WO2014027207A1 - Zeolite promoted v/ti/w catalysts - Google Patents

Description

ZEOLITE PROMOTED V TI/W CATALYSTS

BACKGROUND

A. ) Field of Use:

The present invention relates to catalysts, systems, and methods that are useful for treating an exhaust gas resulting from combustion of hydrocarbon fuel, and particularly exhaust gas containing nitrogen oxides, such as an exhaust gas produced by diesel engines.

B. ) Description of Related Art:

The largest portions of most combustion exhaust gases contain relatively benign nitrogen (N₂), water vapor (H₂0), and carbon dioxide (C0₂); but the exhaust gas also contains in relatively small part noxious and/or toxic substances, such as carbon monoxide (CO) from incomplete combustion, hydrocarbons (HC) from un-burnt fuel, nitrogen oxides (NO_x) from excessive combustion temperatures, and particulate matter (mostly soot). To mitigate the environmental impact of exhaust gas released into the atmosphere, it is desirable to eliminate or reduce the amount of these undesirable components, preferably by a process that, in turn, does not generate other noxious or toxic substances.

One of the most burdensome components to remove from a vehicular exhaust gas is NO_x, which includes nitric oxide (NO), nitrogen dioxide (N0₂), and/or nitrous oxide (N₂0). The reduction of NO_x to N₂ in a lean burn exhaust gas, such as that created by diesel engines, is particularly problematic because the exhaust gas contains enough oxygen to favor oxidative reactions instead of reduction. NO_x can be reduced in a diesel exhaust gas, however, by a process commonly known as Selective Catalytic Reduction (SCR). An SCR process involves the conversion of NO_x, in the presence of a catalyst and with the aid of a reducing agent, into elemental nitrogen (N₂) and water. In an SCR process, a gaseous reductant such as ammonia is added to an exhaust gas stream prior to contacting the exhaust gas with the SCR catalyst. The reductant is absorbed onto the catalyst and the NO* reduction reaction takes place as the gases pass through or over the catalyzed substrate. Several chemical reactions occur in a selective catalytic reduction (SCR) system using NH₃ as reductant, all of which represent desirable reactions which reduce NO_x to elemental nitrogen. The dominant reaction mechanism is represented in equation (1 ).

4NO + 4NH₃ + 0₂→ 4N₂ + 6H₂0 (1 )

Competing, non-selective reactions with oxygen can produce secondary emissions or may unproductively consume NH₃. One such non-selective reaction is the complete oxidation of NH₃, represented in equation (2).

4NH₃ + 50₂→ 4NO + 6H₂0 (2)

Furthermore, the reaction of N0₂ present in the NO_x with NH₃ is considered to proceed according to reaction (3).

3N0₂ + 4NH₃→ (7/2)N₂ +6H₂0 (3) Further, the reaction between NH₃ and NO and N0₂ is represented by reaction (4): NO+N0₂ +2NH₃→ 2N₂ +3H₂0 (4)

Although the reaction rates of the reactions (1 ), (3) and (4) vary greatly depending on the reaction temperature and the sort of the catalyst used, that of the reaction (4) is, in general, 2 to 10 times as high as those of the reactions (1 ) and (3).

The application of SCR technology to treat NOx emissions from vehicular IC engines, particularly lean-burn IC engines, is well known. A typical prior art SCR catalyst disclosed for this purpose includes V2O5/WO3 supported on Ti0₂ (see WO 99/39809). However, in some applications the thermal durability and performance of vanadium-based catalyst may not be acceptable.

One class of SCR catalysts that has been investigated for treating NO_x from internal combustion engine exhaust gas is transition metal exchanged zeolites (see WO 99/39809 and US 4,961 ,917).

However, in use, certain aluminosilicate zeolites such as ZSM-5 and beta zeolites have a number of drawbacks. They are susceptible to dealumination during high temperature hydrothermal ageing resulting in a loss of acidity, especially with Cu/beta and Cu/ZSM-5 catalysts; both beta- and ZSM-5-based catalysts are also affected by hydrocarbons which become adsorbed on the catalysts at relatively low temperatures and are oxidised as the temperature of the catalytic system is raised generating a significant exotherm, which can thermally damage the catalyst. This problem is particularly acute in vehicular diesel applications where significant quantities of hydrocarbon can be adsorbed on the catalyst during cold-start. And beta and ZSM- 5 zeolites are also prone to coking by hydrocarbons, which reduces catalyst performance. Accordingly, there remains a need for improved catalyst for selective catalytic reduction processes.

SUMMARY OF THE INVENTION

Applicants have discovered that blending vanadium-based SCR or ASC catalysts with certain molecular sieves improves the catalytic performance that is not observed when each of these components are considered alone. In particular, catalyst of the present invention achieve improved high temperature performance, improved hydrothermal stability, high sulphur tolerance, and improved N0₂ tolerance compared to known SCR catalyst and ASC catalysts. Such blends preferably contain aluminosilicate or ferrosilicate molecular sieves, preferably in the H+ form or ion exchanged with a transition metal such as Fe. Preferably the molecular sieves have a framework selected from MFI, BEA, or FER.

Accordingly, provided is a catalyst composition for treating exhaust gas comprising a blend of a first component and second component, wherein the first component is an aluminosilicate or ferrosilicate molecular sieve component wherein the molecular sieve is either in H+ form or is ion exchanged with one or more transition metals, and the second component is a vanadium oxide supported on a metal oxide support selected from alumina, titania, zirconia, ceria, silica, and combinations thereof.

According to another aspect of the invention, provided is a catalytic washcoat comprising a catalyst blend as described herein.

According to another aspect of the invention, provided is a catalytic article, preferably an extruded flow-through honeycomb, comprising a catalyst blend as described herein.

According to yet another aspect of the invention, provided is a method for treating NO_x or NH₃ in an exhaust gas, such as an exhaust gas generated by a diesel internal combustion engine, wherein the method involves contacting the exhaust gas with a catalyst blend as described herein whereby the concentration of NO_x or NH₃ in an exhaust gas is reduced.

BRI EF DESCRI PTION OF THE DRAWING

Figure 1 is a graph depicting NO_x conversion data for a fresh catalyst according to an embodiment of the present invention and comparative data for a catalyst known in the prior art.

Figure 2 is a graph depicting NO_x conversion data for a fresh catalyst according to an embodiment of the present invention and comparative data for a catalyst known in the prior art.

Figure 3 is a graph depicting NO_x conversion data for a fresh catalyst according to an embodiment of the present invention and comparative data for a catalyst known in the prior art.

Figure 4 is a graph depicting NO_x conversion data for aged catalysts according to an embodiment of the present invention and comparative data for aged catalysts known in the prior art.

Figure 5 is a graph depicting NO_x conversion data for two different catalysts according to an embodiment of the present invention and comparative data for a catalyst known in the prior art.

DETAILED DESCRI PTION OF PREFERRED EMBODIMENTS OF THE INVENTION

In a preferred embodiment, the invention is directed to a catalyst for improving environmental air quality, particularly for improving exhaust gas emissions generated by diesel and other lean burn engines. Exhaust gas emissions are improved, at least in part, by reducing NO_x and/or NH₃ slip concentrations in lean burn exhaust gas over a broad operational temperature range. Useful catalysts are those that selectively reduce NO_x and/or oxidize ammonia (ammonia slip) in an oxidative environment (i.e. , an SCR catalyst and/or an ASC catalyst).

According to a preferred embodiment, provided is a catalyst composition comprising a blend of (a) a molecular sieve component comprising an iron promoted aluminosilicate molecular sieve or a ferrosilicate molecular sieve (also known as an amorphous iron molecular sieve) having a framework selected from the group consisting of MFI, BEA, and FER; and (b) a vanadium component comprising one or more oxides of vanadium supported on a metal oxide support comprising titanium oxide.

As used herein, the term "blend" means an essentially uniform combination of two or more catalytic components either of which could be used alone for the same purpose as the blend. When combined in a blend, the individual catalytic components are not readily separable. And due at least in part to the synergistic nature of the combination, the catalytic effects of the constituent parts are indistinguishable from one another.

In a preferred embodiment, the catalyst composition comprises a majority of vanadium component (including metal oxide support) relative to molecular sieve component (including iron), based on weight. In certain embodiments, the catalyst composition comprises a vanadium component and a molecular sieve component in weight ratio of about 1 :1 to about 99:1 . Preferably, the vanadium component and molecular sieve component are present in a weight ratio of about 2:1 to about 4:1 , about 5:1 to about 10:1 , or about 10:1 to about 50:1 . Here, the vanadium component is calculated for the weight ratio based on the amount of oxide(s) of titanium oxide, oxide(s) of vanadium, and optionally oxide(s) for tungsten that are present in the blend and does not include other, non -catalytic metal oxides that are present, if any. Non-limiting examples of non-catalytic metal oxides that might be present in the composition include binders and other types of additives such as alumina, zirconia, ceria, silica, mixtures of alumina with zirconia or ceria, ceria coated on alumina, and mixed oxides, such as (non-zeolite) silica- alumina, alumina-zirconia, alumina chromia, and alumina ceria. Binders are distinct from the catalytic metal oxides in the composition because the binders are not promoted with a metal that is catalytically active for SCR processes and/or have a much larger particle size compared to the catalytic metal oxides. One skilled in the art will also appreciate that the ratios describe the relative proportions of catalytically active components in the blend and do not account of other components such as fillers, fibrous reinforcing agents, processing aides, water, and the like that might be present in various forms of the catalyst composition such as slurries, washcoats, and extrudable pastes.

In another embodiment, the catalyst composition comprises about 60 to about 99 weight percent vanadium component and about 1 to about 40 weight percent molecular sieve component, based on the total weight of catalytically active components in the blend. In certain embodiments, the catalyst composition comprises about 60 to about 70, about 75 to about 85, or about 90 to about 97 weight percent vanadium component and about 30 to about 40, about 15 to about 25, or about 3 to about 10 weight percent molecular sieve component.

Preferred vanadium components include oxides of vanadium on a support comprising oxides of titanium and, optionally, oxides of tungsten. In certain embodiments, the oxides of titanium and the oxides of vanadium are present in a weight ratio of about 30:1 to about 2:1 , more preferably from about 20:1 to about 5:1 , and even more preferably from about 15:1 to about 7:1 . In certain embodiments, the catalyst composition comprises up to about 25 weight percent oxides of tungsten, preferably from about 1 to about 25 weight percent, more preferably from about 5 to about 20 weight percent, and even more preferably from about 7 to about 15 weight percent based on the total weight of the vanadium component.

A preferred oxide of titanium is titanium dioxide (Ti0₂) which is also known as titania or titanium(IV) oxide, and is preferably in the anatase form. In certain embodiments, the Ti0₂ is at least 90 weight percent, and more preferably at least 95 weight percent, anatase form relative to the rutile form. In certain embodiments, the Ti0₂ is chemically stabilized and/or pre-calcined, for example as an end product of sulphate processing. Such chemically stabilized Ti0₂ displays the X-ray reflexes that are specific to the Ti0₂ lattice in X-ray diffractometry.

Typically, the Ti0₂ serves as a high surface area support for the oxide(s) of vanadium, which in a preferred embodiment is vanadium pentaoxide (V₂0₅), also known as vanadium (V) oxide or vanadia. In certain embodiments, the oxide(s) of vanadium are one or more of vanadium pentaoxide, vanadium trioxide, vanadium dioxide, or a transition metal or rare earth metal vanadate, such as iron vanadate. The support may also include oxide(s) of tungsten, preferably tungsten trioxide (W0₃), also known as tungsten (VI) oxide. Thus, the V₂0₅-Ti0₂ or V₂0₅-Ti0₂/W0₃ is in the form of self-supporting catalyst particles. In various embodiments, the catalytic metal oxide will have a surface area (BET) of from about 10 to about 300 m²/g or more. In certain embodiments, the Ti0₂ or Ti0₂/W0₃ will have an average particle size of about 10 to about 250 nanometers (nm), preferably about 1 0 to about 100 nm.

Preferably the molecular sieve is an aluminosilicate, preferably without substituted metals in the framework, or a ferrosilicate. Preferred frameworks include FER, MFI, and BEA. In certain embodiments, the molecular sieve is not a small pore molecular sieve. Molecular sieves, particularly aluminosilicates, are in the H+ form or are ion exchanged with a transition metal. Preferably, the aluminosilicate is substantially free of alkali and alkaline earth metals. H+ form molecular sieves preferably are free of non- framework metals. Examples of useful transition metals include Fe, Cu, Ni, Co, Zn, and Ni, with Fe and Cu being preferred, and Fe being particularly preferred. In certain embodiments, the molecular sieve is essentially free of any non-framework metal other than Fe. Preferably, the ion exchange occurs after synthesis of the molecular sieve.

Preferred blends comprise an iron promoted molecular sieve or ferrosilicate molecular sieve having at least one framework selected from MFI, BEA, and FER. The molecular sieves can be selected from zeolites and non-zeolite materials. A zeolites is generally considered to be an aluminosilicates, whereas a non-zeolite molecular sieve is a molecular sieve having a specific zeolite crystal structure (e.g., IZA Framework Type), but instead of being an aluminosilicate, the non-zeolite molecular sieve has one or more non-aluminium/non-silicon cations present in its crystal lattice, e.g. phosphorus, iron, etc. Useful types of non-zeolite molecular sieve include silicoaluminophosphates (SAPOs) and ferrosilicates.

Particularly preferred are iron-containing aluminosilicate zeolites such as Fe-containing MFI, BEA, and FER, with MFI being preferred.

Useful MFI isotypes include ZSM-5, [Fe-Si-0]-MFI, AMS-1 B, AZ-1 , Bor-C, Boralite, Encilite, FZ-1 , LZ-105, Mutinaite, NU-4, NU-5, Silicalite, TS-1 , TSZ, TSZ-III, TZ-01 , USC-4, USI-108, ZBH, ZKQ-1 B, and ZMQ-TB, with ZSM-5 being particularly preferred. Useful FER isotypes include Ferrierite, [Si-0]-FER, FU-9, ISI-6, Monoclinic ferrierite, NU-23, Sr-D, and ZSM-35. Useful BEA isotypes include Beta, [Ti-Si-O]- ^*BEA, CIT-6, and Tschernichite. Typical Si0₂/Al₂0₃ mole ratios for such materials are 30 to 100 and typical Si0₂/Fe₂0₃ mole ratios are 20 to 300 such as 20 to 100.

Preferably, the BEA framework contains either exchanged iron or is an iron isomorphous BEA molecular structure (also referred to as BEA-type ferrosilicate), with iron isomorphous BEA molecular structure being particularly preferred. In certain preferred embodiments, the BEA-type ferrosilicate molecular structure is a crystalline silicate having (1 ) an iron-containing BEA-framework structure that has a Si0₂/Fe₂0₃ mol ratio of about 20 to about 300, and/or (2) at least 80% of the contained iron as isolated iron ions Fe³⁺ in a fresh state. Preferred BEA-type ferrosilicates useful in the present invention have a composition represented by following formula: (x+y) M(2 n₎0 · x Fe₂0₃ · y Al₂0₃ · z Si0₂ · w H₂0 wherein n is an atomic value of cation M; x, y, and z represent mol fractions of Fe₂0₃, Al₂0₃ and Si0₂, respectively; x+y+z=l; w is a number of at least 0; z/x is 20 to 300, y may be 0, and optionally z/y is at least 1 00.

Preferably, iron-containing BEA-framework structure that has a Si0₂/Fe₂0₃ mol ratio of about 25 to about 300, about 20 to about 150, about 24 to about 150, about 25 to about 100, or about 50 to about 80. The upper limit of log (Si0₂/Al₂0₃) by mol is not particularly limited, provided that the log(Si0₂/AI₂0₃) by mol is at least 2 (i.e., the Si0₂/Al₂0₃ ratio by mol is at least 100). The log(Si0₂/AI₂0₃) by mol is preferably at least 2.5 (i.e., the Si0₂/Al₂0₃ ratio by mol is at least 310), more preferably at least 3 (i.e., the Si0₂/Al₂0₃ ratio by mol is at least 1 ,000). When the log(Si0₂/AI₂0₃) by mol exceeds 4 (i.e., the Si0₂/Al₂0₃ ratio by mol becomes at least 10,000).

In certain embodiments, the Fe-BEA aluminosilicate molecular sieve is pre-aged. Pre-aged Fe- BEA aluminosilicate can produce results substantially better than conventional Fe-BEA. Accordingly, instead of the more conventional processing of aging at 500 ^SC for 1 hour, the Fe-BEA aluminosilicate is preferably aged at 600 - 900 ^SC, preferably 650 - 850 ^SC, more preferably 700 - 800 ^SC, and even more preferably 725 - 775 ^SC, for 3 - 8 hours, preferably 4 - 6 hours, more preferably from 4.5 - 5.5 hours, and even more preferably from 4.75 - 5.25 hours. Embodiments using pre-aged Fe-BEA aluminosilicate are advantageous in applications in which the formation of N₂0 is undesirable.

In certain embodiments, the iron is present in the molecular sieve material at a concentration of about 0.1 to about 10 weight percent (wt%) based on the total weight of the molecular sieve, for example from about 0.5 wt% to about 5 wt%, from about 0.5 to about 1 wt%, from abouti to about 5 wt%, about 2 wt% to about 4 wt%, and about 2 wt% to about 3 wt %. Iron may be incorporated into the molecular sieves for use in the present invention using techniques well known in the art, including liquid-phase exchange or solid-ion exchange or by an incipient wetness process. Such materials are referred to herein as iron-containing or iron-promoted molecular sieves. For manufacture of iron-containing aluminosilicate zeolites see Journal of Catalysis 232(2) 318-334 (2005); EP2072128; and

WO2009/023202 which are incorporated herein by reference. The catalyst composition of the present invention can be prepared by blending the vanadium component and the molecular sieve component. The type blending technique is not particularly limited. In certain embodiments, a Ti0₂/W0₃ suspension is prepared to which V₂0₅ powder and iron-promoted molecular sieve powder are added. The resulting suspension can be formulated as a washcoat or can be dried and calcined in a powder form which is then used to prepare a washcoat or an extrudable material.

The catalytic zeolites described herein can promote the reaction of a reductant, preferably ammonia, with nitrogen oxides to selectively form elemental nitrogen (N₂) and water (H₂0) vis-a-vis the competing reaction of oxygen and ammonia. In one embodiment, the catalyst can be formulated to favor the reduction of nitrogen oxides with ammonia (i.e., and SCR catalyst). In another embodiment, the catalyst can be formulated to treat ammonia that is not consumed in the SCR catalyst reaction (i.e. the ammonia slip). Here, the ammonia slip catalyst (ASC) is formulated to favor the oxidation of ammonia with oxygen. In yet another embodiment, an SCR catalyst and an ASC catalyst are used in series, wherein both catalysts comprise the catalyst blend described herein, and wherein the SCR catalyst is upstream of the ASC catalyst.

In certain embodiments, the ASC catalyst is disposed as a top layer on an oxidative under-layer, wherein the under-layer comprises a platinum group metal (PGM) catalyst or a non-PGM catalyst. In certain embodiments, the ASC catalyst is an extruded honeycomb brick or applied to a substrate, preferably substrates that are designed to provide large contact surface with minimal backpressure, such as flow-through metallic or cordierite honeycombs. For example, a preferred substrate has between about 25 and about 300 cells per square inch (CPSI) to ensure low backpressure. Achieving low backpressure is particularly important to minimize the ASC catalyst's effect on the low-pressure EGR performance. The ASC catalyst can be applied to the substrate as a washcoat, preferably to achieve a loading of about 0.3 to 3.5 g/in³. To provide further NO_x conversion, the front part of the substrate can be coated with just SCR coating, and the rear coated with SCR and ASC catalyst which can further include Pt or Pt/Pd on an alumina support.

According to another aspect of the invention, provided is a method for the selective catalytic reduction of NO_x compounds or oxidation of NH₃ in an exhaust gas, which comprises contacting the exhaust gas with a catalyst blend described herein for a time sufficient to reduce the level of NO_x and/or NH₃ compounds in the exhaust gas. In certain embodiments, nitrogen oxides are reduced in the presence of a catalyst blend with the reducing agent at a temperature of at least about 100 ^SC. In certain embodiments, NO_x compounds are reduced at a temperature of about 200 ^SC to about 650 ^SC.

Embodiments utilizing temperatures greater than about 450 ^SC are particularly useful for treating exhaust gases from a heavy and light duty diesel engines that are equipped with an exhaust system comprising (optionally catalyzed) diesel particulate filters which are regenerated actively, e.g. by injecting

hydrocarbon into the exhaust system upstream of the filter, wherein the zeolite catalyst for use in the present invention is located downstream of the filter. In other embodiments, the molecular sieve SCR catalyst is incorporated on a filter substrate. Methods of the present invention may comprise one or more of the following steps: (a) accumulating and/or combusting soot that is in contact with the inlet of a catalytic filter; (b) introducing a nitrogenous reducing agent into the exhaust gas stream prior to contacting the catalytic filter, preferably with no intervening catalytic steps involving the treatment of NO_x and the reductant; (c) generating NH₃ over a NO_x adsorber catalyst, and preferably using such NH₃ as a reductant in a downstream SCR reaction; (d) contacting the exhaust gas stream with a DOC to oxidize hydrocarbon based soluble organic fraction (SOF) and/or carbon monoxide into C0₂, and/or oxidize NO into N0₂, which in turn, may be used to oxidize particulate matter in particulate filter; and/or reduce the particulate matter (PM) in the exhaust gas; (e) contacting the exhaust gas with one or more flow-through SCR catalyst device(s) in the presence of a reducing agent to reduce the NO_x concentration in the exhaust gas; and (f) contacting the exhaust gas with an ASC catalyst, preferably downstream of the SCR catalyst to oxidize most, if not all, of the ammonia prior to emitting the exhaust gas into the atmosphere or passing the exhaust gas through a recirculation loop prior to exhaust gas entering/re-entering the engine.

The reductant (also known as a reducing agent) for SCR processes broadly means any compound that promotes the reduction of NO_x in an exhaust gas. Examples of reductants useful in the present invention include ammonia, hydrazine or any suitable ammonia precursor, such as urea

((NH₂)₂CO), ammonium carbonate, ammonium carbamate, ammonium hydrogen carbonate or ammonium formate, and hydrocarbons such as diesel fuel, and the like. Particularly preferred reductant, are nitrogen based, with ammonia being particularly preferred. In certain embodiments, the reductant can be a hydrocarbon, such as methane, diesel fuel, or the like. In certain embodiments, all or at least a portion of the nitrogen-based reductant, particularly NH₃, can be supplied by a NO_x adsorber catalyst (NAC), a lean NO_x trap (LNT), or a NO_x storage/reduction catalyst (NSRC), disposed upstream of the SCR catalyst, e.g., a SCR catalyst of the present invention disposed on a wall-flow filter. NAC components useful in the present invention include a catalyst combination of a basic material (such as alkali metal, alkaline earth metal or a rare earth metal, including oxides of alkali metals, oxides of alkaline earth metals, and combinations thereof), and a precious metal (such as platinum), and optionally a reduction catalyst component, such as rhodium. Specific types of basic material useful in the NAC include cesium oxide, potassium oxide, magnesium oxide, sodium oxide, calcium oxide, strontium oxide, barium oxide, and combinations thereof. The precious metal is preferably present at about 10 to about 200 g/ft³, such as 20 to 60 g/ft³. Alternatively, the precious metal of the catalyst is characterized by the average concentration which may be from about 40 to about 1 00 grams/ft³.

Under certain conditions, during the periodically rich regeneration events, NH₃ may be generated over a NO_x adsorber catalyst. The SCR catalyst downstream of the NO_x adsorber catalyst may improve the overall system NO_x reduction efficiency. In the combined system, the SCR catalyst is capable of storing the released NH₃ from the NAC catalyst during rich regeneration events and utilizes the stored NH₃ to selectively reduce some or all of the NO_x that slips through the NAC catalyst during the normal lean operation conditions.

In other embodiments, a nitrogenous reducing agent or precursor thereof, is introduced into the exhaust gas flow stream, preferably upstream of an SCR catalyst and downstream of a diesel oxidation catalyst. The introduction of this reducing agent can be accomplished by an injector, spray nozzle, or similar device.

Methods of the present invention can be performed on an exhaust gas derived from a combustion process, such as from an internal combustion engine (whether mobile or stationary), a gas turbine and coal or oil fired power plants. The method may also be used to treat gas from industrial processes such as refining, from refinery heaters and boilers, furnaces, the chemical processing industry, coke ovens, municipal waste plants and incinerators, etc. In a particular embodiment, the method is used for treating exhaust gas from a vehicular lean burn internal combustion engine, such as a diesel engine, a lean-burn gasoline engine or an engine powered by liquid petroleum gas or natural gas.

According to a further aspect, the invention provides an exhaust system for a vehicular lean burn internal combustion engine, which system comprising a conduit for carrying a flowing exhaust gas, a source of nitrogenous reductant, and a catalyst blend described herein. The system can include a controller for the metering the nitrogenous reductant into the flowing exhaust gas only when it is determined that the catalyst blend is capable of catalyzing NO_x reduction at or above a desired efficiency, such as at above 100 ^SC, above 150 ^SC or above 175 ^SC. The determination by the control means can be assisted by one or more suitable sensor inputs indicative of a condition of the engine selected from the group consisting of: exhaust gas temperature, catalyst bed temperature, accelerator position, mass flow of exhaust gas in the system, manifold vacuum, ignition timing, engine speed, lambda value of the exhaust gas, the quantity of fuel injected in the engine, the position of the exhaust gas recirculation (EGR) valve and thereby the amount of EGR and boost pressure.

In a particular embodiment, metering is controlled in response to the quantity of nitrogen oxides in the exhaust gas determined either directly (using a suitable NO_x sensor) or indirectly, such as using pre- correlated look-up tables or maps-stored in the control means-correlating any one or more of the abovementioned inputs indicative of a condition of the engine with predicted NO_x content of the exhaust gas. The metering of the nitrogenous reductant can be arranged such that 60% to 200% of theoretical ammonia is present in exhaust gas entering the SCR catalyst calculated at 1 :1 NH₃/NO and 4:3 NH₃/N0₂. The control means can comprise a pre-programmed processor such as an electronic control unit (ECU).

In a further embodiment, a diesel oxidation catalyst for oxidizing nitrogen monoxide in the exhaust gas to nitrogen dioxide can be located upstream of a point of metering the nitrogenous reductant into the exhaust gas. In one embodiment, the diesel oxidation catalyst is adapted to yield a gas stream entering the SCR zeolite catalyst having a ratio of NO to N0₂ of from about 4:1 to about 1 :3 by volume, e.g. at an exhaust gas temperature at oxidation catalyst inlet of 250 ^SC to 450 ^SC. In another embodiment, the NO to N0₂ is maintained at a ratio of about 1 :2 to about 1 :5 by volume. The diesel oxidation catalyst can include at least one platinum group metal (or some combination of these), such as platinum, palladium, or rhodium, coated on a flow-through monolith substrate. In one embodiment, the at least one platinum group metal is platinum, palladium, or a combination of both platinum and palladium. The platinum group metal can be supported on a high surface area washcoat component such as alumina, a zeolite such as an aluminosilicate zeolite, silica, non-zeolite silica alumina, ceria, zirconia, titania or a mixed or composite oxide containing both ceria and zirconia.

In a further embodiment, a suitable filter substrate is located between the diesel oxidation catalyst and the SCR catalyst. Filter substrates can be selected from any of those mentioned above, e.g. wall flow filters. Where the filter is catalyzed, e.g. with an oxidation catalyst of the kind discussed above, preferably the point of metering nitrogenous reductant is located between the filter and the SCR catalyst blend. Alternatively, if the filter is un-catalyzed, the means for metering nitrogenous reductant can be located between the diesel oxidation catalyst and the filter.

In a further embodiment, the catalyst blend for use in the present invention is coated on a filter located downstream of the oxidation catalyst. Where the filter includes the catalyst blend, the point of metering the nitrogenous reductant is preferably located between the oxidation catalyst and the filter.

In a further aspect, there is provided a vehicular lean-burn engine comprising an exhaust system according to the present invention. The vehicular lean burn internal combustion engine can be a diesel engine, a lean-burn gasoline engine or an engine powered by liquid petroleum gas or natural gas.

As used herein, the term "consists essentially of with respect to a catalytic composition means that the composition contains the named catalytic components but does not contain additional components that materially affect the basic and novel characteristics of the claimed invention. That is, the catalytic composition does not include additional components that would otherwise serve as a catalyst for the intended reaction or serve to enhance the basic catalytic nature of the claimed catalyst.

EXAMPLES

Example 1 : Catalyst Preparation

A catalyst composition was prepared by blending iron exchanged MFI aluminosilicate with a V₂0₅ - Ti0₂/W0₃ suspension. The resulting composition contained about 20 weight percent iron exchanged MFI aluminosilicate based on the combined weight of the iron exchanged MFI aluminosilicate and V₂0₅ - Ti0₂/W0₃ solids. A similar process was followed to prepare a catalyst containing 5 weight percent iron exchanged MFI aluminosilicate; a catalyst containing 20 weight percent iron exchanged FER aluminosilicate; a catalyst containing 5 weight percent iron exchanged FER aluminosilicate; a catalyst containing 20 weight percent a BEA ferrosilicate; and a catalyst containing 10 weight percent a BEA ferrosilicate.

These catalysts blends were formed into an extrudable mass, kneaded, strained, and then extruded to form 1 inch diameter x 140 mm honeycomb bricks.

Additionally, catalyst material containing 20 weight percent iron exchanged MFI aluminosilicate was formed into an extrudable mass, kneaded, strained, and then extruded to form 10.5 inch diameter x 5.0 inch 400/1 1 honeycomb bricks and also 10.5 inch diameter x 7.0 inch 400/1 1 honeycomb bricks.

Example 2: Catalyst Performance (varying N0₂ levels)

An extruded 1 inch diameter x 140 mm honeycomb brick containing a blend of iron exchanged MFI aluminosilicate and V₂0₅ - Ti0₂/W0₃ (20 wt. % Fe-MFI), was exposed to a simulated diesel engine exhaust gas at a space velocity of about 60,000/hour. The simulated exhaust gas contained about 9.3 wt. % 0₂, about 7.0 wt. % H₂0, about 1 00 ppm NO_x (NO only) about 100 ppm NH₃, and the balance N₂. The catalyst's capacity for NO_x conversion was determined at temperatures of 180, 215, 250, 300, 400, and 500 °C.

For comparison, a similar catalytic brick was prepared using only V₂0₅ - Ti0₂/W0₃. The comparative sample was also tested for NO_x conversion under similar conditions.

The NO_x conversion data for these fresh samples (i.e., non-aged) is provided in Figure 1 . Here, the data shows that at 0% N0₂, a catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ results in better of NOx conversion at high temperatures compared to a catalyst containing only V₂0₅ - Ti0₂/W0₃.

This test was repeated except that the NOx stream was adjusted to contain 35 weight percent N0₂. The NO_x conversion data for these fresh samples is provided in Figure 2. Here, the data shows that at 35% N0₂, a catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ results in better of NOx conversion compared to a catalyst containing only V₂0₅ - Ti0₂/W0₃ across a wide range of temperatures.

This test was repeated again except that the NOx stream was adjusted to contain 65 weight percent N0₂. The NO_x conversion data for these fresh samples is provided in Figure 3. Here, the data shows that at 65% N0₂, a catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ results in better of NOx conversion compared to a catalyst containing only V₂0₅ - Ti0₂/W0₃ across a wide range of temperatures.

Example 3: Catalyst Performance (post-hydrothermal aging)

An extruded 1 inch diameter x 140 mm honeycomb fresh brick containing a blend of iron exchanged MFI aluminosilicate and V₂0₅ - Ti0₂/W0₃ (20 weight percent Fe-MFI), was aged for 100 hours at 580 °C. Three additional fresh bricks were also aged, each at one of the following conditions: 100 hours at 580 °C and 10% H₂0; 100 hours at 650 °C; and 100 hours at 650 °C and 10% H₂0.

For comparison, two similar catalytic bricks were prepared using only V₂0₅ - Ti0₂/W0₃. Each of the comparative samples were aged at one of the following conditions: 100 hours at 580 °C and 100 hours at 650 °C.

All of the bricks were exposed to a simulated diesel engine exhaust gas at a space velocity of about 60,000/hour. The simulated exhaust gas contained about 9.3 wt. % 0₂, about 7.0 wt. % H₂0, about 100 ppm NO_x (NO only) about 100 ppm NH₃, and the balance N₂. The catalyst's capacity for NO_x conversion was determined at temperatures of 180, 215, 250, 300, 400, and 500 °C.

The NO_x conversion data for these aged samples is provided in Figure 4. Here, the data shows that the catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ were much more hydrothermally stable compared to catalyst containing only V₂0₅ - Ti0₂/W0₃, particular under harsh aging conditions.

Example 4: Comparative Catalyst Performance

An extruded 1 inch diameter x 140 mm honeycomb brick containing a blend of iron exchanged MFI aluminosilicate and V₂0₅ - Ti0₂/W0₃ (20 weight percent Fe-MFI), was exposed to a simulated diesel engine exhaust gas at a space velocity of about 60,000/hour. The simulated exhaust gas contained about 9.3 wt. % 0₂, about 7.0 wt. % H₂0, about 100 ppm NO_x (65 weight percent N0₂), about 100 ppm NH₃, and the balance N₂. The catalyst's capacity for NO_x conversion was determined at temperatures of 180, 215, 250, 300, 400, and 500 °C.

Another extruded 1 inch diameter x 140 mm honeycomb brick, but containing a blend of iron exchanged FER aluminosilicate and V₂0₅ - Ti0₂/W0₃ (20 weight percent Fe-FER), was exposed to a simulated diesel engine exhaust gas at a space velocity of about 60,000/hour. The simulated exhaust gas contained about 9.3 wt. % 0₂, about 7.0 wt. % H₂0, about 1 00 ppm NO_x (65 weight percent N0₂), about 1 00 ppm NH₃, and the balance N₂. The catalyst's capacity for NO_x conversion was determined at temperatures of 180, 215, 250, 300, 400, and 500 °C.

For comparison, a similar catalytic brick was prepared using only V₂0₅ - Ti0₂/W0₃. The comparative sample was also tested for NO_x conversion under similar conditions.

The ΝΟχ conversion data for these samples is provided in Figure 5. Here, the data shows that at 65% N0₂, a catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ results in better of NOx conversion at high temperatures compared to a catalyst containing a blend of Fe-FER and V₂0₅ - Ti0₂/W0₃, and that a catalyst based on a blend of Fe-MFI and V₂0₅ - Ti0₂/W0₃ results in better of NOx conversion at high temperatures compared to a catalyst containing only V₂0₅ - Ti0₂/W0₃.

Claims

1 . A catalyst composition for treating exhaust gas comprising a blend of a first component and second component, wherein the first component is an aluminosilicate or ferrosilicate molecular sieve component wherein the molecular sieve is either in H+ form or is ion exchanged with one or more transition metals, and the second component is a vanadium oxide supported on a metal oxide support selected from alumina, titania, zirconia, ceria, silica, and combinations thereof.

2. The catalyst of claim 1 , wherein the molecular sieve has a framework selected from MFI, BEA, and FER.

3. The catalyst of claim 2, wherein the molecular sieve is H+/MFI aluminosilicate.

4. The catalyst of claim 1 , wherein the molecular sieve is Fe ion exchanged MFI, BEA, or FER

aluminosilicate.

5. The catalyst of claim 4, wherein molecular sieve comprises about 1 to about 10 weight percent ion exchanged Fe.

6. The catalyst of claim 1 , wherein the molecular sieve is a BEA ferrosilicate.

7. The catalyst of claim 1 , wherein the metal oxide support is titanium oxide.

8. The catalyst composition of claim 1 , wherein the second component further comprises tungsten

oxide.

9. The catalyst composition of claim 1 , wherein the second component further comprises iron vanadate.

10. The catalyst composition of claim 1 , wherein the first component and second component are present in the blend in a respective weight ratio of about 5:95 to about 40:60.

1 1 . The catalyst composition of claim 1 , wherein the blend comprises about 0.5 to about 5 weight percent the vanadium oxide based on the weight of the first and second components.

12. A catalytic washcoat comprising a catalyst according to claim 1 , further comprising one or more fillers, binders, processing aides, water, and dopants.

13. A catalytic article comprising a substrate coated with or incorporating a catalyst according to claim 1 , wherein the substrate is selected from a metal flow-through substrate, a ceramic flow-through substrate, a wall-flow filter, a sintered metal filter, a partial filter, and an extruded catalyst honeycomb.

14. The catalytic article of claim 13, further comprising a washcoat having a second catalyst composition for selectively reducing NO_x and/or for oxidizing NH₃.

15. The catalytic article of claim 14, wherein said second catalyst composition is selected from (a)

catalyst blends according to claim 1 , (b) a transition metal promoted molecular sieve, (c) a platinum group metal catalyst, or (d) a vanadium-based catalyst.

16. The catalyst article of claim 13, wherein the substrate comprises a first layer containing a platinum group metal for oxidizing ammonia and a second layer comprising the catalyst of claim 1 , wherein the first layer is disposed directly on or within the substrate and the second layer covers the first layer.

17. A system for treating exhaust gas comprising a selective catalytic reduction (SCR) catalyst upstream of an ammonia slip catalyst (ASC), wherein in at least one of said SCR and ASC catalysts comprise a catalyst according to claim 1 .

18. The system of claim 17, further comprising a diesel oxidation catalyst having a platinum group metal disposed upstream of said selective catalytic reduction catalyst.

19. A method for treating an exhaust gas comprising the steps of:

a. contacting an exhaust gas stream containing NO_x and/or NH₃ in the presence of a catalyst according to claim 1 ; and

b. converting at least a portion of said NO_x to N₂ and/or converting at least a portion of NH₃ to at least one of N₂ and N0₂.

20. The method of claim 19, wherein said exhaust gas comprises a ratio of NO to N0₂ from about 4:1 to about 1 :3 by volume.