BR112019010118B1 - EXHAUST GAS TREATMENT SYSTEM - Google Patents

Abstract

The present invention relates to a catalyst, preferably for the selective catalytic reduction of NOx, for the oxidation of ammonia, for the oxidation of NO and for the oxidation of a hydrocarbon, comprising a washcoat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises a platinum group metal supported on a metal oxide support material and one or more of an oxidic compound of V, a oxidic compound of W and a zeolite material comprising one or more of Cu and Fe.

Description

FIELD OF THE INVENTION

[001] The present invention relates to a tetrafunctional catalyst for the oxidation of nitrogen monoxide (NO), the oxidation of a hydrocarbon (HC), the oxidation of ammonia (NH3) and the selective catalytic reduction of oxides of nitrogen (NOx). Furthermore, the present invention relates to a system for treating an exhaust gas, the system comprising the tetra-functional catalyst, wherein the tetra-functional catalyst is preferably located upstream of a catalyzed soot filter. Furthermore, the present invention relates to a process for preparing the tetra-functional catalyst.

BACKGROUND OF THE INVENTION

[002] In general, all heavy duty exhaust gas treatment systems, particularly in North America, Japan and Europe, are equipped with a diesel particulate filter due to regulatory requirements. Thus, very economical solutions have great economic potential due to the pressure to minimize costs. With the drive to reduce CO2 emissions, engine NOx levels are increasing to improve fuel economy, which creates the need for new technical solutions to maintain legal emission limits. Consequently, many original equipment manufacturers (OEMs) are looking to increase NOx emissions without engine use, which is a side effect of OEMs trying to reduce their CO2 emissions, while increasing fuel economy due to looming regulations. These higher NOx emissions can be too great a burden for a EU VI/EPA13 standard system. Thus, new layouts are needed to meet the stringent new regulations. A closed-coupled catalyst for selective catalytic reduction (SCR), which can help increase the NOx reduction obligation, especially in NOx with high engine output, would be one such possible new layout.

[003] However, for any new exhaust gas treatment system, the need for a closed diesel particulate filter would still exist. The soot collected in the filter must be converted by a suitable process into gaseous substances (generally CO2), so that the filter does not become clogged. For this reason, diesel oxidation catalysts (DOC) are normally installed upstream of the filter containing relatively high amounts of expensive platinum group metals (PGM). DOC can be used to catalytically burn diesel fuel. A temperature is then produced at which filter regeneration begins or is accelerated and made more efficient. However, during intervals when no fuel is injected to generate a temperature over the catalyzed soot filter (CSF), NO2 generally functions as an oxidant to oxidize the soot in the CSF. This alternative solution would be able to act as a DOC fuel burner as well as an upstream SCR catalyst. Furthermore, this approach can be combined with the DeNOx activity of the material by reacting the NOx with ammonia.

[004] Thus, a major disadvantage of such an approach, where the DOC is replaced by an SCR catalyst, is the loss of NO2 production upstream of a CSF for passive soot regeneration. Furthermore, due to the injection of ammonia upstream of the PGM-rich CSF for DeNOx, the selectivity for N2O may increase.

[005] WO 2015/189680 A1 refers to base metal catalysts, systems and methods of treating emissions. More specifically, embodiments of said application are directed to catalysts, systems and methods having a base metal catalyst positioned upstream of a particulate filter and a selective catalytic reduction (SCR) catalyst. In systems where hydrocarbons (e.g. fuel) are periodically injected upstream of the base metal catalyst, the base metal catalyst generates an exotherm over a temperature range of 300 °C to 650 °C to regenerate the downstream particulate filter that collected soot. In particular, the catalyst of said application is substantially free of platinum group metals. As outlined above, said document also relates to a system for treating a lean combustion engine exhaust gas stream, wherein the system particularly comprises the base metal catalyst disposed on a carrier substrate and a particulate filter and a first SCR catalyst located downstream of the base metal catalyst. Furthermore, the exhaust gas treatment system may further comprise a platinum group metal (PGM) oxidation catalyst downstream of the base metal catalyst and upstream of the particulate filter.

[006] Especially in view of the disadvantages as described above with respect to an approach based on conventionally used components such as catalysts and filters, it was an objective of the present invention to establish a new concept that comes close to mitigating the need for a DOC in an exhaust gas treatment system as conventionally used. More specifically, it was an object of the present invention to provide a new catalyst that is capable of performing in a multifunctional manner, in particular with regard to the four functions of NO oxidation, hydrocarbon oxidation, NH3 oxidation and selective catalytic reduction. of NOx (DeNOx). In particular, by oxidation of a hydrocarbon, a favorable temperature (i.e. an exotherm) is generated which can heat a catalyzed soot filter located downstream of the catalyst. Furthermore, the present invention aims at designing new post-treatment systems. In particular, it was an object of the present invention to provide an exhaust gas treatment system comprising the multifunctional catalyst, preferably as a tetrafunctional catalyst. More specifically, it was an objective of the present invention, with regard to the exhaust gas treatment system, to make redundant the use of a diesel oxidation catalyst (DOC), in particular upstream of a catalyzed soot filter. (CSF).

DESCRIPTION OF THE INVENTION

[007] Thus, it has surprisingly been found that a catalyst comprising a washcoat comprising one or more layers, wherein the washcoat is disposed on a substrate and wherein the washcoat comprises i) a metal of the platinum group supported on a metal oxide support material and ii) one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe, can function in the reduction selective catalysis of NOx, in the oxidation of ammonia, in the oxidation of NO and in the oxidation of a hydrocarbon.

[008] In particular, it was surprisingly found that the catalyst of the invention is capable of minimizing both NH3 slippage and HC slippage and simultaneously can produce NO2 for the passive regeneration of a CSF, as well as reduce NOx when a reductant is present. Furthermore, it has surprisingly been found that the catalyst of the invention can reduce NOx as well as possibly produce a favorable temperature (i.e., an exotherm) for CSF regeneration, especially when fuel is dosed (in the engine cylinder or in the tube). exhaust) and is burned in the catalytic converter. Alternatively, the exotherm can be produced exclusively on the platinum group metal supported on a metal oxide support material, in particular if no other material is upstream of the catalyst of the invention which is capable of oxidizing the HC. The catalyst of the invention can also act as a DeNOx catalyst when a suitable dosage of a reductant (e.g. ammonia or an alternative substance that releases ammonia) is applied to the exhaust gas before reaching the catalyst. In other words, the catalyst of the invention can oxidize NH3 to limit ammonia slippage (e.g. in a CSF located downstream) which simultaneously acts as a NO oxidation catalyst for soot regeneration downstream in the filter.

[009] The catalyst of the invention may comprise a wash coat comprising one or more layers, wherein the wash coat is preferably uniformly disposed on the substrate. In view of an exhaust gas treatment system, the catalyst of the invention can be arranged after the catalyst for burning fuel that does not contain PGM, for example an upstream SCR catalyst, to oxidize possible slippage of NH3. This surprisingly results in N2O production along the CSF and also a good cleaning of the HC slip. Furthermore, the PGM contained in the catalyst of the invention can also be used to oxidize NO to NO2, aiding passive regeneration over CSF, when there is no NH3 present. When dosing at lower NSRs, the NH3 slippage on the catalyst of the invention containing PGM would be negligible and one can thus employ the catalyst of the invention to generate NO2 for passive regeneration in the CSF.

[010] Accordingly, the present invention relates to a catalyst comprising a wash coating comprising one or more layers, the wash coating being disposed on a substrate, wherein the wash coating comprises i) a metal of the platinum group supported on a metal oxide support material, and ii) one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe.

[011] Thus, it is preferred that the catalyst be used for one or more of the selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of NO and the oxidation of a hydrocarbon.

[012] With regard to the wash coat, there are particular restrictions on the number of layers that the wash coat comprises. It is preferred that the wash coat comprises one layer, two layers or three layers.

[013] With regard to the platinum group metal supported on a metal oxide, any suitable platinum group metal can be employed, provided that it can be supported on a metal oxide support material, preferably the platinum group metal supported on a metal oxide support material is one or more of Ru, Rh, Pd, Os, Ir and Pt. More preferably, the platinum group metal supported on a metal oxide support material metal oxide is one or more of Rh, Pd and Pt, more preferably one or more of Pd and Pt, and most preferably Pt.

[014] Regarding the metal oxide support material, any suitable metal oxide support material can be used, provided that it can be used as a support for the platinum group metal, preferably the support material of metal oxide is one or more of alumina, zirconia-alumina, silica-alumina, titania, zirconia-titania, and ceria. More preferably, the metal oxide support material is one or more of alumina, silica-alumina and zirconia-alumina, most preferably zirconia-alumina.

[015] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises iii ) platinum supported on zirconia-alumina, and iv) one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe.

[016] With regard to the zeolite material as such, which may be contained in the catalyst of the invention, no restrictions apply according to the present invention, such that any conceivable zeolite material may be contained therein. However, it is preferred that the catalyst wash coat of the invention comprises a zeolite material.

[017] According to the present invention, it is particularly preferred that the structural structure of the zeolite material comprises a tetravalent element. It is particularly preferred, according to the present invention, that the zeolite material comprises a tetravalent element Y, which is one or more of Si, Sn, Ti, Zr and Ge, preferably Si. structural element of the zeolite material comprises a trivalent element X. It is particularly preferred according to the present invention that the zeolite material comprises one or more of B, Al, Ga and In, preferably Al.

[018] Furthermore, with regard to the structural structure of the zeolite material that may be contained in the catalyst of the invention, once again no particular restrictions apply, such that the zeolite material may have any type of structural structure. Generally speaking, it is conceivable that the structural structure type of the zeolite material is one of the following: ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR, AFS, AFT, AFV, AFX, AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AVL, AWO, AWW, BCT, BEA, BEC, BIK, BOF, BOG, BOZ, BPH, BRE, BSV, CAN, CAS, CDO, CFI, CGF, CGS, CHA, -CHI, -CLO, CON, CSV, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI, EEI, EMT, EON, EPI, ERI, ESV, ETR, EUO, *-EWT, EZT, FAR, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFO, IFR, -IFU, IFW, IFY, IHW, IMF, IRN , IRR, -IRY, ISV, ITE, ITG, ITH, *-ITN, ITR, ITT, -ITV, ITW, IWR, IWS, IWV, IWW, JBW, JNT, JOZ, JRY, JSN, JSR, JST, JSW , KFI, LAU, LEV, LIO, -LIT, LOS, LOV, LTA, LTF, LTJ, LTL, LTN, MAR, MAZ, MEI, MEL, MEP, MER, MFI, MFS, MON, MOR, MOZ, *MRE , MSE, MSO, MTF, MTN, MTT, MTW, MVY, MWF, MWW, NAB, NAT, NES, NON, NPO, NPT, NSI, OBW, OFF, OKO, OSI, OSO, OWE, -PAR, PAU, PCR, PHI, PON, POS, PSI, PUN, RHO, - RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAF, SAO, SAS, SAT, SAV, SBE, SBN, SBS, SBT, SEW , SFE, SFF, SFG, SFH, SFN, SFO, SFS, *SFV, SFW, SGT, SIV, SOD, SOF, SOS, SSF, *-SSO, SSY, STF, STI, *STO, STT, STW, - SVR, SVV, SZR, TER, THO, TOL, TON, TSC, TUN, UEI, UFI, UOS, UOV, UOZ, USI, UTL, UWY, VET, VFI, VNI, VSV, WEI, -WEN, YUG, ZON , mixtures of two or more of these, and mixed types of two or more of these. According to the present invention, it is preferable that the structural structure type of the zeolite material is one of AEI, GME, BEA, CHA, FAU, FER, HEU, LEV, MEI, MEL, MFI or MOR, more preferably, one of AEI, GME, CHA, MFI, BEA, FAU or MOR, more preferably one of CHA, AEI or BEA, more preferably one of CHA and/or AEI, and most preferably CHA .

[019] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises v ) platinum supported on zirconia-alumina, and vi) a zeolite material having CHA-type structural structure and comprising one or more of Cu and Fe.

[020] Regarding the zeolite material, it is preferable that it is in its calcined state. According to the present invention, the zeolite material can comprise any other chemical elements, as long as these elements can establish one or more of the type of structure defined above. However, it is preferred that the backbone of the zeolite material comprises Si, Al, O and H and wherein at least 99.0% by weight, preferably at least 99.5% by weight, more preferably, at least 99.9% by weight of the zeolite material structural structure consists of Si, Al, O and H.

[021] With regard to the oxidic compound of V that may be contained in the wash coating of the catalyst of the invention, no restrictions apply to the chemical nature of said compound, provided that it comprises an oxygen atom bonded to a vanadium atom. It is preferred that the oxidic compound of V is one or more of an ammonium vanadate, a sodium vanadate, an iron vanadate, vanadium pentoxide and vanadium pentoxide stabilized with iron oxide. In accordance with the present invention, a vanadate may be a compound containing a vanadium oxoanion generally in its highest oxidation state of +5. The simplest vanadate may be the anion VO43- (orthovanadate), which is present, for example, in sodium orthovanadate and in solutions of V2O5 in a strong base (pH > 13). Other vanadates can be the V2O74- anion and the V3O93- anion.

[022] With regard to the oxidic compound of W that may be contained in the wash coating of the catalyst of the invention, once again no restrictions apply to the chemical nature of said compound, provided that it comprises an oxygen atom bonded to an atom of tungsten. It is preferred that the oxidic compound of W is one or more of an ammonium tungstate, a sodium tungstate and tungsten trioxide. According to the present invention, a tungstate can be a compound containing a tungsten oxoanion or it is a tungsten-containing mixed oxide. The simplest tungstate ion can be the WO42- (orthotungstate) anion.

[023] Furthermore, it is preferable, according to the present invention, that one or more oxidic compounds of V and the oxidic compound of W are supported on one or more titania and zirconia-titania, preferably on titania. Thus, it is particularly preferred that the oxidic compound of V is supported on titania.

[024] When the wash coating comprises one or more of an oxidic compound of V and an oxidic compound of W, no restriction applies as to the amount of one or more of an oxidic compound of V and an oxidic compound of W that can be contained in the wash liner. Thus, any suitable amount of one or more of an oxidic compound of V and an oxidic compound of W can be contained in the wash coat. In this regard, the amount of an oxidic compound of V is calculated as V2O5 and the amount of an oxidic compound of W is calculated as WO3. Thus, the wash coating may comprise an oxidic compound of V, calculated as V2O5, in the range of 0.1 to 10% by weight, preferably from 1 to 9% by weight, more preferably from 2 to 8 % by weight, more preferably from 3 to 7% by weight, more preferably from 3.5 to 6% by weight, most preferably from 4 to 5% by weight, based on total weight of the wash coat.

[025] Furthermore, the wash coating may comprise an oxidic compound of W, calculated as WO3, in the range of 1 to 20% by weight, preferably from 3 to 18% by weight, more preferably from 5 to 16% by weight, more preferably from 7 to 14% by weight, most preferably from 9 to 13% by weight, based on the total weight of the wash liner.

[026] Furthermore, it is preferred that the wash coating of the catalyst of the invention comprises a zeolite material comprising one or more of Cu and Fe. With regard to the zeolite material comprising one or more of Cu and Fe, it is not applies restriction on how the one or more of Cu and Fe is comprised in the zeolite material. Thus, the one or more of Cu and Fe can be comprised in the zeolite material as structural structural element or non-structural structural element. According to the present invention, it is preferred that the one or more of Cu and Fe is comprised in the zeolite material as a non-structural structural element.

[027] As mentioned above, it is preferred that the wash coating comprises a zeolite material comprising one or more of Cu and Fe. Furthermore, it is particularly preferred that the wash coat comprises a zeolite material comprising Cu, preferably as non-structural structure element.

[028] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises viii ) platinum supported on zirconia-alumina, and viii) a zeolite material having CHA-like structural structure and comprising Cu.

[029] Furthermore, it is preferred, according to the present invention, that the structural structure of the zeolite material comprises Si and Al and that the zeolite material further comprises Cu.

[030] When the zeolite material comprising Cu is comprised in the wash coating, it is further preferred that the zeolite material comprises Si, Al, O, H and Cu in any conceivable amount thereof. However, it is preferred that at least 99.0% by weight, preferably at least 99.5% by weight, most preferably at least 99.9% by weight of the zeolite material consist of Si, Al, O, H and Cu.

[031] When the wash coating comprises a zeolite material comprising Cu, any suitable amount of Cu may be comprised in the zeolite material. The zeolite material preferably comprises Cu, calculated as CuO, in an amount in the range from 0.1 to 5% by weight, more preferably from 1.0 to 4.5% by weight, most preferably , from 2 to 4% by weight, more preferably from 2.5 to 3.5% by weight, most preferably from 3 to 3.5% by weight, based on the total weight of the zeolite material.

[032] A zeolite material having the structural structure CHA and comprising Cu can be prepared according to conventional methods. In view of the direct synthesis of a zeolite material having the CHA structure comprising Cu and/or a method of preparation including incorporation of Cu into a zeolite material via ion exchange, reference is made to US 9,272,272 B2, US 8,715,618 B2, US 8,293,199 B2, US 8,883,119 B2, US 8,961,914 B2 and US 9,242,238 B2, in particular the Examples and preferred methods of preparation as disclosed in said documents, all of which are incorporated herein by reference.

[033] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises i ) platinum supported on zirconia-alumina, and ii) a zeolite material having a CHA-type structural structure and comprising Cu, wherein the zeolite material comprises Cu, calculated as CuO, in an amount in the range of 0.1 to 5% by weight more preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, most preferably from 2.5 to 3.5% by weight, so more preferably, from 3 to 3.5% by weight, based on the total weight of the zeolite material.

[034] Therefore, the present invention more preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises i) platinum supported on zirconia-alumina, and ii) a zeolite material having a CHA-type structural structure and comprising Cu, wherein the zeolite material comprises Cu, calculated as CuO, in an amount in the range of 0.1 to 5% by weight, more preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, most preferably from 2.5 to 3.5% by weight, more preferably from 3 to 3.5% by weight based on the total weight of the zeolite material, wherein at least 99.5% by weight, preferably wherein at least 99.9% by weight of the material Zeolite consist of Si, Al, O, H and Cu.

[035] When the wash coating comprises a zeolite material comprising Fe, it is preferred that the zeolite material comprises Fe as a non-structural structural element. Further preferably, the structural structure of the zeolite material comprises Si and Al and that the zeolite material comprises Fe. The zeolite material comprises Si, Al, O, H and Fe in any conceivable amount. It is preferred that at least 99.0% by weight, preferably at least 99.5% by weight, most preferably at least 99.9% by weight of the zeolite material consist of Si, Al, O, H and Fe. When the wash coating comprises a zeolite material comprising Fe, any suitable amount of Fe may be comprised in the one or more of the zeolite materials. Thus, the zeolite material can comprise Fe, calculated as Fe2O3, in an amount in the range of 0.1 to 5% by weight, preferably 1.0 to 4.5% by weight, more preferably 2 to 4% by weight, more preferably from 3 to 3.5% by weight, based on the total weight of the zeolite material.

[036] When the wash coating comprises a zeolite material comprising one or more of Cu and Fe, there is no particular restriction as to how one or more of Cu and Fe is included in the zeolite material, preferably as a structural element not structural, was introduced in it. Thus, one or more of Cu and Fe comprised in the zeolite material as an element of non-structural structure can be introduced therein using any suitable method, wherein the introduction is preferably effected by means of impregnation of the zeolite material with a salt of the metal and/or by ion exchange of the metal ion. It is particularly preferred that the one or more Cu and Fe comprised in the zeolite material, preferably as a non-structural structure element, have been introduced into the zeolite material by ion exchange.

[037] According to the present invention, the wash coating may comprise a binder material, for example, a metal oxide binder material. There is no specific restriction on the amount and chemical nature of the binder material. It is preferred that the wash coating further comprises iii) a metal oxide binder material.

[038] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises i ) platinum supported on zirconia-alumina, ii) a zeolite material having a CHA-type structural structure and comprising Cu, wherein the zeolite material comprises Cu, calculated as CuO, in an amount in the range of 0.1 to 5% by weight, more preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, more preferably from 2.5 to 3.5% by weight, more preferably preferably from 3 to 3.5% by weight based on the total weight of the zeolite material, wherein at least 99.5% by weight, preferably at least 99.9% by weight of the zeolite material consists of Si, Al, O, H and Cu, and iii) a metal oxide binder material.

[039] With regard to the metal oxide binder material, no restrictions apply as to the chemical nature of the metal oxide binder material, provided it comprises a metal atom bonded to an oxygen atom. However, it is preferred in accordance with the present invention that the metal oxide binder material is one or more of zirconia, alumina, silica, titania, silica-zirconia and zirconia-titania, preferably one or more of zirconia and titania-zirconia, most preferably zirconia.

[040] Therefore, the present invention preferably relates to a catalyst comprising a wash coat comprising one or more layers, the wash coat being disposed on a substrate, wherein the wash coat comprises i ) platinum supported on zirconia-alumina, ii) a zeolite material having a CHA-type structural structure and comprising Cu, wherein the zeolite material comprises Cu, calculated as CuO, in an amount in the range of 0.1 to 5% by weight, more preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, more preferably from 2.5 to 3.5% by weight, more preferably preferably from 3 to 3.5% by weight based on the total weight of the zeolite material, wherein at least 99.5% by weight, preferably at least 99.9% by weight of the zeolite material consists of Si, Al, O, H and Cu, and iii) zirconia as a metal oxide binder material.

[041] With regard to the substrate on which the wash coating comprising one or more layers is provided on the catalyst of the invention, no particular restrictions apply, such that any suitable substrate can be provided for this purpose, provided that a coating of washing can be placed on it. In particular, the type of substrate that can be contained in the catalyst of the invention is not restricted either in terms of its shape or in terms of the materials it consists of.

[042] Thus, the substrate contained in the catalyst of the invention may comprise any suitable substance or substances, wherein the substrate preferably comprises one or more of a ceramic and metal substance, and preferably comprises a ceramic substance. Among the preferred ceramic substances, it is particularly preferred that the substrate comprises one or more of alumina, silica, silicates, aluminosilicates, aluminotitanates, silicon carbide, cordierite, mullite, zirconia, spinel, magnesia and titania, more preferably one or more more of alpha-alumina, aluminotitanates, silicon carbide and cordierite, more preferably one or more of Al2TiO5, SiC and cordierite, more preferably the substrate comprising cordierite, more preferably more of the substrate consists of cordierite. Regardless, the shape of the substrate comprised in the catalyst of the invention may, by way of example, be one or more of a granule, a pellet, a mesh, a ring, a sphere, a cylinder, a hollow cylinder and a monolith, in that the substrate is preferably a monolith, more preferably a honeycomb monolith, wherein the honeycomb monolith is preferably a wall-flow or flow-through monolith, preferably a flow-through monolith .

[043] Furthermore, it is preferred, according to the present invention, that the substrate has a plurality of longitudinally extending passages, formed by longitudinally extending walls, delimiting and defining the passages and a total length longitudinal extending between a front end and a rear end of the substrate.

[044] As mentioned above, there is no particular restriction with regard to the number of layers that the wash coat comprises.

[045] According to a first embodiment of the present invention, the wash coating preferably comprises a layer. Provided that the substrate has a length of substrate, where the substrate is preferably as defined herein, the layer can be arranged on the substrate at any length. It is preferred that the layer be disposed in 50 to 100%, preferably in 75 to 100%, more preferably in 95 to 100%, more preferably in 100% of the total length of the substrate.

[046] When the wash coating consists of a layer, according to the particular and preferred embodiments of the catalyst of the invention, in which a platinum group metal is comprised in the layer, there is, in principle, no particular restriction as to platinum group metal loading, preferably the platinum group metal loading comprised in the one layer is in the range of 1 to 15 g/ft3 (0.035 to 0.529 kg/m3), more preferably, from 3 to 10 g/ft3 (0.106 to 0.353 kg/m3), more preferably from 4.5 to 8.5 g/ft3 (0.141 to 0.282 kg/m3), more preferably from 5.5 to 8.5 g/ft3 (0.176 to 0.282 kg/m3), more preferably from 7.5 to 8.5 g/ft3 (0.247 to 0.282 kg/m3).

[047] When the wash coating consists of a layer, according to the particular and preferred embodiments of the catalyst of the invention, there is, in principle, no restriction on loading a zeolite material in a layer, preferably the load of the zeolite material comprised in the one layer is in the range of 1.0 to 4.5 g/in3 (61.0 to 274.6 kg/m3), more preferably, from 1.5 to 4.0 g /in3 (91.5 to 244.1 kg/m3), more preferably from 2.0 to 3.75 g/in3 (122.0 to 228.8 kg/m3), more preferably from 2.75 to 3.5 g/in3 (167.8 to 213.5 kg/m3)

[048] According to the present invention, it is therefore particularly preferred that the catalyst of the invention is constituted by the wash coating disposed on the substrate and the wash coating is constituted by a layer.

[049] According to a second embodiment of the present invention, the wash coating preferably comprises two layers, a first layer and a second layer.

[050] When the wash coating consists of a first and a second layer, there is, in principle, no restriction whether one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe is contained in the first layer, or in the second layer, or in the first and second layers. It is preferred, according to the present invention, that the one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe, is contained in the first layer. Furthermore, it is preferred that the one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe be as defined herein. Thus, the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe is preferably as defined hereinabove.

[051] When the wash coating consists of a first layer and a second layer, it is preferred that the first layer comprises a zeolite material comprising one or more of Cu and Fe. There is, in principle, no restriction on loading of a zeolite material contained in the first layer, preferably the zeolite material is contained in the first layer at a loading in the range of 1.5 to 4.0 g/in3 (91.5 to 244.1 kg/m3), of more preferably, from 2.0 to 4.0 g/in3 (122.0 to 244.1 kg/m3), more preferably, from 2.0 to 3.5 g/in3 (122.0 to 213 kg/m3), more preferably from 3.0 to 3.5 g/in3 (183.0 to 213 kg/m3).

[052] When the wash coating consists of a first layer and a second layer, the first layer may further comprise a binder material, for example, a metal oxide binder material. Furthermore, it is preferred that the binder material be as defined herein. Therefore, it is preferred that the metal oxide binder material is as defined herein. According to the particular and preferred embodiments of the catalyst of the invention, in which the first layer comprises a metal oxide binder material, there is, in principle, no particular restriction on the loading of a metal oxide binder material, preferably, the loading of a metal oxide binder material contained in the first layer is in the range of 0.02 to 0.25 g/in3 (1.2 to 15.2 kg/m3), more preferably, of 0.07 to 0.25 g/in3 (4.2 to 15.2 kg/m3), more preferably from 0.1 to 0.25 g/in3 (6.1 to 15.2 kg/m3 ), more preferably from 0.2 to 0.25 g/in3 (12.2 to 15.2 kg/m3).

[053] When the wash coating consists of a first layer and a second layer, it is particularly preferred that the first layer is substantially free of Pt, preferably substantially free of one or more of Pd and Pt, more preferably , substantially free of one or more platinum group metals. Thus, it is preferred in accordance with the present invention that the first layer does not comprise platinum group metal supported on the metal oxide support material. More preferably, the first layer consists of the zeolite material comprising one or more of Cu and Fe, and preferably the metal oxide binder material.

[054] When the wash coating consists of a first layer and a second layer, there is, in principle, no restriction regarding the platinum group metal supported on the metal oxide support material, whether it is contained in the first layer, second layer or first and second layer. However, it is preferred in accordance with the present invention that the platinum group metal supported on a metal oxide support material is contained in the second layer. Furthermore, it is preferred that the platinum group metal supported on a metal oxide support material is as defined herein. Therefore, it is preferred that at least one of the platinum group metals and the support material are as defined herein, respectively. According to the present invention, there is, in principle, no restriction on the charging of the platinum group metal contained in the second layer. Preferably, the platinum group metal is contained in the second layer at a charge in the range of 2 to 30 g/ft3 (0.070 to 1.059 kg/m3), more preferably 6 to 20 g/ft3 (0.211 to 0.706 kg/m3), more preferably from 9.5 to 17 g/ft3 (0.317 to 0.600 kg/m3), more preferably from 11 to 17 g/ft3 (0.388 to 0.600 kg/m3).

[055] When the wash coating consists of a first layer and a second layer, it is particularly preferred that the second layer is substantially free of Cu, preferably substantially free of one or more Cu and Fe, more preferably substantially free of Cu, Fe, V and W. Thus, it is preferred according to the present invention that the second layer does not comprise an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe. Furthermore, it is preferred that the second layer be substantially free of a metal oxide binder material, wherein the metal oxide binder material is preferably as defined herein. Thus, more preferably, the second layer does not comprise the metal oxide binder material. More preferably, the second layer consists of the platinum group metal supported on a metal oxide support material.

[056] When the wash coating consists of a first layer and a second layer, the order in which the first layer and the second layer are arranged on the substrate and/or on top of each other does not in principle apply . Thus, the first layer or the second layer can be arranged directly on the substrate. As a first alternative, the first layer is placed on the substrate and the second layer is at least partially placed on the first layer. Furthermore, it is preferred that the first layer is disposed on the substrate and the second layer is completely disposed on the first layer. As a second alternative, the second layer is placed on the substrate and the first layer is at least partially placed on the second layer. Furthermore, it is preferred that the second layer is disposed on the substrate and that the first layer is completely disposed on the second layer.

[057] With regard to the first alternative mentioned above, when the first layer is arranged on the substrate and the second layer is at least partially placed on the first layer, when the coating consists of a first layer and a second layer and under the proviso that the substrate has a plurality of longitudinally extending passageways formed by longitudinally extending walls delimiting and defining the passageways and an overall longitudinal length extending between a front end and a rear end of the substrate, the first layer can be laid on the substrate at any length. Preferably, the first layer is disposed in 50 to 100%, more preferably in 75 to 100%, more preferably in 95 to 100%, more preferably in 100% of the total length of the substrate, so preferably from the front end of the substrate. Furthermore, the second layer can be arranged in any length. Thus, the second layer can be at least partially disposed either on the substrate or on the first layer. Preferably, the second layer is disposed in 25 to 75%, more preferably in 35 to 65%, more preferably in 45 to 55%, more preferably in 50% of the total length of the substrate, preferably from the rear end of the substrate.

[058] With regard to the aforementioned second alternative, when the second layer is arranged on the substrate and the first layer is at least partially placed on the second layer, when the coating consists of a first layer and a second layer and under the proviso that the substrate has a plurality of longitudinally extending passageways formed by longitudinally extending walls delimiting and defining the passageways and an overall longitudinal length extending between a front end and a rear end of the substrate, the second layer can be laid on the substrate at any length. Preferably, the second layer is disposed in 50 to 100%, more preferably in 75 to 100%, more preferably in 95 to 100%, more preferably in 100% of the total length of the substrate, so preferably from the front end of the substrate. Furthermore, the first layer can be arranged in any length. Thus, the first layer can be at least partially disposed on the substrate or on the second layer. Preferably, the first layer is disposed in 50 to 100%, more preferably in 75 to 100%, more preferably in 95 to 100%, more preferably in 100% of the total length of the substrate, so preferably from the rear edge of the substrate.

[059] According to a third embodiment of the present invention, the wash coating preferably comprises three layers, a first layer and a second layer and a third layer.

[060] Preferably, at least one of the first layer and the second layer are as defined above. In principle, the third layer may comprise one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe and/or a platinum group metal supported on a material of metal oxide support. Furthermore, it is preferred that the oxidic compound of V, the oxidic compound of W, the zeolite material comprising one or more Cu and Fe and the platinum group metal supported on a metal oxide support material is as defined herein , respectively, if contained in the third layer. Therefore, at least one of the oxidic compound of V, the oxidic compound of W, the zeolite material comprising one or more of Cu and Fe, the platinum group metal and the metal oxide support material is preferably , as defined here, respectively.

[061] When the wash coating consists of a first layer, a second layer and a third layer, it is preferred that the third layer comprises one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material that comprises one or more of Cu and Fe. Thus, it is preferred that the one or more of an oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe are as defined herein. Accordingly, the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe are as defined herein, respectively.

[062] When the wash coating consists of a first layer, a second layer and a third layer, it is further preferred that the third layer is substantially free of Pt, preferably substantially free of one or more of Pd and Pt, so most preferably, substantially free of one or more platinum group metals. Thus, it is preferred in accordance with the present invention that the third layer does not comprise a platinum group metal supported on a metal oxide support material. More preferably, the third layer consists of one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe, and preferably a binder material of oxide metal.

[063] When the wash coating consists of a first layer, a second layer and a third layer, it is preferred that the third layer comprises a zeolite material comprising one or more of Cu and Fe, where the zeolite material is, preferably as defined herein. According to the present invention, there is, in principle, no restriction on the loading of the zeolite material contained in the third layer. Preferably, the zeolite material is contained in the third layer at a charge in the range of 0.2 to 0.8 g/in3 (12.2 to 48.8 kg/m3), more preferably, from 0.3 to 0.7 g/in3 (18.3 to 42.7 kg/m3), more preferably from 0.4 to 0.6 g/in3 (24.4 to 36.6 kg/m3).

[064] When the wash coating consists of a first layer, a second layer and a third layer, the third layer may further comprise a binder material, for example, a metal oxide binder material. Furthermore, it is preferred that the binder material be as defined herein. Therefore, it is preferred that the metal oxide binder material is as defined herein. According to particular and preferred embodiments of the catalyst of the invention, in which the third layer comprises a metal oxide binder material, there is, in principle, no particular restriction on the charge of the metal oxide binder material on the third layer. layer. Preferably, the loading of the metal oxide binder material comprised in the third layer is in the range from 0.02 to 0.14 g/in3 (1.2 to 8.5 kg/m3), more preferably from 0 .05 to 0.11 g/in3 (3.0 to 6.7 kg/m3). more preferably, from 0.07 to 0.09 g/in3 (4.2 to 5.5 kg/m3).

[065] When the consistency of a first layer, a second layer and a third layer, no restriction applies in principle as to the order in which the first layer, the second layer and the third layer are arranged on the substrate and/or one on the other. Thus, the first layer, the second layer or the third layer can be arranged on the substrate. Furthermore, it is particularly preferred that the first layer is disposed on the substrate and that the second layer is at least partially, preferably completely, placed on the substrate. Thus, it is preferred according to the present invention that the first layer is disposed on the substrate, that the second layer is at least partially disposed on the substrate and that the third layer is at least partially, preferably completely, disposed on the substrate. second layer.

[066] When the wash coating consists of a first layer, a second layer and a third layer and under the condition that the substrate, wherein the substrate is preferably as defined herein, has a plurality of passages that intersect extending longitudinally, formed by longitudinally extending walls delimiting and defining the passageways, and an overall longitudinal length extending between a front end and a rear end of the substrate, it is preferred that the third layer be disposed at 25 at 75%, more preferably at 35 to 65%, most preferably at 45 to 55% of the total length of the substrate, preferably from the rear end of the substrate.

[067] When the wash coating consists of a first layer, a second layer and a third layer and under the condition that the substrate, wherein the substrate is preferably as defined herein, has a plurality of passages that intersect extending longitudinally, formed by longitudinally extending walls delimiting and defining the passageways, and an overall longitudinal length extending between a front end and a rear end of the substrate, it is preferred that the first layer be arranged at 25 at 75%, more preferably at 35 to 65%, more preferably at 45 to 55%, most preferably at 50% of the total length of the substrate from the front end of the substrate and the second layer is placed within 25 to 75%, more preferably within 35 to 65%, most preferably within 45 to 55%, most preferably within 50% of the total length of the substrate from the rear end of the substrate , wherein the first and second layers in total are preferably arranged over 100% of the total length of the substrate. Furthermore, the third layer can be placed on the first layer and/or on the second layer. It is preferable that the third layer is arranged on the second layer. Thus, no restrictions apply to the length of the third layer. Thus, by way of example, the third layer may be arranged at 25 to 75%, preferably at 35 to 65%, more preferably at 45 to 55%, more preferably at 50% of the total length. substrate, preferably from the rear end of the substrate. It is preferred according to the present invention that the third layer is the same length as the second layer.

[068] According to a particular embodiment of the present invention, it is preferable that the wash coating consists of the first, second and third layers, wherein at least one of the first, second and third layers is preferably as defined here above. It is most preferred that the first, second and third layers are as defined herein.

[069] Furthermore, it is preferred that the catalyst of the present invention is comprised, as a second catalyst, in a sequence of two or more catalysts, preferably of two catalysts, in which a first catalyst is comprised in said sequence, whose first catalyst is preferably located upstream of said second catalyst in an exhaust gas treatment system, preferably in an exhaust gas treatment system as described hereinbelow. In principle, there is no restriction on the chemical structure of the substrate of said first catalyst. It is preferred that the substrate be as defined herein above, more preferably as being of the same chemical structure as the substrate of the catalyst as defined herein, more preferably as being identical with the substrate of the catalyst as defined above. Thus, it is preferred that the substrate of said second catalyst comprises a wash coat layer comprising one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe. It is particularly preferred that the one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe is preferably as defined herein. Therefore, at least one of the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe is preferably as defined herein.

[070] Preferably, the total charge of the catalyst in relation to the sum of V, W and Ti, also said as the total charge of VWT and being calculated as the total charge of V2O5, WO3 and TiO2, can be in the range of 1 to 5 g/in3 (61.0 to 305 kg/m3).

[071] Furthermore, it is preferred according to the present invention that the catalyst of the invention according to any one of the particular and preferred embodiments defined in the present invention is used in a process for an exhaust gas treatment as a catalyst tetra-functional for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon.

[072] Furthermore, the present invention relates to the use of the catalyst of the invention for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, preferably in a treatment of an exhaust gas.

[073] Furthermore, the present invention relates to the use of the catalyst of the invention for the treatment of an exhaust gas, preferably for the treatment of an industrial or automotive exhaust gas, more preferably for the treatment of an automobile exhaust gas. Thus, it is preferred that the automotive exhaust gas is an exhaust gas from an internal combustion engine, more preferably a diesel engine, most preferably a heavy-duty diesel engine.

[074] Furthermore, the present invention relates to a method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, preferably in a treatment of a exhaust gas, using a catalyst according to any of the particular and preferred embodiments defined in the present application.

[075] Furthermore, the present invention relates to a method for treating an exhaust gas, preferably for treating an industrial or automotive exhaust gas, more preferably for treating an exhaust gas. automobile exhaust, using a catalyst according to any one of the preferred and particular embodiments defined in the present application. Thus, it is preferred that the automobile exhaust gas be an exhaust gas from an internal combustion engine, preferably a diesel engine, most preferably a heavy-duty diesel engine.

[076] According to a particular preferred embodiment of the present invention, the catalyst according to any of the particular and preferred embodiments defined herein is comprised in an exhaust gas treatment system that, preferably, in communication fluid with an internal combustion engine, preferably a diesel engine, preferably a heavy-duty diesel engine.

[077] Furthermore, the present invention relates to an exhaust gas treatment system, preferably in fluid communication with an internal combustion engine, said exhaust gas system comprising the catalyst described above and in any one of the particular and preferred embodiments defined in the present application, wherein an internal combustion engine, preferably a diesel engine, more preferably a heavy-duty diesel engine. With regard to the exhaust gas treatment system of the present invention, no particular restrictions apply as to any additional components that may be comprised therein.

[078] Preferably, the exhaust gas treatment system has one or more components in addition to the catalyst described above. More preferably, the exhaust gas treatment system comprises one or more catalysts for the selective catalytic reduction of NOx and a catalyzed soot filter. Optionally, the exhaust gas treatment system comprises a catalyst for ammonia oxidation. Preferably, the exhaust gas treatment system comprises one or more reductant injectors, more preferably two or more reductant injectors, most preferably two reductant injectors. Preferably at least one reducing injector, preferably all reducing injectors are urea injectors.

[079] Therefore, the present invention also relates to the above exhaust gas treatment system, comprising - a first reducing injector, - a first catalyst for the selective catalytic reduction of NOx, preferably the first catalyst as defined herein above and, in particular, in embodiment 55 or 56 below, - a second catalyst, said second catalyst being the catalyst as described above and in embodiments 1 to 56 below; - a catalyzed soot filter, - a second reducing injector, - a third catalyst for the selective catalytic reduction of NOx, and - a fourth catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia.

[080] Regarding the positions of said components in the exhaust gas treatment system, there are no specific restrictions, provided that the exhaust gas stream can be treated with them according to specific needs. Preferably, the first catalyst is located upstream of the second catalyst, the second catalyst is located upstream of the third catalyst, and the third catalyst is located upstream of the fourth catalyst. Furthermore, it is preferred that a first reductant injector is located upstream of the first catalyst. Furthermore, it is preferred that a second reductant injector be located upstream of the third catalyst, where it is more preferred that it be located downstream of the catalyzed soot filter and upstream of the third catalyst.

[081] Preferably, in the exhaust gas treatment system of the present invention, no diesel oxidation catalyst is located downstream of the second catalyst and upstream of the catalyzed soot filter. More preferably, in the exhaust gas treatment system of the present invention, no diesel oxidation catalyst is located upstream of the catalyzed soot filter. More preferably, the exhaust gas treatment system of the present invention does not contain diesel oxidation catalyst.

[082] According to the present invention, it is preferred that the exhaust gas treatment system does not contain more catalyst than the catalysts described above. Therefore, with regard to the catalytic components and the reductant injectors, it is preferred that the exhaust gas treatment system of the present invention consists of - a first reductant injector, - a first catalyst for the selective catalytic reduction of NOx, of preferably the first catalyst as defined herein above and in particular in embodiment 55 or 56 below, - a second catalyst, said second catalyst being the catalyst as described above and in embodiments 1 to 56 below; - a catalyzed soot filter, - a second reducing injector, - a third catalyst for the selective catalytic reduction of NOx, and - a fourth catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia.

[083] Thus, with regard to the catalytic components and the reductant injectors, it is more preferred that the exhaust gas system of the present invention consists of - a first reductant injector, which is located upstream - a first catalyst for the reduction NOx selective catalyst, preferably the first catalyst as defined hereinabove, and in particular in embodiment 55 or 56 below, which is located upstream of - a second catalyst, wherein said second catalyst is the NOx catalyst any one of embodiments 1 to 56, which is located upstream of - a catalyzed soot filter, which is located upstream - a second reductant injector, which is located upstream - a third catalyst for the selective catalytic reduction of NOx , which is located upstream - a fourth catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia.

[084] In general, it is also conceivable, according to the present invention, that the exhaust gas treatment system comprises - a reducing injector, preferably a urea injector, located upstream - a catalyst for catalytic reduction NOx selective reduction and/or ammonia oxidation, preferably NOx selective catalytic reduction and ammonia oxidation, which is located upstream of - a catalyzed soot filter, which is located upstream - reductant injector , preferably a urea injector, located upstream - a catalyst for the selective catalytic reduction of NOx, which is located upstream - a catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia, preferably, the selective catalytic reduction of NOx and for the oxidation of ammonia; - wherein, preferably, and with regard to the catalytic components and the reducing injectors, the gas treatment system of - reducing injector, preferably a urea injector, located upstream - a catalyst for selective catalytic reduction of NOx and/or for the oxidation of ammonia, preferably for the selective catalytic reduction of NOx and for the oxidation of ammonia, which is located upstream of - a catalyzed soot filter, which is located upstream - reductant injector, preferably a urea injector, located upstream - a catalyst for the selective catalytic reduction of NOx, which is located upstream - a catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia, preferably at selective catalytic reduction of NOx and for the oxidation of ammonia; - in which, in particular, no diesel oxidation catalyst is located upstream of the catalysed soot filter, and in which, in particular, no diesel oxidation catalyst is comprised in the exhaust gas treatment system.

[085] Furthermore, the present invention relates to a method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, comprising

[086] (1) providing a gas stream comprising one or more of NOX, ammonia, nitrogen monoxide and a hydrocarbon;

[087] (2) contacting the gas stream supplied in (1) with the catalyst of any of the particular and preferred embodiments defined in the present application.

[088] Thus, it is preferred that the gas flow is an exhaust gas flow from an internal combustion engine, preferably a diesel engine, most preferably a heavy-duty diesel engine. According to the method of the invention, it is preferred that the gaseous stream treated by contact with the catalyst of the invention comprises one or more reducing agents for selective catalytic reduction of NOx. For this purpose, any suitable reducing agent or combination of reducing agents can be used. employ, provided they can reduce NOx to nitrogen gas. According to the method of the invention, it is, however, preferred that urea and/or ammonia is comprised among the reducing agents used, wherein, more preferably, urea and/or ammonia is employed as reducing agent in the method of the invention. invention, preferably ammonia. It is therefore preferred, according to the method of the invention, that the gas flow further comprises one or more reducing agents, the reducing agent or agents preferably comprising urea and/or ammonia, preferably ammonia.

[089] As described above, it is preferred that the catalyst of the present invention described above is comprised in an exhaust gas treatment system, preferably in an exhaust gas treatment system described above. Therefore, the present invention also relates to a method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, comprising (1) providing a gas stream comprising a or more of NOX, ammonia, nitrogen monoxide and a hydrocarbon; (2) introduce the gas stream into an exhaust gas treatment system described above and pass the gas stream through the system.

[090] With regard to the gas stream comprising one or more of NOX, ammonia, nitrogen monoxide and a hydrocarbon, there is no particular restriction according to the present invention as to how said gas stream is supplied, so such that it can be derived from any conceivable source. However, it is preferred in accordance with the present invention that the gas flow comprises an exhaust gas stream containing NOx from an internal combustion engine, preferably a diesel engine.

[091] Furthermore, the present invention relates to a process for preparing the catalyst of any of the particular and preferred embodiments defined in the present application, the process comprising disposing of one or more pastes on a substrate, one or more further pastes comprising the platinum group metal supported on a metal oxide support material and one or more of the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe, wherein , after a paste has been placed on the substrate, a treated paste. A dry and calcined substrate is obtained.

[092] Furthermore, it is preferred that the one or more folders comprise one or more of a first folder, a second folder and a third folder. Thus, it is preferred that one or more folders comprise a first folder.

[093] Therefore, the present invention relates to a process for preparing the catalyst of any of the particular and preferred embodiments defined in the present application, the process comprising (a) placing a first paste on a substrate, obtaining a paste-treated substrate; (b) drying the paste-treated substrate obtained from (a), (c) calcining the dry paste-treated substrate obtained from (b), obtaining the substrate having a first layer disposed thereon.

[094] According to a preferred embodiment of the process, the first paste comprises the platinum group metal supported on a metal oxide support material and/or the one or more of one oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe. However, it is particularly preferred that the first slurry comprises the platinum group metal supported on a metal oxide support material and one or more of a compound oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe.

[095] Furthermore, it is preferred that the first paste further comprises a disposition aid. Thus, there is no restriction with regard to the chemical structure of the disposal aid, as long as the disposal aid is suitable for aiding the elimination of the first paste on the substrate. It is particularly preferred according to the present invention that the first paste comprises one or more of tartaric acid and monoethanolamine, more preferably tartaric acid and monoethanolamine.

[096] According to the process of the invention in which the first paste is placed on the substrate, there is no restriction with regard to the length at which the first paste is placed on the substrate. Thus, it is preferred that the substrate be as defined herein, more preferably having a length of substrate. Thus, the first paste can be placed on the substrate, where the substrate has a length of substrate, in any length relative to the length of the substrate. Thus, by way of example, the first paste can be placed at 50 to 100%, preferably at 75 to 100%, more preferably at 95 to 100%, more preferably at 100% of the total length of the substrate.

[097] With regard to drying in (b), no restrictions apply such that drying can be carried out in any suitable manner, provided that the paste-treated substrate obtained in (a) is dried to some extent. It is preferred that drying be carried out to remove between 85% and 95% moisture. Thus, it is preferred, according to the present invention, that a gas atmosphere is used for the heat exchange for this purpose. As far as the gas atmosphere for drying in (b) is concerned, no particular restrictions apply, such that any gas may be used, provided the gas is adequate to provide a gas atmosphere at a useful temperature for the drying process. heat exchange. Thus, by way of example, the gas atmosphere may comprise one or more of nitrogen, oxygen, an inert gas and carbon dioxide, preferably nitrogen. Alternatively, the gas atmosphere may comprise air.

[098] With regard to the temperature of the gas atmosphere for drying in (b), no particular restriction is applicable such that any suitable temperature can be chosen provided that the paste-treated substrate obtained in (a) can be dried to a certain extent, resulting substrate treated with dry paste. Thus, by way of example, the drying in (b) can be carried out using a gaseous atmosphere with a temperature in the range of 90 to 170°C, preferably 100 to 140°C, and more preferably of 110 to 130 °C.

[099] With regard to calcination in c), no restrictions apply such that calcination can be carried out in any suitable way, provided that the substrate treated with dry paste is calcined to a certain extent and provided that calcination results in a substrate having a first layer disposed thereon. However, it is preferred according to the present invention that a gas atmosphere is used for the heat exchange for this purpose. As regards the gas atmosphere for calcination in c), the same applies as for the gas atmosphere for drying, so that in principle any gas can be used, provided it is suitable to provide an atmosphere of gas at a useful temperature for calcination. Thus, by way of example, the gas atmosphere may comprise one or more of nitrogen, oxygen, an inert gas and carbon dioxide, preferably nitrogen.

[100] With regard to the temperature of the gas atmosphere for calcination in (c), any suitable temperature can be chosen in principle, provided that the dry paste-treated substrate obtained in one or more of (b) can be effectively calcined. Thus, by way of example, the calcination in (c) can be carried out using a gaseous atmosphere with a temperature in the range of 350 to 550 °C, preferably 400 to 500 °C, more preferably 440 to 460 °C.

[101] As mentioned above, in view of the process for preparing the catalyst of any of the particular and preferred embodiments defined in the present application, it is preferred that one or more slurries comprise one or more of a first slurry, a second slurry and a third folder. Thus, it is preferred that the one or more folders comprise a first folder and a second folder.

[102] Therefore, the process for preparing the catalyst of any of the particular and preferred embodiments defined in the present patent application further comprises (d) disposing a second paste on the substrate having a first layer disposed thereon, obtaining a paste-treated substrate, (e) drying the paste-treated substrate obtained in (d), (f) calcining the dry paste-treated substrate obtained from (e), obtaining the substrate having a first and a second layer arranged on it.

[103] With respect to the first slurry in the process comprising (a) to (f), preferably, according to any one of the particular and preferred embodiments as defined herein, the first slurry may comprise the one or more of an oxidic compound of V, an oxidic compound of W, a zeolite material comprising one or more of Cu and Fe and the platinum group metal supported on a metal oxide support material. With respect to the second slurry in the process comprising (a) to (f), the second slurry may comprise the one or more of an oxidic compound of V, an oxidic compound of W, a zeolite material comprising one or more Cu and Fe and the platinum group metal supported on a metal oxide support material.

[104] As a first alternative, the first slurry comprises the one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe, and the second slurry comprises the group metal of platinum supported on a metal oxide support material.

[105] As a second alternative, the first slurry comprises the platinum group metal supported on a metal oxide support material and the second slurry comprises the one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe.

[106] With regard to the drying in (e), the same applies to the drying in (b) as defined herein. As regards the calcination in (f), the same applies to the calcination in (c) as defined herein.

[107] As mentioned above, in view of the process for preparing the catalyst of any of the particular and preferred embodiments defined in the present application, it is preferred that one or more slurries comprise one or more of a first slurry, a second slurry and a third folder. Thus, it is preferred that the one or more folders comprise a first folder, a second folder and a third folder.

[108] Accordingly, the process for preparing the catalyst of any of the particular and preferred embodiments defined in the present patent application further comprises (g) placing a third slurry on the substrate having a first and a second layer thereover , obtaining a paste-treated substrate, (h) Dry the paste-treated substrate obtained from (g), [1] calcine the dry paste-treated substrate obtained from (h), obtaining the substrate having a third layer disposed therein.

[109] With regard to the third slurry in the process comprising (a) to (k), preferably, according to any one of the particular and preferred embodiments as defined herein, the third slurry may comprise one or more compounds oxidic compound of V, an oxidic compound of W, a zeolite material comprising one or more of Cu and Fe and a platinum group metal supported on a metal oxide support material as defined herein. However, it is preferred that the third slurry comprises one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe as defined herein.

[110] When one or more folders comprise a first, a second and a third folder, there is no restriction in what order the first folder, the second folder and the third folder are arranged on the substrate. Thus, by way of example, the first or second paste can be directly disposed on the substrate, where it is preferred that the first paste be directly disposed on the substrate, resulting in a first layer. With regard to the second paste, it is thus particularly preferred that the second paste is disposed at least partially, preferably completely, on the substrate, also resulting in a second layer. As regards the third folder, it is conceivable that the third folder is arranged at least partially on the first layer or on the second layer, preferably at least partially on the second layer.

[111] When one or more slurries comprise a first, a second and a third slurry and provided that the substrate, preferably as defined herein, thus having a plurality of longitudinally extending passages formed by walls which extend longitudinally, and by defining the passages and an overall longitudinal length that extend between a front end and a rear end of the substrate, it is preferred that the arrangement of the first slurry is carried out in any length of the total length of the substrate from the front end of the substrate, disposing the second slurry any length of the total length of the substrate from the rear end of the substrate, and disposing the third slurry any length of the total length of the substrate, preferably from the rear end of the substrate.

[112] When one or more pastes comprise a first, a second and a third paste, according to any one of the particular and preferred embodiments of the process and under the condition that the substrate, preferably, as defined herein, having thus a plurality of longitudinally extending passageways formed by longitudinally extending walls delimiting and defining the passageways and an overall longitudinal length extending between a front end and a rear end of the substrate, arranging the first slurry in 25 to 75%, preferably 35 to 65%, more preferably, on 45 to 55% of the total length of the substrate from the front end of the substrate, with the second paste arranging 25 to 75%, preferably, on 35 to 65%, more preferably, in 45 to 55% of the total length of the substrate from the rear end of the substrate, and the arrangement of the third paste is carried out in 25 to 75%, preferably in 35 to 65%, more preferably, within 45 to 55% of the total length of the substrate, preferably from the rear end of the substrate.

[113] When one or more folders comprise a first, a second and a third folder and according to any one of the particular and preferred embodiments of the process comprising (a) to (k), it is particularly preferred that the third folder is arranged into the second layer, preferably along the same length as the second layer.

[114] With respect to the first pulp, the second pulp and the third pulp in the process according to any one of the particular and preferred embodiments of the process as defined herein, it is preferred that the first pulp, the second pulp and the third paste further comprises liquid component. Thus, there is no restriction with regard to the liquid component, as long as it allows the homogenization of one or more of the first paste, the second paste and the third paste. It is preferred that the first slurry, second slurry and third slurry further comprise, as a liquid component, one or more of water, methanol, ethanol, isopropanol, n-propanol, formic acid, acetic acid and propionic acid, preferably one or more of water and acetic acid, more preferably water.

[115] Furthermore, with regard to the first pulp, the second pulp and the third pulp in the process according to any one of the particular and preferred embodiments as defined herein, it is preferred that the first pulp, the second pulp and the third paste further comprises one or more of zirconyl acetate, a silicate, silica, an aluminate, alumina, a titanate and titania, preferably zirconyl acetate.

[116] With regard to the drying in (h), the same applies to the drying in (b) as defined here.

[117] With regard to calcination in (k), the same applies to calcination in (c) as defined here.

[118] As regards the method for arranging one or more of the first folder, the second folder and the third folder, no restriction applies such that any suitable method can be applied to this effect, provided that a paste-treated substrate. However, it is preferred, in accordance with the present invention, that the elimination of one or more of the first slurry, the second slurry and the third slurry is effected by wet impregnation or spraying, preferably by wet impregnation.

[119] With regard to the charge value of the zeolite material comprising one or more Cu and Fe, charging the platinum group metal supported on a metal support and charging the metal oxide binder material on the substrate expressed in grams per cubic inch, it is noted that, in the sense of the present invention, the weight in grams refers to the weight of the zeolite material containing a metal and the volume expressed in cubic inches refers to the volume of the substrate and, preferably , of the uncoated substrate, said volume including any pores, cavities and channels that may be present in the substrate form. In particular, in particularly preferred cases where a honeycomb monolith substrate is used, the volume refers to the total volume of the honeycomb substrate including the channels contained therein.

[120] The expression "substantially free of" as disclosed herein characterizes an object by the fact that it contains less than 0.1% by weight, preferably less than 0.01% by weight, more preferably less than 0.001 % by weight of a substance, element or group of elements from the periodic table of elements.

[121] The units of inches (abbreviated as in) and feet (abbreviated as ft), as disclosed herein, refer to units of length in the US and Imperial customary measurement systems. There are 12 inches in a foot. One inch equals 2.54 cm.

[122] The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from dependencies and backreferences as indicated. In particular, note that in each case where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", each embodiment in this range is intended to be explicitly disclosed to the person skilled in the art, i.e. the term of this term is to be understood by the person skilled in the art to be synonymous with "The process of any one of Embodiments 1, 2, 3 and 4".

[123] 1. A catalyst, preferably, for the selective catalytic reduction of NOx, for the oxidation of ammonia, for the oxidation of NO and for the oxidation of a hydrocarbon, comprising a wash coating comprising one or more layers, the wash coat being disposed on a substrate, the wash coat comprising i) a platinum group metal supported on a metal oxide support material, and ii) one or more of an oxidic compound of V, a oxide compound of W, and a zeolite material comprising one or more of Cu and Fe, wherein the wash coating comprises iii) a platinum group metal supported on a metal oxide support material, and iv) a material zeolite comprising one or more of Cu and Fe.

[124] 2. The catalyst of Embodiment 1, wherein the platinum group metal is one or more of Pt, Pd and Rh, preferably one or more of Pt and Pd, most preferably Pt.

[125] 3. The catalyst of embodiment 1 or 2, wherein the metal oxide support material is one or more of alumina, zirconia-alumina, silica-alumina, titania, zirconia-titania and ceria, preferably one or more of alumina, silica-alumina and zirconia-alumina, more preferably zirconia-alumina.

[126] 4. The catalyst of any one of embodiments 1 to 3, wherein the structural structure of the zeolite material comprises a tetravalent element Y which is one or more of Si, Sn, Ti, Zr and Ge, preferably Si .

[127] 5. The catalyst of any one of embodiments 1 to 4, wherein the backbone of the zeolite material comprises a trivalent element X which is one or more of B, Al, Ga and In, preferably Al.

[128] 6. The catalyst of any one of embodiments 1 to 5, wherein the zeolite material has a structural structure of the type ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR , AFS, AFT, AFV, AFX,AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AVL, AWO,AWW, BCT, BEA, BEC, BIK, BOF, BOG , BOZ, BPH, BRE, BSV, CAN, CAS, CDO, CFI, CGF, CGS, CHA, -CHI, -CLO, CON, CSV, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI , EEI, EMT, EON, EPI, ERI, ESV, ETR, EUO, *-EWT, EZT, FAR, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFO, IFR, -IFU, IFW, IFY, IHW, IMF, IRN, IRR, -IRY, ISV, ITE, ITG, ITH, *-ITN, ITR, ITT, -ITV, ITW, IWR, IWS, IWV, IWW, JBW, JNT, JOZ, JRY, JSN, JSR, JST, JSW, KFI, LAU, LEV, LIO, -LIT, LOS, LOV, LTA, LTF, LTJ, LTL, LTN, MAR, MAZ, MEI, MEL, MEP, MER, MFI, MFS , MON, MOR, MOZ, *MRE, MSE, MSO, MTF, MTN, MTT, MTW, MVY, MWF, MWW, NAB, NAT, NES, NON, NPO, NPT, NSI, OBW, OFF, OKO, OSI, OSO, OWE, -PAR, PAU, PCR, PHI, PON, POS, PSI, PUN, RHO, - RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAF, SAO, SAS, SAT, SAV, SBE, SBN, SBS, SBT, SEW, SFE, SFF, SFG, SFH, SFN, SFO, SFS, *SFV, SFW, SGT, SIV, SOD, SOF, SOS, SSF, *-SSO, SSY, STF, STI , *STO, STT, STW, - SVR, SVV, SZR, TER, THO, TOL, TON, TSC, TUN, UEI, UFI, UOS, UOV, UOZ, USI, UTL, UWY, VET, VFI, VNI, VSV , WEI, -WEN, YUG, ZON, mixtures of two or more of these, and mixed types of two or more of these, preferably of the type AEI, GME, BEA, CHA, FAU, FER, HEU, LEV, MEI, MEL , MFI or MOR, more preferably of the type AEI, GME, CHA, MFI, BEA, FAU or MOR, more preferably of the type CHA, AEI or BEA, more preferably of the type CHA and/ or AEI, and more preferably of the CHA type.

[129] 7. The catalyst of any one of embodiments 1 to 6, wherein the structural structure of the zeolite material comprises Si, Al, O and H and wherein at least 99.0% by weight, preferably, at at least 99.5% by weight, more preferably at least 99.9% % by weight of the structural structure of the zeolite material consists of Si, Al, O and H.

[130] 8. The catalyst of any one of embodiments 1 to 7, wherein the oxidic compound of V is one or more of an ammonium vanadate, a sodium vanadate, an iron vanadate, vanadium pentoxide and vanadium pentoxide vanadium stabilized with iron oxide.

[131] 9. The catalyst of any one of embodiments 1 to 8, wherein the oxidic compound of W is one or more of an ammonium tungstate, a sodium tungstate and tungsten trioxide.

[132] 10. The catalyst of any one of embodiments 1 to 9, wherein one or more of the oxidic compound of V and the oxidic compound of W is supported on one or more titania and zirconia-titania, preferably on titania.

[133] 11. The catalyst of any one of embodiments 1 to 10, wherein the zeolite material comprises Cu.

[134] 12. The catalyst of any one of embodiments 1 to 11, wherein the structural structure of the zeolite material comprises Si and Al and the zeolite material comprises Cu.

[135] 13. The catalyst of any one of embodiments 1 to 12, wherein the zeolite material comprises Si, Al, O, H and Cu and wherein at least 99.0% by weight, preferably at least 99.5% by weight, more preferably at least 99.9% by weight The structural structure of the zeolite material consists of Si, Al, O, H and Cu.

[136] 14. The catalyst of any one of embodiments 1 to 13, wherein the zeolite material comprises Cu, calculated as CuO, respectively, in an amount in the range of 0.1 to 5% by weight, preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, more preferably from 2.5 to 3.5% by weight, more preferably from 3 to 3.5% by weight, based on the total weight of the zeolite material.

[137] 15. The catalyst of any one of embodiments 1 to 14, wherein the zeolite material comprises Fe.

[138] 16. The catalyst of any one of embodiments 1 to 15, wherein the structural structure of the zeolite material comprises Si and Al and the zeolite material comprises Fe.

[139] 17. The catalyst of any one of embodiments 1 to 16, wherein the zeolite material comprises Si, Al, O, H and Fe and wherein at least 99.0% by weight, preferably at least 99.5% by weight, more preferably at least 99.9% by weight of the zeolite material consists of Si, Al, O, H and Fe.

[140] 18. The catalyst of any one of embodiments 1 to 17, wherein the zeolite material comprises Fe, calculated as Fe2O3, respectively, in an amount in the range of 0.1 to 5% by weight, preferably from 1.0 to 4.5% by weight, more preferably from 2 to 4% by weight, most preferably from 3 to 3.5% by weight, based on the total weight of the zeolite material.

[141] 19. The catalyst of any one of Embodiments 1 to 18, wherein the wash coating further comprises 111) a metal oxide binder material.

[142] 20. The catalyst of embodiment 19, wherein the metal oxide binder material is one or more of zirconia, alumina, silica, titania, silica-zirconia and zirconia-titania, preferably one or more of zirconia and titania-zirconia, most preferably zirconia.

[143] 21. The catalyst of any one of embodiments 1 to 20, wherein the substrate comprises a ceramic and/or a metal substance, preferably a ceramic substance, more preferably a ceramic substance than a or more of alumina, silica, silicates, aluminosilicates, aluminotitanates, silicon carbide, cordierite, mullite, zirconia, spinel, magnesia and titania, more preferably one or more of alpha-alumina, aluminotitanates, silicon carbide and cordierite, more preferably one or more of Al2TiO5, SiC and cordierite, more preferably the substrate comprising cordierite, more preferably the substrate being cordierite.

[144] 22. The catalyst of any one of embodiments 1 to 21, wherein the substrate is one or more of a granule, a pellet, a mesh, a ring, a sphere, a cylinder, a hollow cylinder and a monolith, wherein the substrate is preferably a monolith, more preferably a honeycomb monolith, wherein the honeycomb monolith is preferably a flow wall or continuous flow monolith, preferably a continuous flow monolith.

[145] 23. The catalyst of any one of embodiments 1 to 22, wherein the substrate has a plurality of longitudinally extending passageways formed by longitudinally extending walls delimiting and defining the passageways and an overall longitudinal length extending between a front end and a rear end of the substrate.

[146] 24. The catalyst of any one of embodiments 1 to 23, wherein the wash coat consists of a layer.

[147] 25. The catalyst of embodiment 24, wherein the substrate has a length of substrate and wherein the layer is disposed at 50 to 100%, preferably at 75 to 100%, more preferably at 95 to 100%, more preferably, over 100% of the total substrate length.

[148] 26. The catalyst of embodiment 24 or 25, wherein the layer comprises platinum group metal at a charge in the range of 1 to 15 g/ft3 (0.035 to 0.529 kg/m3), preferably from 3 to 10 g/ft3 (0.106 to 0.353 kg/m3), more preferably from 4.5 to 8.5 g/ft3 (0.141 to 0.282 kg/m3), more preferably from 5.5 to 8.5 g/ft3 (0.176 to 0.282 kg/m3), more preferably from 7.5 to 8.5 g/ft3 (0.247 to 0.282 kg/m3).

[149] 27. The catalyst of any one of embodiments 24 to 26, wherein the layer comprises the zeolite material at a charge in the range of 1.0 to 4.5 g/in3 (61.0 to 274.6 kg/m3), preferably from 1.5 to 4.0 g/in3 (91.5 to 244.1 kg/m3), more preferably from 2.0 to 3.75 g/in3 (122 0 to 228.8 kg/m3), more preferably from 2.75 to 3.5 g/in3 (167.8 to 213.5 kg/m3).

[150] 28. The catalyst of any one of embodiments 24 to 27, wherein the catalyst is the wash coating disposed on the substrate.

[151] 29. The catalyst of any one of embodiments 1 to 23, wherein the wash coat comprises a first and a second layer.

[152] 30. The catalyst of embodiment 29, wherein the first layer comprises one or more of the oxidic compound of V, the oxidic compound of W, and the zeolite material comprising one or more of Cu and Fe.

[153] 31. The catalyst of embodiment 30, wherein the first layer comprises the zeolite material at a load in the range of 1.5 to 4.0 g/in3 (91.5 to 244.1 kg/m3) , preferably from 2.0 to 4.0 g/in3 (122.0 to 244.1 kg/m3), more preferably from 2.0 to 3.5 g/in3 (122.0 to 213 .5 kg/m3), more preferably from 3.0 to 3.5 g/in3 (183 to 213.5 kg/m3).

[154] 32. The catalyst of embodiment 30 or 31, wherein the first layer further comprises the metal oxide binder material as defined in embodiment 19 or 20.

[155] 33. The catalyst of embodiment 32, wherein the first layer comprises the metal oxide binder material at a charge in the range of 0.02 to 0.25 g/in3 (1.2 to 15.2 kg/m3), preferably from 0.07 to 0.25 g/in3 (4.2 to 15.2 kg/m3), more preferably from 0.1 to 0.25 g/in3 (6 .1 to 15.2 kg/m3), more preferably from 0.2 to 0.25 g/in3 (12.2 to 15.2 kg/m3).

[156] 34. The catalyst of any one of Embodiments 30 to 33, wherein the first layer does not comprise platinum group metal supported on the metal oxide support material.

[157] 35. The catalyst of any one of embodiments 30 to 34, wherein the first layer consists of one or more of the oxidic compound of V, the oxidic compound of W, and the zeolite material comprising one or more of Cu and Fe and, preferably, the metal oxide binder material.

[158] 36. The catalyst of any one of Embodiments 29 to 35, wherein the second layer comprises the platinum group metal supported on the metal oxide support material.

[159] 37. The catalyst of embodiment 36, wherein the second layer comprises platinum group metal at a charge in the range of 2 to 30 g/ft3 (0.070 to 1.059 kg/m3), preferably of 6 to 20 g/ft3 (0.211 to 0.706 kg/m3), more preferably 9.5 to 17 g/ft3 (0.317 to 0.600 kg/m3), more preferably 11 to 17 g/ft3 (0.388 at 0.600 kg/m3).

[160] 38. The catalyst of embodiment 36 or 37, wherein the second layer does not comprise the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe.

[161] 39. The catalyst of any one of Embodiments 36 to 38, wherein the second layer does not comprise the metal oxide binder material as defined in Embodiments 19 or 20.

[162] 40. The catalyst of any one of Embodiments 36 to 39, wherein the second layer consists of the platinum group metal supported on the metal oxide support material.

[163] 41. The catalyst of any one of Embodiments 29 to 40, wherein the first layer is disposed on the substrate, or wherein the second layer is disposed on the substrate.

[164] 42. The catalyst of any one of embodiments 29 to 41, wherein the first layer is disposed on the substrate and the second layer is at least partially disposed on the first layer, or wherein the second layer is disposed on the substrate and in the first layer, is at least partially disposed in the second layer.

[165] 43. The catalyst of any one of embodiments 29 to 42, wherein the first layer is disposed on the substrate and the second layer is disposed completely on the first layer, or wherein the second layer is disposed on the substrate and the first layer completely laid out on the second layer.

[166] 44. The catalyst of any one of embodiments 29 to 43, preferably of any one of embodiments 41 to 43, more preferably of embodiment 43, wherein the substrate is as defined in embodiment 23, and wherein the first layer is disposed at 25 to 100%, preferably at 50 to 100%, more preferably at 75 to 100%, most preferably at 90 to 100% , more preferably in 95 to 100%, more preferably in 100% of the total length of the substrate, preferably from the front end of the substrate, or where the second layer is disposed in 25 to 100% preferably by 50 to 100%, more preferably by 75 to 100%, more preferably by 90 to 100%, more preferably by 95 to 100%, most preferably by 100 % of the total substrate length, preferably from the front end of the substrate.

[167] 45. The catalyst of any one of embodiments 29 to 44, preferably of embodiment 44, wherein the substrate is as defined in embodiment 23, and wherein the second layer is disposed at 25 to 75%, preferably within 35 to 65%, more preferably within 45 to 55%, most preferably within 50% of the total length of the substrate, preferably from the rear end of the substrate, or where the first layer is disposed on 50 to 100%, preferably 75 to 100%, more preferably 95 to 100%, most preferably 100% of the total length of the substrate, preferably from the rear end of the substrate.

[168] 46. The catalyst of any one of Embodiments 29 to 45, wherein the wash coat consists of the first and second layers.

[169] 47. The catalyst of any one of Embodiments 29 to 45, wherein the wash coat further comprises a third layer.

[170] 48. The catalyst of embodiment 47, wherein the third layer further comprises one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe.

[171] 49. The catalyst of embodiment 48, wherein the third layer comprises the zeolite material at a load in the range of 0.2 to 0.8 g/in3 (12.2 to 48.8 kg/m3) , preferably from 0.3 to 0.7 g/in3 (18.3 to 42.7 kg/m3), more preferably from 0.4 to 0.6 g/in3 (24.4 to 36 .6 kg/m3).

[172] 50. The catalyst of any one of embodiments 47 to 49, wherein the substrate as defined in embodiment 23 and wherein the third layer is disposed at 25 to 75%, preferably at 35 to 65 %, more preferably within 45 to 55% of the total length of the substrate, preferably from the trailing edge of the substrate.

[173] 51. The catalyst of any one of embodiments 47 to 50, wherein the first layer is disposed at 25 to 75%, preferably at 35 to 65%, more preferably at 45 to 55% of the total length of the substrate from the front end of the substrate and the second layer is disposed in 25 to 75%, preferably in 35 to 65%, more preferably in 45 to 55% of the total length of the substrate from the end rear of the substrate, wherein the first and second layers in total are preferably arranged over 100% of the total length of the substrate.

[174] 52. The catalyst of embodiment 51, wherein the third layer is disposed on the second layer.

[175] 53. The catalyst of embodiment 52, wherein the third layer is the same length as the second layer.

[176] 54. The catalyst of any one of Embodiments 47 to 53, wherein the wash coat consists of the first, second and third layers.

[177] 55. The catalyst of any one of embodiments 1 to 54, being comprised, as a second catalyst, in a sequence of two or more catalysts, preferably of two catalysts, in which a first catalyst is comprised in said sequence, wherein the substrate of the first catalyst, preferably as defined in any one of embodiments 18 to 20, more preferably, as being of the same chemical structure as the substrate of the second catalyst, more preferably, being identical to the substrate of the second catalyst, wherein the first catalyst comprises a wash coat layer comprising one or more of an oxidic compound of V, an oxidic compound of W and a zeolite material comprising one or more of Cu and Fe, wherein the one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe, preferably as defined in any one of Embodiments 8 to 17.

[178] 56. The catalyst of embodiment 55, wherein the first catalyst comprises one or more of a zeolite material comprising one or more Cu and Fe, preferably a zeolite material comprising Cu, wherein the one or more of a zeolite material comprising one or more Cu and Fe are preferably as defined in any one of Embodiments 8 to 17, wherein more preferably the first catalyst more preferably comprises a catalyst for the selective catalytic reduction of NOx.

[179] 57. The catalyst of any one of embodiments 1 to 56 for use in a process for an exhaust gas treatment as a tetra-functional catalyst for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon.

[180] 58. Use of the catalyst of any one of embodiments 1 to 56 for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, preferably in one treatment of an exhaust gas.

[181] 59. Use of the catalyst of any one of the embodiments 1 to 56 for the treatment of an exhaust gas, preferably for the treatment of an industrial or automotive exhaust gas, more preferably for the treatment of an automobile exhaust gas.

[182] 60. The use of Embodiment 59, wherein the automotive exhaust gas is an exhaust gas from an internal combustion engine, preferably a diesel engine, more preferably a heavy-duty diesel engine.

[183] 61. A method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, preferably in an exhaust gas treatment, using a catalyst of any one of embodiments 1 to 56.

[184] 62. A method for treating an exhaust gas, preferably for treating an industrial or automotive exhaust gas, more preferably for treating an automotive exhaust gas, using a catalyst any one of embodiments 1 to 56.

[185] 63. The method of embodiment 62, wherein the automotive exhaust gas is an exhaust gas from an internal combustion engine, preferably a diesel engine, more preferably a diesel engine. hard work.

[186] 64. The catalyst of any one of embodiments 1 to 56, wherein the catalyst is comprised in an exhaust gas treatment system that is preferably in fluid communication with an internal combustion engine, of preferably a diesel engine, more preferably a heavy duty diesel engine.

[187] 65. An exhaust gas treatment system, preferably in fluid communication with an internal combustion engine, said exhaust gas system comprising the catalyst of any one of embodiments 1 to 56, wherein the internal combustion engine is preferably a diesel engine, more preferably a heavy-duty diesel engine.

[188] 66. The exhaust gas treatment system of embodiment 65, comprising a first reductant injector, a first catalyst for the selective catalytic reduction of NOx, preferably the first catalyst as defined in embodiment 55 or 56, a second catalyst, wherein said second catalyst is the catalyst of any one of Embodiments 1 to 56; a catalyzed soot filter, a second reducing injector, a third catalyst for the selective catalytic reduction of NOx, and a fourth catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia.

[189] 67. The exhaust gas treatment system of embodiment 66, wherein the first catalyst is located upstream of the second catalyst, the second catalyst is located upstream of the third catalyst, and the third catalyst is located upstream of the second catalyst. amount of the fourth catalyst.

[190] 68. The exhaust gas treatment system of embodiment 66 or 67, wherein the first reductant injector is located upstream of the first catalyst.

[191] 69. The exhaust gas treatment system of any one of embodiments 66 to 68, wherein the second reductant injector is located downstream of the catalyzed soot filter and upstream of the third catalyst.

[192] 70. The exhaust gas treatment system of any of the embodiments 66 to 69, which does not contain diesel oxidation catalyst located downstream of the second catalyst and upstream of the catalyzed soot filter, preferably no diesel oxidation catalyst located upstream of the catalyzed soot filter, more preferably, the exhaust gas treatment system does not contain any diesel oxidation catalyst.

[193] 71. The exhaust gas treatment system of any of the embodiments 66 to 70, which does not contain additional catalyst and which no longer contains a reductant injector.

[194] 72. The exhaust gas treatment system of any one of embodiments 66 to 71, wherein the first reducing injector is a urea injector.

[195] 73. The exhaust gas treatment system of any one of embodiments 66 to 72, wherein the second reducing injector is a urea injector.

[196] 74. The exhaust gas treatment system of any one of embodiments 66 to 73, wherein the first catalyst is closely coupled to the internal combustion engine, preferably located directly downstream of the combustion engine internal.

[197] 75. A method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, including: [1] providing a gas stream comprising one or more of NOX, ammonia, nitrogen monoxide and a hydrocarbon; [2] contacting the gas stream supplied in (1) with the catalyst of any one of embodiments 1 to 56.

[198] 76. The method of embodiment 75, wherein the gas stream is an exhaust gas stream from an internal combustion engine, preferably a diesel engine, more preferably a diesel engine heavy duty.

[199] 77. The method of embodiment 75 or 76, wherein the catalyst of any one of embodiments 1 to 56 according to (2) is comprised in an exhaust gas treatment system according to any one of embodiments 65 to 74.

[200] 78. The method of embodiment 75 or 76, wherein to contact the gas stream with the catalyst of any one of embodiments 1 to 56 according to (2), the gas stream is introduced into an exhaust gas treatment system according to any one of embodiments 65 to 74.

[201] 79. A method for the simultaneous selective catalytic reduction of NOx, the oxidation of ammonia, the oxidation of nitrogen monoxide and the oxidation of a hydrocarbon, including: [1] providing a gas stream comprising one or more of NOX, ammonia, nitrogen monoxide and a hydrocarbon; [2] introducing the gas stream into an exhaust gas treatment system according to any one of embodiments 65 to 74 and passing the gas stream through the system.

[202] 80. A process for preparing the catalyst of any one of embodiments 1 to 56, the process comprising disposing one or more slurries on a substrate, one or more slurries comprising the platinum group metal supported on a support material of metal oxide and one or more of the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe, wherein, after a paste has been placed on the substrate, obtained a paste-treated substrate that is dried and calcined.

[203] 81. The process of embodiment 80, comprising (a) placing a first paste on a substrate, obtaining a paste-treated substrate; (b) drying the paste-treated substrate obtained in (a), (c) calcining the substrate treated with dry paste obtained from (b), obtaining the substrate having a first layer disposed thereon.

[204] 82. The process of embodiment 81, wherein the first slurry comprises the platinum group metal supported on a metal oxide support material and one or more of the oxidic compound of V, the oxidic compound of W and the zeolite material comprising one or more of Cu and Fe, wherein the first paste preferably further comprises a disposable adjuvant, preferably one or more of tartaric acid and monoethanolamine, more preferably tartaric acid and monoethanolamine.

[205] 83. The process of variant 82, wherein the substrate has a length of substrate, the process comprising placing the first paste at 50 to 100%, preferably at 75 to 100%, more preferably at 95 to 100%, more preferably, on 100% of the total substrate length.

[206] 84. The process of embodiment 81, further comprising (d) disposing a second paste on the substrate having a first layer disposed thereon, obtaining a paste-treated substrate, (e) drying the paste-treated substrate obtained in (d), (f) calcining the substrate treated with dry paste obtained from (e), obtaining the substrate having a first and a second layer disposed thereon.

[207] 85. The process of embodiment 84, wherein the first slurry comprises one or more of the oxidic compound of V, the oxidic compound of W, and the zeolite material comprising one or more of Cu and Fe and wherein the second slurry comprises platinum group metal supported on a metal oxide support material, or wherein the first slurry comprises platinum group metal supported on a metal oxide support material and the second slurry comprises one or more more of the oxide compound of V, the oxide compound of W and the zeolite material comprising one or more of Cu and Fe.

[208] 86. The process of embodiment 84 or 85, comprising disposing the first paste directly onto the substrate and depositing the second paste completely onto the first layer.

[209] 87. The process of any one of embodiments 84 to 86, preferably of embodiment 76, wherein the substrate is as defined in embodiment 23, the process comprising disposing the first slurry at 25 at 100%, preferably at 50 to 100%, more preferably at 75 to 100%, more preferably at 90 to 100%, more preferably at 95 to 100%, most preferably , on 100% of the total length of the substrate, preferably from the front end of the substrate.

[210] 88. The process of any one of embodiments 84 to 87, preferably of embodiment 87, wherein the substrate as defined in embodiment 23, comprising the process of placing the second paste on 25 to 75%, preferably within 35 to 65%, more preferably within 45 to 55%, most preferably within 50% of the total length of the substrate, preferably from the rear end of the substrate.

[211] 89. The process of any one of embodiments 84 to 88, comprising (g) placing a third paste over the substrate having a first and a second layer thereover, obtaining a paste-treated substrate, h ) Drying the paste-treated substrate obtained from (g), (k) calcining the dry paste-treated substrate obtained from (h), obtaining the substrate having a third layer disposed thereon.

[212] 90. The process of embodiment 89, wherein the third slurry comprises one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe.

[213] 91. The process of embodiment 89 or 90, wherein the substrate as defined in embodiment 23, further comprising disposing the first slurry in 25 to 75%, preferably in 35 to 65%, of more preferably in 45 to 55% of the total length of the substrate from the front end of the substrate, with the second paste arranging in 25 to 75%, preferably in 35 to 65%, more preferably in 45 to 55 % of the total length of the substrate from the back end of the substrate and arranging the third paste at 25 to 75%, preferably at 35 to 65%, more preferably at 45 to 55% of the total length of the substrate, from preferably from the rear edge of the substrate.

[214] 92. The process of embodiment 91, comprising arranging the third slurry in the second layer preferably along the same length as the second layer.

[215] 93. The process of any one of embodiments 81 to 92, wherein one or more of the first suspension of embodiment 81, the first suspension of embodiment 84, the second suspension and the third suspension further comprises , as the liquid component, one or more of water, methanol, ethanol, isopropanol, n-propanol, formic acid, acetic acid and propionic acid, preferably one or more of water and acetic acid, most preferably water.

[216] 94. The process of any one of embodiments 81 to 93, wherein one or more of the first suspension of embodiment 81, the first suspension of embodiment 84 and the third suspension further comprises one or more of zirconylacetate, a silicate, silica, an aluminate, alumina, a titanate and titania, preferably zirconylacetate.

[217] 95. The process of any one of embodiments 81 to 94, wherein the drying according to one or more of (b), (e) and (h) is carried out using a gas atmosphere having a temperature in the range from 90 to 170°C, preferably from 100 to 140°C, and more preferably from 110 to 130°C.

[218] 96. The process of any one of embodiments 81 to 95, wherein the calcination according to one or more of (c), (f) and (k) is carried out using a gas atmosphere having a temperature in the range from 350 to 550°C, preferably from 400 to 500°C, more preferably from 440 to 460°C.

[219] 97. The process of any one of the embodiments 81 to 96, comprising disposing one or more of the first slurry, the second slurry and the third slurry by wet soaking or spraying, preferably, by wet impregnation.

[220] The present invention is further illustrated by the following examples and reference examples.

EXAMPLES REFERENCE EXAMPLE 1: DETERMINATION OF D90 VALUES

[221] The D90 particle size as stated in the context of the present invention was measured with a Sympatec particle size instrument using laser diffraction (HELOS system from Sympatec allowing the determination of the particle size distribution in the range of 0.1 to 8,750 micrometers). According to this method, the particle size distribution was evaluated with a parameterless and model-independent mathematical algorithm, performed by introducing the Phillips-Twomey algorithm for the inversion process.

REFERENCE EXAMPLE 2: PREPARATION OF A CUCHA ZEOLITE

[222] The zeolite material having the structural structure of the CHA type comprising Cu and used in the examples of the present invention was prepared according to the teachings of US 8,293,199 B2. Particular reference is made to Inventive Example 2 of US 8,293,199 B2, column 15, lines 26 to 52.

EXAMPLE 1: PREPARATION OF A CATALYST COMPRISING A WASH COATING LAYER

[223] A solution of a platinum precursor with platinum as an amine-stabilized Pt(iV) hydroxo complex (Pt content between 10 and 20% by weight) was added dropwise at 0.25 g/in3 (15, 2 kg/m3) of zirconia-alumina (alumina doped with 20% by weight of zirconia, Puralox® SBa-200 Zr20, Sasol) under constant agitation, thus carrying out an incipient moisture impregnation. The amount of liquid added was properly calculated to fill the pore volume of the zirconia alumina. The final solid content after incipient wetting was approximately 75% by weight. The resulting mixture after incipient moisture impregnation was pre-calcined at 590 °C for four hours to remove any moisture and to fix the platinum on the metal oxide support material giving a dry platinum content of 5 g/ft3 (0.176 Kg/m3).

[224] Separately, 0.08 g/in3 (4.9 kg/m3) (calculated as ZrO2) zirconyl acetate solution with between 29.5 and 30 wt% solids was added to water to create a mixture with a solids content of approximately 10% by weight. To this, 1.66 g/in3 (101.3 kg/m3) of the CuCHA zeolite prepared according to reference example 2 of the present invention was added. The resulting slurry was then milled until the resulting D90 particle size, determined as described in Reference Example 1, was between 3.5 micrometers and 6 micrometers in diameter. Subsequently, the pre-calcined Pt-impregnated zirconia-alumina was made into a paste. First, tartaric acid in a proportion of five times the amount of Pt remaining after pre-calcination was added to the water as well as monoethanolamine in a proportion of 1/10 the amount of tartaric acid. Second, the Pt-impregnated zirconia-alumina was added to this solution and mixed into the solution, thus forming a paste. The slurry was then milled to a D90 particle size, determined as described in Reference Example 1, being between 9 micrometers and 11 micrometers in diameter. To this slurry, CuCHA direct exchange zeolite slurry was added and mixed, creating the final slurry that is ready for disposal. The final slurry was then placed along the entire length of honeycombed cordierite monolith substrates (10.5” x 3” cylindrical substrate with 300 cells per square inch and 5 mil wall thickness). Afterwards, the substrates were dried to remove between 85 and 95% moisture and were then calcined at 450 °C. The total dry gain after calcination was 2.0 g/in3 (122.0 kg/m3).

EXAMPLE 2: PREPARATION OF A CATALYST COMPRISING A WASH COAT LAYER

[225] The procedure as in Example 1 was repeated with the exception that 0.25 g/in3 (15.2 kg/m3) of titania was used instead of zirconia-alumina. The total dry gain after calcination was 2.0 g/in3 (122.0 kg/m3).

EXAMPLE 3: PREPARATION OF A CATALYST CONTAINING A WASH COATING LAYER

[226] The procedure as per Example 1 was repeated with the exception that 1.0 g/in3 (61.0 kg/m3) was used instead of 0.25 g/in3 (0.25 kg/m3) of zirconia-alumina (alumina doped with 20% by weight of zirconia, Puralox® SBa-200 Zr20, Sasol). The total dry gain after calcination was 2.75 g/in3 (167.8 kg/m3).

EXAMPLE 4: PREPARATION OF A CATALYST COMPRISING TWO LAYERS OF WASH COATING

[227] For the first layer (bottom layer), 0.08 g/in3 (4.9 kg/m3) solution of zirconylacetate with between 29.5 and 30 wt% solids was added to water to create a mixture with a solids content of approximately 10% by weight. To this, 1.66 g/in3 (101.3 kg/m3) of the CuCHA zeolite prepared according to reference example 2 of the present invention was added. The resulting slurry was then milled until the resulting D90 particle size determined as described in Reference Example 1 was between 9 micrometers and 12 micrometers in diameter. The slurry was then placed over the entire length of honeycombed cordierite monolith substrates (10.5” x 3” cylindrical substrate with 300 cells per square inch and 5 mil wall thickness). Afterwards, the substrates were dried to remove between 85 and 95% moisture and were then calcined at 450 °C. The total dry gain of the first layer after calcination was 1.75 g/in3 (106.8 kg/m3).

[228] For the second layer (top layer), a solution of a platinum precursor with platinum as an amine-stabilized Pt(iV) hydroxo complex was diluted to 20% and then added dropwise at 0.5 g/in3 (30.5 kg/m3) of silica-alumina (alumina doped with 1.5 wt% silica, Siralox® 1.5/100, Sasol) under constant agitation, thus carrying out an incipient moisture impregnation. The amount of liquid added was properly calculated to fill the silica-alumina pore volume. To this incipient water saturation mixture, acetic acid was added in the amount of 9% by weight of the target total dry gain of the topcoat and additional water. The final solid content after incipient wetting impregnation was approximately 70% by weight. Water was then added to the mixture along with n-octanol based on 0.2% of the topcoat target dry gain. The solids content after this step was between 43 and 47% by weight. The slurry was then milled until the D90 particle size, determined as described in Reference Example 1, was between 6 micrometers and 9 micrometers in diameter. The slurry was then placed from the back end of the honeycomb monolith substrate at 50% of the length of the substrate to form the top layer giving a dry platinum content of 10 g/ft3 (0.353 kg/m3) for the corresponding layer ( corresponding to a Pt content of 5 g/ft3 (0.176 kg/m3) in relation to the total substrate). The substrate was then dried to remove 85 to 95% of the moisture and then calcined at 450 °C. The total dry gain of the second layer after calcination was 0.51 g/in3(31.1 kg/m3).

EXAMPLE 5: PREPARATION OF A CATALYST WITH THREE LAYERS OF WASH COATING

[229] For the second Pt-based layer (bottom layer), a solution of a platinum precursor with platinum as an amine-stabilized Pt(iV) hydroxo complex was diluted to 20% and then added dropwise to 1, 0 g/in3 (61.0 kg/m3) of silica-alumina (alumina doped with 1.5% by weight of silica, Siralox® 1.5/100, Sasol) under constant agitation, thus carrying out an incipient moisture impregnation . The amount of liquid added was properly calculated to fill the silica-alumina pore volume. To this incipient water saturation mixture, acetic acid was added in the amount of 9% by weight of the intended total dry gain of the second layer and additional water. The final solids content after incipient wetting was approximately 70% by weight. Water was then added to the mixture along with n-octanol based on 0.2% of the target dry gain of the second layer. The solids content after this step was between 43 and 47% by weight. The slurry was then milled until the D90 particle size determined as described in Reference Example 1 was between 6 micrometers and 9 micrometers in diameter. The second layer slurry containing Pt was then placed from the back end of a honeycomb cordierite monolith substrate (10.5" x 3" cylindrical substrate with 300 cells per square inch and 5 mil wall thickness) to 50% of the length of the substrate giving a dry platinum content of 10 g/ft3 (0.353 kg/m3) for the corresponding layer (corresponding to a Pt content of 5 g/ft3 (0.176 kg/m3) in relation to the substrate in the total). The substrate was then dried to remove 85 to 95% of the moisture and then calcined at 450 °C.

[230] Next, a zeolite slurry was produced. Zirconylacetate solution with between 29.5 and 30% solids by weight (amount calculated as 1/20 of the amount of zeolite (dry/dry basis)) was added to water to create a mixture with a solids content of approximately 10% by weight. To this, 1.66 g/in3 (101.3 kg/m3) of the CuCHA zeolite prepared according to reference example 2 of the present invention was added. The resulting slurry was then milled until the D90 particle size determined as described in Reference Example 1 was between 9 micrometers and 12 micrometers in diameter. To form the first layer, the zeolite slurry was placed 50% of the length of the honeycombed cordierite monolith substrates, on top of which the second layer was already laid, starting from the front end of the substrate. The dry gain of the first layer was 1.75 g/in3 (106.8 kg/m3). Afterwards, the substrates were dried to remove between 85 and 95% moisture and were then calcined at 450 °C.

[231] Finally, the zeolite slurry was again used to coat the third layer (outer top coat). The slurry was arranged to a length of 50% of the length of the honeycomb monolith substrates from the rear edge of the substrate. The dry gain of the third layer was 0.5 g/in3 (30.5 kg/m3). Afterwards, the substrates were dried to remove 85 to 95% of the moisture and then calcined at 450 °C.

[232] The total dry gain after calcination was 1.01 g/in3 (61.6 kg/m3).

EXAMPLE 6: PREPARATION OF A CATALYST COMPRISING A WASH COATING LAYER

[233] The procedure as in Example 1 was repeated with the exception that 0.5 g/in3 (30.5 kg/m3) was used instead of 0.25 g/in3 (15.2 kg/m3 ) of zirconia-alumina-zirconia-alumina. The total dry gain after calcination was 2.25 g/in3 (137.3 kg/m3).

EXAMPLE 7: PREPARATION OF A CATALYST COMPRISING TWO LAYERS OF WASH COATING

[234] For the first layer (bottom layer), a solution of a platinum precursor with platinum as an amine-stabilized Pt(iV) hydroxo complex was diluted to 20% and then added dropwise at 0.5 g/in3 (30.5 kg/m3) of silica-alumina (alumina doped with 1.5 wt% silica, Siralox® 1.5/100, Sasol) under constant agitation, thus carrying out an incipient moisture impregnation. The amount of liquid added was properly calculated to fill the silica-alumina pore volume. To this incipient moisture soak mixture, acetic acid was added in the amount of 9% by weight of the intended total dry gain of the bottom layer and additional water. The final solid content after incipient wetting impregnation was approximately 70% by weight. Water was then added to the mixture along with n-octanol based on 0.2% of the target dry gain of the bottom coat. The solids content after this step was between 43 and 47% by weight. The slurry was then milled until the D90 particle size, determined as described in Reference Example 1, was between 6 micrometers and 9 micrometers in diameter. The slurry was then discarded from the back end of the honeycomb monolith substrate (10.5" x 3" cylindrical substrate with 300 cells per square inch and 5 mil wall thickness) at 100% of the length of the substrate to form the layer. below a dry platinum content of 16 g/ft3 (0.565 kg/m3) for the corresponding layer (corresponding to a Pt content of 8 g/ft3 (0.282 kg/m3) relative to the substrate in total). The substrate was then dried to remove 85 to 95% of the moisture and then calcined at 450 °C. The total dry gain of the first layer after calcination was 0.51 g/in3 (31.1 kg/m3).

[235] For the second layer (top layer), 0.17 g/in3 (10.3 kg/m3) solution of zirconylacetate with between 29.5 and 30 wt% solids was added to water to create a mixture with a solids content of approximately 10% by weight. To this, 3.33 g/in3 (203.2 kg/m3) of the CuCHA zeolite prepared according to reference example 2 here was added. The resulting slurry was then milled until the resulting D90 particle size determined as described in Reference Example 1 was between 9 micrometers and 12 micrometers in diameter. The slurry was then placed along the entire length (i.e., 100% of the substrate length) of honeycombed cordierite monolith substrates. Afterwards, the substrates were dried to remove between 85 and 95% moisture and were then calcined at 450 °C. The total dry gain of the second layer after calcination was 3.5 g/in3 (213.5 kg/m3).

[236] The total dry gain of the final product was 4.0 g/in3 (244.1 kg/m3).

EXAMPLE 8: PREPARATION OF A CATALYST COMPRISING A WASH COATING LAYER

[237] A solution of a platinum precursor with platinum as an amine-stabilized Pt(iV) hydroxo complex (Pt content between 10 and 20% by weight, produced in-house by BASF) was added dropwise to 0.25 g /in3 (15.2 kg/m3) of zirconia-alumina (alumina doped with 20 wt% zirconia, Puralox® SBa-200 Zr20, Sasol) under constant agitation, thus performing an incipient moisture impregnation. The amount of liquid added was properly calculated to fill the pore volume of the zirconia alumina. The final solid content after incipient wetting was approximately 75% by weight. The resulting mixture after incipient wet impregnation was pre-calcined at 590°C for four hours to remove any moisture and to fix the platinum on the metal oxide support material giving a dry platinum content of 8 g/ft3 (0.282 kg /m3). Separately, 0.08 g/in3 (4.88 kg/m3) (calculated as ZrO2) solution of zirconylacetate with between 29.5 and 30 wt% solids was added to water to create a mixture with a solids content of approximately 10% by weight. To this, 3.33 g/in3 (203.2 kg/m3) of the CuCHA zeolite prepared according to reference example 2 here was added. The resulting slurry was then milled until the resulting D90 particle size, determined as described in Reference Example 1, was between 3.5 micrometers and 6 micrometers in diameter. Subsequently, the pre-calcined Pt-impregnated zirconia-alumina was made into a paste. First, tartaric acid in a proportion of five times the amount of Pt remaining after precalcination was added to water as well as monoethanolamine in a proportion of 1/10 of the amount of tartaric acid. Second, the Pt-impregnated zirconia-alumina was added to this solution and mixed into the solution creating a paste. The slurry was then milled until the D90 particle size, determined as described in Reference Example 1, was between 9 micrometers and 11 micrometers in diameter. To this slurry, CuCHA direct exchange zeolite slurry was added and mixed, creating the final slurry that is ready for disposal. The final slurry was then placed along the entire length of cordierite monolith substrates in a cylindrical substrate honeycomb (10.5” x 3” with 400 cells per square inch and 4 mil wall thickness). Afterwards, the substrates were dried to remove between 85 and 95% moisture and were then calcined at 450 °C. The total dry gain after calcination was 3.75 g/in3 (228.8 kg/m3).

EXAMPLE 9: USE OF THE CATALYST OF EXAMPLES 1 TO 6 - NO2 PRODUCTION

[238] The catalysts were tested in a diesel system simulator capable of emulating the transients experienced by a catalyst downstream of a combustion engine. The tests were carried out under steady state condition. The dimensions of the cores were 1” (diameter) x 3” (length). All gas composition measurements were performed on an FTIR spectrometer. Tests to measure NO2 production were performed under NOx-only conditions, meaning that no ammonia was added. The catalysts of Examples 1 to 6 were tested using a gas characterized by content as shown below. Space velocity for each test was set to 100,000 h-1. According to the present invention, space velocity is understood as the number of volumes of exhaust gas equal to the volume of coated catalyst that is passed through it every hour. Space velocity is a means of eliminating any catalyst size influences when making performance comparisons. Space velocity is calculated by the volumetric gas flow rate [m3/h] per volume of catalyst [m3] and is therefore expressed in the unit [1/h]. Thus, the NO2/NOx ratio was determined in relation to the gas temperature, the amount of NOx being equal to the sum of the amounts of NO and NO2. The resulting curve represents the light curve. The shutdown curve was measured between 150 and 450 °C for each of the catalysts of Examples 1 to 6, whereby a ramp rate (for both acceleration and deceleration times) of 10 K/min was established. Initially, the light curve was measured during heating (boosting). Then, the temperature was maintained at 450 °C for 10 min. After that, the light curve was measured when cooling down (decelerating).TABLE 1

[239] Characteristics of the gas used

[240] The results for shutdown are shown in Figures 1 and 2, Samples 1 to 6 refer to Examples 1 to 6 respectively. Figure 1 shows the cut-off curve for acceleration. As can be taken from Figure 1, it was found that the catalyst of Example 1 according to the present invention (see sample 1) shows the highest NO2/NOx ratio in the temperature range of 250 to 425 °C and the catalyst of Example 4 (see sample 4) in the temperature range of 175 to 215 °C. Figure 2 shows the shutdown curve for deceleration, samples 1 to 6 refer to Examples 1 to 6 respectively. As can be seen from Figure 2, the catalyst from Example 4 (see sample 4) shows the highest NO2/NOx ratio in the temperature range 290 to 450 °C, the catalyst from Example 5 (see sample 5) in the range temperature from 240 to 265 °C and the catalyst of Example 1 (see sample 1) below 230 °C.

EXAMPLE 10: USE OF THE CATALYST OF EXAMPLES 1 TO 6 - AMMONIA OXIDATION, N2O PRODUCTION AND NOx PRODUCTION

[241] In order to determine the ammonia oxidation efficiency, the N2O production and the NOx production of the catalysts of Examples 1 to 6, the ammonia slip, the N2O production, and the NOx production, respectively, were measured at steady state points. Eight steady-state points were chosen to balance the temperature range and test suitability. The temperature range of 200 to 450°C is considered to be most relevant for heavy-duty diesel operations. The gas concentrations were considered to represent potential concentrations to be encountered by an AMox in operation. NOx would normally contain only NO and far less than the engine output due to the effect of an SCR catalyst located upstream. If operating under overdosing conditions (ie, more reductant is in the gas stream than NOx), there would be an excess of NH3 entering the AMox compared to NOx. The O2 and H2O concentrations are considered consistent with typical operations diesel engines. Furthermore, the given space velocity was considered adequate for a typical Euro VI AMox volume. The characteristics of the eight steady state points are shown in Table 1 below. Space velocity was fixed at 120,000 h-1. TABLE 2

[242] Characteristics of Steady State Point Measurements

AMMONIA OXIDATION

[243] The results of the ammonia slip measurements are presented in Figure 3, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 3 shows the ammonia slip with respect to each steady state point. Thus, the catalyst from Example 1 (see sample 1) was found to have the lowest ammonia slip of all Examples for each steady-state point.

N2O PRODUCTION

[244] The results of measurements of N2O production are shown in Figure 4, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 4 shows the N2O production relative to each steady state point. Surprisingly, the catalyst of Example 2 (see sample 2) exhibits the lowest N2O selectivity of all catalysts on average, in particular the catalyst exhibits the lowest N2O production produced at steady state points 2 to 7. of equilibrium 8, the catalyst from Example 1 (see sample 1) shows the lowest N2O production.

THE PRODUCTION OF NOX

[245] The NOx production results are shown in Figure 5, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 5 shows NOx production relative to each steady state point. Thus, it was surprisingly found that the catalyst of Example 2 (see sample 2) shows the least amount of NOx production at steady state points 1 to 6, whereas the catalyst of Example 1 (see sample 1) shows the lowest lower N2O production at steady state points 7 and 8.

EXAMPLE 11: USE OF THE CATALYST OF EXAMPLES 1 TO 6 - DENOX PERFORMANCE, NOx SLIPS, NH3 SLIPS, Nθ2 PRODUCTION

[246] To measure DeNOx performance, NOx slip, ammonia slip, and NO2 production, the relative amount of reduced NOx was determined at five different steady state points. Similar to the AMox test, the five steady-state points were chosen to balance the most relevant temperatures for the SCR with test convenience. Between 250 and 400 °C, almost all SCR catalysts are very active, so measurements at these temperatures would not give as much information.

[247] From 175 °C to 250 °C, the NO-only activity of an SCR catalyst is greatly stressed while above 400 °C, the extent of NH3 oxidation can be observed, although this reaction becomes more noticeable at higher temperatures. (higher than 400 °C). However, temperatures in excess of 400 °C are rarely encountered in typical operations. It is considered that the NH3 adsorption capacity of the catalyst is much higher at lower temperatures and that, therefore, it takes longer to equilibrate and reach maximum conversion. Thus, lower temperatures are maintained much longer than higher temperatures. With regard to gas composition, these are values that may represent European engine calibrations with overdose. (Note that the NO concentration here is much higher than for the AMox test as this is a test for SCR conversion, not for NO or NH3 oxidation.)

[248] The temperature and duration of each steady state point are given in Table 3 below, as well as the characteristics of the gas used. Space velocity was fixed at 62,000 h-1.TABLE 3

[249] Characteristics of DeNOx measurements

DENOX PERFORMANCE

[250] Results for DeNOx performance are shown in Figure 6, where samples 1 to 6 refer to Examples 1 to 6, respectively. As can be seen from Figure 6, the catalyst from Example 1 (see sample 1) surprisingly shows the best DeNOx performance at steady state points 1, 2 and 3, while the catalyst from Example 4 (see sample 4) shows the best performance of DeNOx at steady state point 4 and the catalyst from Example 5 (see sample 5) at steady state point 5.

NOX SLIP

[251] In addition, NOx slip was determined. The results of the respective measurements are shown in Figure 7, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 7 shows the NOx slip relative to each steady state point. As can be seen in Figure 7, the catalyst from Example 1 (see sample 1) exhibits the lowest NOx slip at steady state points 1, 2 and 3, while the catalyst from Example 4 (see sample 4) exhibits the lowest minor NOx slip at steady state points 4 and the catalyst from Example 5 (see sample 5) at steady state point 5.

AMMONIA SLIP

[252] In addition, ammonia slip was determined. The results are shown in Figure 8, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 8 shows the ammonia slip with respect to each steady state point. In it, it can be seen that the catalyst from Example 1 (see sample 1) shows the least ammonia slip at steady state points 1 to 4, while the ammonia slip at steady point 5 is almost similar for all catalysts. The catalyst of Example 1 (see sample 1) was found to oxidize about 22 ppm of ammonia at 220°C, about 55 ppm at 225°C, and about 90 ppm at 250°C. In comparison, the catalyst in Example 5 (see sample 5) oxidizes about 22 ppm of ammonia at 200°C, about 30 ppm at 225°C, and 65 ppm at 250°C.

NO2 PRODUCTION

[253] In addition, NO2 production was determined. The results of the respective measurements are presented in Figure 9, where samples 1 to 6 refer to Examples 1 to 6, respectively. Figure 9 shows NO2 production relative to each steady state point. It can be seen that NO2 levels are generally very low. Furthermore, it can be seen that the catalyst from Example 1 (see sample 1) shows the highest NO2 production at steady state points 4 and 5, while the NO2 production at steady state points 1 to 3 are almost similar. for all catalysts.

EXAMPLE 12: USE OF THE CATALYST FROM EXAMPLES 7 AND 8 TO INFLUENCE THE NO2/NOx RATIO

[254] The catalysts of Examples 7 and 8 were tested on a EU VI non-EGR 13L diesel combustion engine in a test cell. The tests were carried out under steady state condition. A urea doser was located downstream of the engine, followed by the rear exhaust gas treatment in a cone piping configuration. Seven steady-state points were chosen to balance the temperature range and test suitability. The characteristics of the seven steady state points that are designated as load points (LP1 to LP7) are shown in Table 4 below. TABLE 4

[255] Characteristics of the seven steady-state point measurements

[256] All gas composition measurements were performed on an FTIR spectrometer. The tests for evaluating the NO2/NOx ratio were performed under two different conditions in relation to the ammonia to nitrogen ratio (NSR) being (1) an NSR of 0 and (2) an NSR of 0.5.

[257] Thus, the NO2 to NOx ratio was determined with respect to each steady-state point, where the amount of NOx is equal to the sum of the amounts of NO and NO2. The results of the measurements are shown in Figures 10 and 11, where in both Figures the "Layered AMox design 8 g/ft3" refers to Example 7 and "Mixed AMox design 8 g/ft3" refers to Example 8. It can be seen from Figure 10 that the catalyst from Example 8 (“Mixed AMox 8 g/in3”) shows a higher NO2 to NOx ratio for the steady state points LP1, LP2, LP3, LP5, LP6 and LP7 compared to Example 7 ("AMox 8 g/in3 ") when an ammonia to nitrogen ratio (NSR) of 0 is applied. At the LP4 steady state point, the catalyst of Example 7 shows a higher NO2 to NOx ratio. It can be taken from Figure 11 that the catalyst from Example 8 shows a higher NO2 to NOx ratio for steady state points LP1, LP2, LP3, LP5, LP6 and LP7 compared to Example 7 (“AMox layered 8 g/in3 ”) when an ammonia to nitrogen ratio (NSR) of 0.5 is applied.

BRIEF DESCRIPTION OF THE FIGURES

[258] Figure 1: Shows the turn-off curve for samples 1 to 6 when heating the sample up (turn-off curve for acceleration). Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the temperature is shown along the abscissa and the NO2/NOx ratio is shown along the ordinate.

[259] Figure 2: Shows the deactivation curve of samples 1 to 6 when cooling the sample (deactivation curve for deceleration). Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the temperature is shown along the abscissa and the NO2/NOx ratio is shown along the ordinate.

[260] Figure 3: shows the ammonia slip from samples 1 to 6 for each of the eight steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the ammonia slip is shown on the ordinate with respect to each of the eight steady-state points for samples 1 through 6 shown on the abscissa.

[261] Figure 4: shows the N2O production of samples 1 to 6 for each of the eight steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, N2O production is shown on the ordinate relative to each of the eight steady state points for samples 1 to 6 shown on the abscissa.

[262] Figure 5: Shows the NOx production for samples 1 to 6 for each of the eight steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, NOx production is shown on the ordinate relative to each of the eight steady state points for samples 1 to 6 shown on the abscissa.

[263] Figure 6: Shows the DeNOx performance of samples 1 through 6 for each of the five steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the relative amount of reduced NOx is shown on the ordinate with respect to each of the five steady-state points for samples 1 through 6 shown on the abscissa.

[264] Figure 7: shows the NOx slip from samples 1 to 6 for each of the five steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the NOx slip is shown on the ordinate with respect to each of the five steady-state points for samples 1 to 6 shown on the abscissa.

[265] Figure 8: shows the ammonia slip from samples 1 to 6 for each of the five steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, the ammonia slip is shown on the ordinate with respect to each of the five steady-state points for samples 1 through 6 shown on the abscissa.

[266] Figure 9: Shows the NO2 production of samples 1 to 6 for each of the five steady state points. Samples 1 to 6 refer to the catalysts of Examples 1 to 6, respectively. In the Figure, NO2 production is shown on the ordinate relative to each of the five steady state points for samples 1 to 6 shown on the abscissa.

[267] Figure 10: shows the NO2/NOx ratio in the ammonia to nitrogen ratio (normalized stoichiometric ratio = NSR) from 0 for the “Project AMox in layers 8 g/ft3” and for the “Project AMox mixed 8 g/ft3 ” for each of the seven steady state points. “8 g/ft3 Layered AMox Design” refers to Example 7 and “8 g/ft3 Mixed AMox Design” refers to Example 8. In the Figure, the NO2/NOx ratio is shown on the ordinate relative to each one of the seven steady state points for the “Project AMox layered 8 g/ft3” and for the “Project AMox mixed 8 g/ft3” shown on the abscissa.

[268] Figure 11: shows the NO2/NOx ratio in the ammonia to nitrogen ratio (NSR) of 0.5 for the “Project AMox in layers 8 g/ft3” and for the “Project AMox mixed 8 g/ft3” for each of the seven steady state points. “8 g/ft3 Layered AMox Design” refers to Example 7 and “8 g/ft3 Mixed AMox Design” refers to Example 8. In the Figure, the NO2/NOx ratio is shown on the ordinate relative to each one of the seven steady state points for the “Project AMox layered 8 g/ft3” and for the “Project AMox mixed 8 g/ft3” shown on the abscissa. LITERATURE CITED - WO 2015/189680 A1 - US 9,272,272 B2 - US 8,715,618 B2 - US 8,293,199 B2 - US 8,883,119 B2 - US 8,961,914 B2 - US 9,242,238 B2

Claims (16)

1. EXHAUST GAS TREATMENT SYSTEM, characterized in that said exhaust gas system comprises: a first reducing injector, a first catalyst for the selective catalytic reduction of NOx, a second catalyst, wherein the second catalyst is a catalyst comprising a washcoat comprising one or more layers, the washcoat being disposed on a substrate, the washcoat comprising: i) a platinum group metal supported on a metal oxide support material, and ii) one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe; a catalyzed soot filter, a second reductant injector, a third catalyst for the selective catalytic reduction of NOx, and a fourth catalyst for the selective catalytic reduction of NOx and/or for the oxidation of ammonia, where the system does not contain a catalyst diesel oxidation. 2. SYSTEM according to claim 1, characterized in that the wash coating of the second catalyst comprises: i) a platinum group metal supported on a metal oxide support material, and ii) a zeolite material comprising one or more more than Cu and Fe. 3. SYSTEM according to any one of claims 1 to 2, characterized in that the platinum group metal of the second catalyst is one or more of Pt, Pd and Rh, preferably one or more of Pt and Pd, more preferably Pt, in that the metal oxide support material is preferably one or more of alumina, zirconia-alumina, silica-alumina, titania, zirconia-titania and ceria, more preferably, one or more of alumina, silica-alumina and zirconia-alumina, more preferably, zirconia-alumina. 4. SYSTEM, according to any one of claims 1 to 3, characterized in that the structural structure of the zeolite material of the second catalyst comprises a tetravalent element Y which is one or more of Si, Sn, Ti, Zr and Ge, preferably Si, and wherein the backbone of the zeolite material preferably comprises a trivalent element X which is one or more of B, Al, Ga and In, preferably Al. 5. SYSTEM according to any one of claims 1 to 4, characterized in that the zeolite material of the second catalyst has a structural structure of the type AEI, GME, BEA, CHA, FAU, FER, HEU, LEV, MEI, MEL, MFI or MOR, more preferably of the AEI, GME, CHA, MFI, BEA, FAU or MOR type, preferably of the CHA, AEI or BEA type, more preferably of the CHA or AEI type, and most preferably of the CHA type. 6. SYSTEM, according to any one of claims 1 to 5, characterized in that the zeolite material comprises Cu. 7. SYSTEM, according to any one of claims 1 to 6, characterized in that the substrate of the second catalyst has a plurality of passages that extend longitudinally, formed by walls that extend longitudinally, delimiting and defining the passages and a full longitudinal length extending between a front end and a rear end of the substrate. 8. SYSTEM according to any one of claims 1 to 7, characterized in that the second catalyst wash coat consists of one layer. 9. SYSTEM, according to claim 8, characterized in that the substrate has a substrate length and in which the one layer is arranged in 50 to 100%, preferably in 75 to 100%, more preferably in 95 to 100%, more preferably on 100% of the total substrate length. 10. SYSTEM according to any one of claims 1 to 7, characterized in that the wash coating of the second catalyst comprises a first and a second layer, wherein the first layer preferably comprises one or more of the oxidic compound of V, the oxidic compound of W, and the zeolite material comprising one or more of Cu and Fe, preferably the zeolite material comprising one or more of Cu and Fe, and wherein the second layer comprises platinum group metal supported on the support material of W metal oxide. 11. SYSTEM, according to claim 10, characterized in that the first layer is arranged on the substrate and the second layer is preferably at least partially, preferably completely, arranged on the first layer, or in which the second layer is arranged on the substrate and the first layer is preferably at least partially, preferably completely, disposed on the second layer. 12. SYSTEM according to any one of claims 10 to 11, characterized in that the wash coating of the second catalyst further comprises a third layer, wherein the third layer preferably comprises one or more of an oxidic compound of V, an oxidic compound of W, and a zeolite material comprising one or more of Cu and Fe, preferably a zeolite material comprising one or more of Cu and Fe. 13. SYSTEM, according to any one of claims 1 to 12, characterized in that the system is in fluid communication with an internal combustion engine, in which the internal combustion engine is preferably a diesel engine, more preferably a diesel engine of hard work. 14. SYSTEM according to any one of claims 1 to 13, characterized in that the second catalyst is located upstream of the catalyzed soot filter. 15. SYSTEM according to any one of claims 1 to 14, characterized in that the first reducing injector is a urea injector. 16. SYSTEM according to any one of claims 1 to 15, characterized in that the first catalyst is closely coupled to the internal combustion engine.