al-Si-Ce-ZSM5 330 240 DIE1 150 200 84 9 Al-Ce-ZSM5(33 211 DIE1 152 220 75 10 AI-Ce-Zr-Beta (25)-La 105 DIE1 175 211 77 11 Al-Ce-Zr 105 DIE1 192 230 62 12 Al-Ce-Zr-ZSM5(33) 181 DIE1 164 179 93 13 Al-Ce-Zr-Y (80) 70 DIE2+SO2 189 228 27 14 Ai-Ce-Zr-Beta (150) 70 DIE2+SO2 187 206 34 15 Al-Ce-Zr-ZSM5 (33) 70 DIE2+S02 208 236 32 15 AI-Ce-Zr-ZSM5 (33) 70 DIE3 182 205 51 16 Al-Ce-Zr-ZSM5 (33)-Ti 70 DIE3 152 161 34 17 Al-Ce-Zr-ZSM5 (280) 70 DIE2+S02 211 227 24 18 Al-Ce-Zr-ZSM5 (33) 70 DIE2+SO2 203 223 22 19 A !-Ce-Zr-ZSM5 (33) 70 DIE3 156 159 44 20 Al-Ce-Zr-ZSM5 (33) 70 DIE3 157 166 28 21 Ai-Ce-Zr-ZSM5 (33) 70 DIE3 163 171 36 Al-Ce-Zr-ZSM5(33)- 23 70 DIE3 150 159 35 Pt/Beta(300) Al-Ce-Zr-ZSM5(33)- 24 70 DIE3 149 156 35 Beta(300) Al-Ce-Zr-ZSM5(33)- 25 70 DIE3 154 162 41 Pt/Beta(300) Al-Ce-Zr-Pt/ZSM5(33)- 70 DIE3 162 176 33 Beta(300) Al-Ce-Zr-ZSM5(50)- 27 70 DIE3 156 158 37 Beta 300 28 Al-Ce-Zr-ZSM5(50)- 40 DIE3 171 188 24 Beta(300)-Pt/Y 80 29 Al-Ce-Zr-ZSM5(33)- 70 DIE3 113 156 38 Pt/Beta(300)-Fe 30 Al-Ce-Zr-Ce/Beta(300) 70 DIE3 142 168 33 31 Al-Ce-Zr-Ce/Y (80) 70 DIE3 159 166 33 32 Al-Ce-Zr-ZSM5 (33)-Ti 70 DIE3 151 160 35 33 Al-Ce-Zr-ZSM5 (33)-Ti- 70 DIE3 124 166 32 34 Ai-Ce-Zr-ZSM5 (33)-70 DIE3 118 169 30 Pt/Beta(300)-Ti-Fe Al-Ce-Zr-ZSM5(33)- 35 70 DIE3 151 160 45 Pt/Beta (300)-Ti 36 Al-Ce-Zr-ZSM5(33)- 70 DIE3 116 164 41 Pt/Beta(300)-Ti-Fe 37 Ai-Ce-ZSM5 (33)- 70 DIE3 145 162 41 Beta (300)-Ti 38 Al-Ce-ZSM5(33)- 70 DIE3 148 157 38 Beta(300)-Ti 39 A !-Ce-Zr-ZSM5 (33)-Mn 174 DIE1 190 181 59 40 AI-Ce-Zr-ZSM5 (33)-Mn 70 DIE2+SO2 217 246 25 41 Al-Ce-Zr-ZSM5(33)-Mn 62 DIE2+SO2 247 262 21 42 Al-Ce 145 DIE1 195 250 53 Al-Pt/CeZr- 43 70 DIE3 137 157 44 Fe/Beta922)-ZSM5(50) 44 Al-Ce-Zr-Fe/Beta(22)- 70 DIE3 133 156 33 Y80-Ti Al-Ce-Pr-ZSM5(33)- 45 70 DIE3 149 157 45 Beta(300)

Tso = temperature corresponding to 50% conversion in the light-off experiment.

Example 1 For lean conditions, prior art uses oxidation catalysts comprising alumina, zeolite, mixtures of alumina and zeolite, and further, alumina combined with other metal oxides (Si02, TiO2). In Table 2, the catalysts no. 2, 7, 8, 12,13, 14,15, 17, 18, 19, 20,21 are catalysts of the invention containing, besides aluminium oxide and adhesives, one zeolite (ZSM5 (33), ZSM5 (280, Beta (25), Beta (300), Y (80) ), Ce oxide and Ce promoter. The amount of the Ce promoter (Zr, Si) dispersed in Ce oxide is clearly lower than that of Ce. Results from the activity testing carried out in a mixture simulating diesel exhaust gases (DIE1) show that the light-off temperatures are lower for the catalysts of the invention than for comparative catalysts (1,4, 5,9, 11,42). Catalysts having zeolite contents varying from 19 to 75% are compared by means of the catalysts 18-21. Catalyst no. 15 contains zeolite only 7%. Higher zeolite contents can be used, if the ageing conditions of catalysts are mild. It is preferable to use catalysts having lower zeolite content in case they are exposed to high temperatures under operation conditions for longer periods of time. DIE1 mixture contains relatively high amounts of hydrocarbons

causing nitrogen oxides to be reduced in a narrow temperature range of 180-300 °C. In some cases, maximum conversions of nitrogen oxides were higher for catalysts also having higher light-off temperatures. The comparison of the catalysts of the invention with the catalyst no. 42 shows that low activities are attained with Ce evenly dispersed in alumina, and accordingly, the invention substantially improves the performances of oxidation catalysts.

Example 2 The catalysts no. 3,6, 10,16, 32 and 33 of Table 1 comprise an aluminium oxide based composition of the invention containing one zeolite (ZSM5 (33) or Beta (25)), Ce mixed oxide (Ce promoter: Co, Zr), and a first promoter (La, Ti, Fe) dispersed mainly on the aluminium oxide surface in the form of small particles. Of these, after ageing at 700 °C, the catalyst no. 3 having a Pt load of 40 g/cft was weaker with respect to light-off in comparison to the comparative catalyst no. 5, whereas fresh catalyst of the invention was better. In contrast, the catalyst of the invention was substantially better than the comparative catalyst no. 4 for higher loads (no.

6). Based on this result, Co is a suitable Ce promoter in case Pt load in the catalyst is high.

Example 3 The catalysts no. 24 and 27 of Table 1 comprise an aluminium oxide based composition further containing two different zeolites and mixed Ce oxide (Ce oxide and Ce promoter). Pt is added to the samples in two steps, strating with an impregnation solution containing a Pt (NH3) 4 complex, followed by a solution containing a Pt (NH3) 4 (OH) 2 complex. In this way, catalysts having substantially lower light-off temperatures in a DIE3 mixture in comparison to that of a catalyst comprising a single zeolite no. 15 were obtained. An improvement of the performance of the catalyst was thus achieved by the addition of Pt from two different impregnation solutions and precursors.

Example 4 The catalysts no. 25, 26 and 28 of Table 1 comprise an aluminium oxide based composition further containing two, or three different zeolites and mixed Ce oxide.

Moreover, part of the Pt present in the catalyst is added to one zeolite (Pt: Beta (300), Pt: ZSM5 (33) or Pt: Y (80)). Also in this case, the light-off temperatures are lower than for the catalyst no. 15, even though the catalyst no.

26 where Pt was added to ZSM5 (33) was the poorest one of the concepts

comprising two zeolites. The result obtained with the catalyst 28 is not quite suitable for comparison due to a different coating method.

Example 5 The catalysts no. 30 and 31 of Table 1 comprise an aluminium oxide based composition further containing a zeolite and mixed Ce oxide. Moreover, 2% Ce (first promoter) is added to the zeolite (Beta (300), or Y (80) ). Ce addition to zeolite was advantageous to reactions, decreasing the light-off temperatures in comparison to, say, catalyst 13.

Example 6 The catalysts no. 29,34, 35 and 36 of Table 1 comprise an aluminium oxide based composition further containing two different zeolites, mixed Ce oxide (Zr as Ce promoter), and first promoter (Ti, Fe) mainly dispersed on alumina surface.

Moreover, part of the Pt present in the catalyst is added to one zeolite (Pt: Beta (300), Pt: ZSM5 (33), or Pt: Y (80)). With the Fe addition, low CO light-off was achieved, whereas with Ti addition, HC activity was improved in comparison, e. g. to the catalyst no. 15.

Example 7 The catalysts no. 37 and 38 of Table 1 comprise an aluminium oxide based composition further containing two zeolites (Beta (300), and ZSM5 (33) ), as well as coarsely divided Ce (dso > 0. 4 pm) and Ti oxides (= second promoter, d > 0. 4 pm). The light-off temperatures were substantially improved in comparison to the catalyst no. 15.

Example 8 The catalysts no. 39,40 and 41 of Table 1 comprise an aluminium oxide based composition having a structure of two layers, the lower layer further containing one zeolite and mixed Ce oxide (Zr), second promoter (Mn02, Mn304) and first promoter (Ce) being present as large particles in the upper layer within aluminium oxide. Upper layer is free of Pt. The aim is to separate Pt and the second promoter, thus preventing interferences with oxidation reactions due to interactions thereof on Pt surface in fresh or aged form, this being advantageous for oxidation of soot and hydrocarbons. In the catalysts of the invention, the second promoter is often a compound promoting the combustion of soot, the thermal stability thereof

being lower that that of other components. For this reason, it is incorporated, if possible, into a different layer that the other components in order not to compromize the thermal, or chemical stability thereof (Pt being most important).

Example 9 The catalyst no. 22 of Table 1 was used in an effluent gas flow rich in oxygen from a pulp plant, the effluent gas further containing more than 400 mg/m3 of hydrogen sulfide, and various organic sulfides (methyl mercaptan, dimethyl sulfide, dimethyl disulfide). While the total emissions of sulfur compounds and other harmful effects might be relatively low, bad odour is caused by sulfides even at very low concentrations in the outside air. For this reason, the aim is to convert sulfides using a catalyst unit to sulfur oxides, preferably to sulfur dioxide, having a significantly higher threshold of bad odour than that of sulfides, and the remaining sulfides mixed with the outside air not exceeding the threshold of odour for humans. For all sulfides, the light-off temperature (Taj) of the catalyst was clearly below 300°C, whereas the light-off temperature was almost 400°C for a normal aluminium oxide based catalyst having identical size (space velocity of 50,000 h-1) and identical Pt loading. Accordingly, said catalyst can be used in various VOC applications where low light-off and operation temperatures of different hydrocarbons are important.

Example 10-Figure 2 The catalysts no. 7 and 8 of Table 1 were tested under heterogeneous lean-rich conditions (Figure 2). Mean NOx conversion of even higher that 60-80% was achieved with said catalysts at about 200°C temperatures necessary for diesel catalysts. The catalysts being totally free of normal NOx adsorption materials (Ba, Sr, K, Na, Mg, La) forming stable harmful sulfates under lean conditions, the stability thereof in exhaust gases containing SO2 is high, the catalyst being regenerated to be free of sulfates even at a temperature below 300°C during normal enrichments or even during a lean phase. While the operation window is relatively narrow, the NOx adsorption capacity of the catalyst is significant since it worked in the tested mixture (lean 60 s/rich 5 s, normal test for NOx adsorption catalysts), and thus the window is perfectly suitable for the purposes of diesel passenger cars (100-350°C).

Conditions for Figure 2: - HT aged 700 °C/20 h catalyst for lean-rich mixture.

- Lean : 500 ppm NO, 3000 ppm HC, 0.25% CO, 0.08% H2, 7% ou, 10% CO2, 10% H20, balance being N2.

- Rich : 1500 ppm NO, 3000 ppm HC, 6% CO, 2% H2, 0.1% 02, 10% CO2, 10% H20, balance being N2.

Example 11-Figure 3 The catalysts of the invention differed from each other with respect to CO and HC activities. An optimal combination was obtained by dividing the catalysts between two parallel foils, one catalyst composition to a smooth and the other to a corrugated foil, thus igniting both CO and HC in the test mixture DIE3 at low temperatures (Figure 3).

Conditions for Figure 3: - Division of the catalyst composition by combining a superior catalyst of the invention for CO (cat 29) and HC oxidation (cat32).

- Fresh oxidation catalysts 13, 29 and 32 in DIE3 light-off mixture.

- In divided structure, Catalyst 29 in a smooth, and catalyst 32 in a corrugated foil.

Using this divided composition, the CO light-offtemperature (Tso) was 107°C, and the HC light-off temperature was 147°C. Based on laboratory testing, no major differences between the light-off temperatures of fresh, and aged samples were found, that is, the resistance of the catalysts of the invention to hydrothermal ageing even at 700°C is high.