NOx Adsorber (NA) catalyst with tunable NOx adsorption and desorption properties

The present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, the catalyst comprising (I) a specific substrate; (ii) a first coating disposed thereon, wherein the first coating comprises a NOx adsorber material comprising (ii.1) a first platinum group metal component and (ii .2) one or more zeolitic materials; and (ill) a second coating disposed on the first coating, wherein the second coating comprises a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania. Further, the present invention relates to a process for the preparation of such a catalyst and to a use thereof.

In the automotive industry, there is a continuous need to reduce NOx emissions from engines as these emissions are harmful for humans. Thus, it is important to cope with present legislations setting limits for NOx emissions. From a technical point of view, it is challenging to remove the NOx emissions directly after the cold-start period as the temperature for the NOx conversion over a catalytic exhaust gas treatment system is comparatively low. NOx adsorption during coldstart period, in particular at temperatures below 300 °C post turbo charger temperatures, can reduce significantly the NOx emissions.

WO 2015/085300 A1 discloses a cold-start catalyst comprising a molecular sieve catalyst and a supported platinum group metal (PGM) catalyst, wherein the molecular sieve catalyst consists essentially of a molecular sieve and a noble metal and the supported PGM catalyst comprises platinum and/or palladium on one or more inorganic carriers. US 2017/0096923 A1 discloses a NOx adsorber catalyst comprising a first NOx adsorber material which is a molecular sieve catalyst comprising a noble metal and a molecular sieve and a second NOx adsorber which comprises palladium supported on an oxide of cerium.

Further, Porta et al. disclose a “Low Temperature NOx Adsorption Study on Pd-Promoted Zeolites”, with respect to different Pd-zeolites such as Pd-BEA, Pd-MFI, Pd-FER and Pd-MOR and their respective NOx adsorption properties. Finally, Zheng et al., “Low-Temperature Pd/Zeolite Passive NOx Adsorbers: Structure, Performance, and Adsorption Chemistry”, and Ryou et aL, “Effect of various activation conditions on the low temperature NO adsorption performance of Pd/SSZ-13 passive NOx adsorber”, also disclose the NOx adsorption properties of Pd-promoted zeolitic materials.

It was therefore an object of the present invention to provide a NOx adsorber catalyst for the treatment of an exhaust gas, being particularly suitable for a respective exhaust gas treatment systems, wherein the catalyst exhibits in particular an improved performance with respect to its NOx adsorption and/or desorption properties, and which in particular permits to increase the NOx adsorption and delay the NOx desorption to higher targeted temperatures, especially after hydrothermal aging. Further, it was an object of the present invention to provide a process for the preparation of such a catalyst. Thus, it was surprisingly found that a NOx adsorber catalyst for the treatment of an exhaust gas according to the present invention can solve the above problems. In particular with respect to the improved performance with respect to the adsorption and/or desorption of NOx, it is attained thanks to the inventive catalyst which particularly comprises a specific NOx adsorber material comprised in a first coating and a specific diesel oxidation material comprised in a second coating. Indeed, it was found that an improved catalyst for the adsorption and/or desorption of NOx can be provided in particular comprising two specific coatings, wherein the first (bottom) coating comprises a specific NOx adsorber material and the second (top) coating comprises a specific diesel oxidation material. It has been surprisingly been found that both of said functions together can achieve an improved performance with respect to the adsorption and/or desorption of NOx. Surprisingly, the NOx adsorber catalyst of the present invention thus shows an excellent behavior as concerns NOx release and NOx adsorption.

I. A NOx adsorber catalyst with a DOC function for the treatment of an exhaust gas

Therefore, the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, wherein the catalyst comprises

(I) a substrate comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough;

(ii) a first coating disposed on the substrate, the first coating comprising a NOx adsorber material comprising

(11.1) a first platinum group metal component;

(11.2) one or more zeolitic materials;

(ill) a second coating disposed on the first coating, the second coating comprising a diesel oxidation material comprising a second platinum group metal component and a non-zeo- litic oxidic material comprising one or more of alumina, silica, zirconia and titania.

Preferably, the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, wherein the catalyst comprises

(I) a substrate comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough;

(ii) a first coating disposed on the substrate, the first coating comprising a NOx adsorber material comprising

(ii.1) a first platinum group metal component;

(ii.2a) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material; or

(ii.2b) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga; or (ii .2c) a zeolitic material having a framework type LEV;

(iii) a second coating disposed on the first coating, the second coating comprising a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania.

It is preferred that the first platinum group metal component according to (ii.1) of the catalyst comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, wherein the first platinum group metal component more preferably comprises, more preferably is, palladium.

It is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the NOx adsorber material comprised in the first coating according to (ii) of the catalyst consist of the first platinum group metal component according to (ii.1) and the one or more zeolitic materials according to (ii.2).

It is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the first coating according to (ii) of the catalyst consist of the NOx adsorber material.

It is preferred that the NOx adsorber material comprised in the first coating according to (ii) of the catalyst comprises from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ce, calculated as CeOz, wherein the NOx adsorber material comprised in the first coating according to (ii) is preferably essentially free of Ce, wherein the first coating according to (ii) more preferably is free of Ce.

It is preferred that the first coating according to (ii) of the catalyst comprises from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ce, calculated as CeOz, wherein the first coating according to (ii) is preferably essentially free of Ce, wherein the first coating according to (ii) more preferably is free of Ce.

According to a first alternative, it is preferred that the first coating according to (ii) of the catalyst comprises (ii.2a) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material.

In the case where the first coating according to (ii) of the catalyst comprises (ii.2a) an 8-mem- bered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the first platinum group metal component according to (ii.1) is comprised in both the 8- membered ring pore zeolitic material and the 10-membered ring pore zeolitic material according to (ii.2a), wherein the first platinum group metal according to (ii.1) more preferably is comprised in said zeolitic materials in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1 ) and the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material according to (ii.2a).

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the 8-membered ring pore zeolitic material according to (ii.2a) has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KFI, ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material according to (ii.2a) has a framework type CHA.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the framework structure of the 8-membered ring pore zeolitic material according to (ii .2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12: 1 to 16: 1 .

In the case where the framework structure of the 8-membered ring pore zeolitic material according to (ii .2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12:1 to 16:1 , it is preferred that Y comprises, more preferably is, Si.

Further in the case where the framework structure of the 8-membered ring pore zeolitic material according to (ii.2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12:1 to 16:1 , it is preferred that X comprises, more preferably is, one or more of Al and B, more preferably Al. Further in the case where the framework structure of the 8-membered ring pore zeolitic material according to (ii.2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12:1 to 16:1 , it is preferred that Y is Si and X is Al.

Further in the case where the framework structure of the 8-membered ring pore zeolitic material according to (ii.2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12:1 to 16:1 , it is preferred that the 10-membered ring pore zeolitic material according to (ii.2a) has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of FER, TON, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER and TON, wherein more preferably the 10-membered ring pore zeolitic material according to (ii.2a) has a framework type FER.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the framework structure of the 10-membered ring pore zeolitic material according to (ii .2a) comprises, preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 45:1 , preferably in the range of from 10:1 to 40:1 , more preferably in the range of from 12:1 to 30:1 , more preferably in the range of from 15:1 to 28:1 , more preferably in the range of from 18:1 to 25:1 .

In the case where that the framework structure of the 10-membered ring pore zeolitic material according to (ii.2a) comprises, preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 45:1 , preferably in the range of from 10:1 to 40:1 , more preferably in the range of from 12:1 to 30:1 , more preferably in the range of from 15:1 to 28:1 , more preferably in the range of from 18:1 to 25:1 , it is preferred that Y comprises, more preferably is, Si. Further in the case where that the framework structure of the 10-membered ring pore zeolitic material according to (ii.2a) comprises, preferably consists of, a tetravalent element Y, a triva- lent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 2:1 to 45:1 , preferably in the range of from 10:1 to 40:1 , more preferably in the range of from 12:1 to 30:1 , more preferably in the range of from 15:1 to 28:1 , more preferably in the range of from 18:1 to 25:1 , it is preferred that X comprises, more preferably is, one or more of Al and B, more preferably Al.

Further in the case where that the framework structure of the 10-membered ring pore zeolitic material according to (ii.2a) comprises, preferably consists of, a tetravalent element Y, a triva- lent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2C>3, is in the range of from 2:1 to 45:1 , preferably in the range of from 10:1 to 40:1 , more preferably in the range of from 12:1 to 30:1 , more preferably in the range of from 15:1 to 28:1 , more preferably in the range of from 18:1 to 25:1 , it is preferred that Y is Si and X is Al.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the weight ratio of the 10-membered ring pore zeolitic material according to (ii .2a) to the 8-membered ring pore zeolitic material according to (ii.2a) is in the range of from 10:1 to 1 :10, more preferably in the range of from 5:1 to 1 :5, more preferably in the range of from 3:1 to 1 :3, more preferably in the range of from 2:1 to 1 :2.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the first coating comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 175 g/ft ³ , more preferably in the range of from 40 to 150 g/ft ³ , more preferably in the range of from 70 to 140 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ . It might alternatively be conceivable that the first coating preferably comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, preferably as elemental Pd, in the range of from 100 to 140 g/ft ³ .

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the first coating comprises the zeolitic materials according to (ii.2a) in an amount in the range of from 80 to 99.5 weight-%, more preferably in the range of from 85 to 99 weight-%, more preferably in the range of from 90 to 99 weight-%, more preferably in the range of from 95 to 98.5 weight-%, based on the weight of the first coating. Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1 ) and the 8-membered ring pore zeolitic material according to (ii.2a) and the 10-membered ring pore zeolitic material according to (ii.2a), wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the 8-membered ring pore zeolitic material according to (ii.2a) and the 10- membered ring pore zeolitic material according to (ii.2a).

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2a) an 8- membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, it is preferred that the NOx adsorber material consists of the first platinum group metal component according to (ii.1), the 8-membered ring pore zeolitic material according to (ii.2a) and the 10-mem- bered ring pore zeolitic material according to (ii.2a).

According to a second alternative, it is preferred that the first coating according to (ii) of the catalyst comprises (ii.2b) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga.

In the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10-mem- bered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that Y comprises, more preferably is, Si.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that X comprises, more preferably is, one or more of Al and B, more preferably Al.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that Y is Si and X is Al. Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that the first platinum group metal component according to (ii.1 ) is comprised in the 10- membered ring pore zeolitic material according to (ii .2b), wherein the first platinum group metal according to (ii.1 ) more preferably is comprised in said zeolitic material in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1) and the 10-membered ring pore zeolitic material according to (ii.2b).

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that the 10-membered ring pore zeolitic material according to (ii.2b) has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER, MFI, TON, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER and MFI, wherein more preferably the 10-membered ring pore zeolitic material according to (ii .2b) has a framework type FER.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that, in the 10-membered ring pore zeolitic material according to (ii.2b), the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 35:1 to 150:1 , more preferably in the range of from 40:1 to 100:1 , preferably in the range of from 45:1 to 80:1 , more preferably in the range of from 48:1 to 70:1 , more preferably in the range of from 50:1 to 65:1.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti , Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that the first coating comprises the first platinum group metal, preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 40 to 120 g/ft ³ , more preferably in the range of from 60 to 100 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that the first coating comprises the 10-membered ring pore zeolitic material according to (ii.2b) in an amount in the range of from 80 to 99.75 weight-%, more preferably in the range of from 85 to 99.5 weight-%, more preferably in the range of from 90 to 99.25 weight-%, more preferably in the range of from 95 to 99 weight-%, based on the weight of the first coating.

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the 10-membered ring pore zeolitic material according to (ii.2b), wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1 ) and the 10-membered ring pore zeolitic material according to (ii.2b).

Further in the case where the first coating according to (ii) of the catalyst comprises (ii.2b) a 10- membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, it is preferred that the NOx adsorber material consists of the first platinum group metal component according to (ii.1) and the 10-membered ring pore zeolitic material according to (ii.2b).

According to a third alternative, it is preferred that the first coating according to (ii) of the catalyst comprises (ii .2c) a zeolitic material having a framework type LEV.

In the case where the first coating according to (ii) of the catalyst comprises (ii.2c) a zeolitic material having a framework type LEV, it is preferred that the first platinum group metal component according to (ii.1 ) is comprised in the zeolitic material having a framework type LEV according to (ii.2c), wherein the first platinum group metal according to (ii.1) more preferably is comprised in said zeolitic material in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii.2c).

Further in the case where the first coating according to (ii) of the catalyst comprises (ii .2c) a zeolitic material having a framework type LEV, it is preferred that the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1.

In the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that Y comprises, more preferably is, Si.

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that X comprises, more preferably is, one or more of Al and B, more preferably AL

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2C>3, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that Y is Si and X is Al.

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YOz^Os, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that the first coating comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 40 to 120 g/ft ³ , more preferably in the range of from 60 to 100 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2C>3, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that the first coating comprises the zeolitic material having a framework type LEV according to (ii.2c) in an amount in the range of from 80 to 99.75 weight-%, more preferably in the range of from 85 to 99.5 weight-%, more preferably in the range of from 90 to 99.25 weight-%, more preferably in the range of from 95 to 99 weight-%, based on the weight of the first coating.

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2C>3, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight- %, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the zeolitic material having a framework type LEV according to (ii.2c), wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the zeolitic material having a framework type LEV according to (ii.2c).

Further in the case where the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1 , it is preferred that the NOx adsorber material consists of the first platinum group metal component according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii.2c).

It is preferred that the second platinum group metal component of the second coating according to (ill) of the catalyst comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum.

In the case where the second platinum group metal component of the second coating according to (ill) of the catalyst comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, it is preferred according to a first alternative that the second platinum group metal component comprises, preferably is, platinum.

Further in the case where the second platinum group metal component of the second coating according to (ill) of the catalyst comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, it is preferred according to a second alternative that the second platinum group metal component comprises, more preferably is, platinum and palladium, wherein the weight ratio of Pt to Pd, calculated as elemental Pt and Pd, respectively, more preferably is in the range of from 2:1 to 20:1 , more preferably in the range of from 3:1 to 15:1 , more preferably in the range of from 5: to 12:1 , more preferably in the range of from 7:1 to 11 :1.

It is preferred that the second coating according to (ill) of the catalyst comprises the second platinum group metal component, more preferably platinum or platinum and palladium, at a loading, calculated as elemental platinum group metal(s), more preferably as elemental Pd or as elemental Pt and Pd, respectively, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 30 to 100 g/ft ³ , more preferably in the range of from 40 to 80 g/ft ³ , more preferably in the range of from 50 to 70 g/ft ³ . It is preferred that the non-zeolitic oxidic material of the second coating according to (ill) of the catalyst comprises one or more of alumina, silica, zirconia, silica-alumina, silica-zirconia, and alumina-zirconia, more preferably one or more of alumina, silica and zirconia, preferably one or more of alumina and silica.

In the case where the non-zeolitic oxidic material of the second coating according to (ill) of the catalyst comprises one or more of alumina, silica, zirconia, silica-alumina, silica-zirconia, and alumina-zirconia, more preferably one or more of alumina, silica and zirconia, preferably one or more of alumina and silica, it is preferred that the non-zeolitic oxidic material of the second coating according to (ill) comprises alumina, more preferably gamma-alumina, and more preferably further comprises manganese, wherein the non-zeolitic oxidic material of the second coating according to (ill) more preferably comprises alumina and manganese, wherein the non-zeolitic oxidic material more preferably comprises the alumina in an amount in the range of from 80 to 99 weight-%, more preferably in the range of from 85 to 98 weight-%, more preferably in the range of from 90 to 97 weight-%, based on the weight of the non-zeolitic oxidic material.

Further in the case where the non-zeolitic oxidic material of the second coating according to (ill) of the catalyst comprises one or more of alumina, silica, zirconia, silica-alumina, silica-zirconia, and alumina-zirconia, more preferably one or more of alumina, silica and zirconia, preferably one or more of alumina and silica, it is preferred that the non-zeolitic oxidic material of the second coating according to (ill) exhibits a BET specific surface area of greater than 75 m ² /g, more preferably greater than 100 m ² /g, more preferably determined according to Reference Example 1.2.

Further in the case where the non-zeolitic oxidic material of the second coating according to (ill) of the catalyst comprises one or more of alumina, silica, zirconia, silica-alumina, silica-zirconia, and alumina-zirconia, more preferably one or more of alumina, silica and zirconia, preferably one or more of alumina and silica, it is preferred that the non-zeolitic oxidic material of the second coating according to (ill) exhibits a pore volume of greater than 0.04 cm ³ /g, more preferably greater than 0.06 cm ³ /g, more preferably determined according to Reference Example 1 .4.

It is preferred that the second coating according to (ill) of the catalyst further comprises a second non-zeolitic oxidic material, wherein the second non-zeolitic material more preferably comprises one or more of alumina, silica-alumina, titania-alumina, silica and titania, more preferably one or more of alumina and silica-alumina, more preferably silica-alumina.

In the case where the second coating according to (ill) of the catalyst further comprises a second non-zeolitic oxidic material, wherein the second non-zeolitic material more preferably comprises one or more of alumina, silica-alumina, titania-alumina, silica and titania, more preferably one or more of alumina and silica-alumina, more preferably silica-alumina, it is preferred that the second non-zeolitic oxidic material comprises the alumina in an amount in the range of from 80 to 99 weight-%, more preferably in the range of from 85 to 98 weight-%, more preferably in the range of from 90 to 97 weight-%, based on the weight of the second non-zeolitic oxidic material. Further in the case where the second coating according to (iii) of the catalyst further comprises a second non-zeolitic oxidic material, wherein the second non-zeolitic material more preferably comprises one or more of alumina, silica-alumina, titania-alumina, silica and titania, more preferably one or more of alumina and silica-alumina, more preferably silica-alumina, it is preferred that the second non-zeolitic oxidic material of the second coating according to (iii) exhibits a BET specific surface area of greater than 75 m ² /g, more preferably greater than 100 m ² /g, more preferably determined according to Reference Example 1 .2.

Further in the case where the second coating according to (iii) of the catalyst further comprises a second non-zeolitic oxidic material, wherein the second non-zeolitic material more preferably comprises one or more of alumina, silica-alumina, titania-alumina, silica and titania, more preferably one or more of alumina and silica-alumina, more preferably silica-alumina, it is preferred that the second non-zeolitic oxidic material of the second coating according to (iii) exhibits a pore volume of greater than 0.04 cm ³ /g, more preferably greater than 0.06 cm ³ /g, more preferably determined according to Reference Example 1 .4.

It is preferred that the second coating according to (iii) of the catalyst further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12-membered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12-mem- bered ring pore zeolitic material has a framework type BEA.

In the case where the second coating according to (iii) of the catalyst further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12-mem- bered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12-mem- bered ring pore zeolitic material has a framework type BEA, it is preferred that the framework structure of the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises, more preferably consists of, Si, Al and oxygen, wherein the molar ratio of Si:AI, calculated as SiC^AhOs, is in the range of from 2:1 to 60:1 , more preferably in the range of from 10:1 to 50:1 , more preferably in the range of from 15:1 to 40:1 , more preferably in the range of from 20:1 to 30:1 , more preferably in the range of from 22:1 to 28:1.

Further in the case where the second coating according to (iii) of the catalyst further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12- membered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12- membered ring pore zeolitic material has a framework type BEA, it is preferred that the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises iron, wherein the amount of iron in the zeolitic material, calculated as FezOs, more preferably is in the range of from 0.1 to 5 weight-%, more preferably in the range of from 0.5 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the weight of the zeolitic material comprising iron.

Further in the case where the second coating according to (ill) of the catalyst further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12- membered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12- membered ring pore zeolitic material has a framework type BEA, it is preferred that the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises at most 0.001 weight-%, more preferably from 0 to 0.0001 weight-%, more preferably from 0 to 0.00001 weight-%, of iron, calculated as FezOs, more preferably of iron and copper, calculated as FezOs and CuO, respectively. the case where the second coating according to (ill) of the catalyst further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12-membered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12-mem- bered ring pore zeolitic material has a framework type BEA, it is preferred that the weight ratio of the non-zeolitic material of the second coating according to (ill) to the zeolitic material of the second coating according to (ill) is in the range of from 1 :1 to 10:1 , more preferably in the range of from 2:1 to 8:1 , more preferably in the range of from 2.5:1 to 5:1.

It is preferred that the catalyst comprises the second coating according to (ill) at a loading in the range of from 0.5 to 5 g/in ³ , preferably in the range of from 0.75 to 4 g/in ³ , more preferably in the range of from 1 to 3 g/in ³ , more preferably in the range of from 1.25 to 2.5 g/in ³ .

It is preferred that from 98 to 100 weight-%, preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the second coating according to (ill) of the catalyst consist of the second platinum group metal component, the non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64, wherein more preferably the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64; or wherein from 98 to 100 weight-%, preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material, a second non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64, wherein more preferably the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material, a second non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64.

It is preferred that the substrate according to (I) of the catalyst is a flow-through substrate or a wall-flow filter substrate, preferably a flow-through substrate, wherein the flow-through substrate more preferably is one or more of a cordierite flow-through substrate or a metallic flow-through substrate, more preferably a cordierite flow-through substrate.

It is preferred that the substrate according to (I) of the catalyst is a monolith, more preferably a honeycomb monolith.

It is preferred that the first coating according to (ii) of the catalyst is disposed on the surface of the internal walls of the substrate.

It is preferred that the first coating according to (ii) of the catalyst is disposed on the surface of the internal walls of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

It is preferred that the second coating according to (ill) of the catalyst is disposed on the first coating over y % of the substrate axial length, wherein y is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100, wherein more preferably the first coating according to (ii) is disposed on the surface of the internal walls of the substrate over x % of the substrate axial length according to embodiment 70 and wherein x = y.

Preferably, the second coating according to (ill) consist of one single coat.

Alternatively, it is preferred that the second coating (ill) comprises, more preferably consists of,

(iii.1 ) an inlet coat disposed on the first coating extending from the inlet end toward the outlet end of the substrate over y ¹ % of the substrate axial length, wherein y ¹ is in the range of from 20 to 80, more preferably in the range of from 40 to 60, more preferably in the range of from 45 to 55; wherein the inlet coat comprises a diesel oxidation material comprising the second platinum group metal component as defined in the foregoing, the second platinum group metal component more preferably comprising, more preferably being, platinum and palladium, and the non-zeolitic oxidic mate- rial as defined in the foregoing with respect to the second coating (iii), the non-zeolitic oxidic material more preferably comprising, more preferably consisting of, silica and alumina; and

(iii.2) an outlet coat disposed on the first coating extending from the outlet end toward the inlet end of the substrate over y ² % of the substrate axial length, wherein y ² is in the range of from 20 to 80, more preferably in the range of from 40 to 60, more preferably in the range of from 45 to 55, wherein the outlet coat comprises a diesel oxidation material comprising the second platinum group metal component as defined in the foregoing, the second platinum group metal component more preferably comprising, more preferably is, platinum and the non-zeolitic oxidic material as defined in the foregoing, the non-zeolitic oxidic material more preferably comprising, more preferably consisting of, alumina and manganese .

Preferably y ¹ + y ² = y.

Preferably the amount of the second platinum group metal component in the inlet coat (iii.1 ) and the amount of the second platinum group metal component in the outlet coat (iii.2) is in the range of from 15 to 200 g/ft ³ , preferably in the range of from 20 to 175 g/ft ³ , more preferably in the range of from 40 to 150 g/ft ³ , more preferably in the range of from 70 to 140 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

Preferably the catalyst comprises the inlet coat (iii.1 ) at a loading in the range of from 1.0 to 2.0 g/in ³ , more preferably in the range of from 1 .25 to 1 .75 g/in ³ , more preferably in the range of from 1 .4 to 1 .6 g/in ³ .

Preferably the weight ratio of Pt to Pd, calculated as elemental Pt and Pd, in the inlet coat (iii.1 ) is in the range of from 5:1 to 1 :2, more preferably in the range of from 3:1 to 1 :1.

Preferably the inlet coat (iii.1 ) further comprises a zeolitic material as defined in the foregoing with respect to the second coating (iii), more preferably a zeolitic material having a framework type BEA comprising Fe as defined in the foregoing. More preferably, the inlet coat (iii.1) comprises the second platinum group metal component, the non-zeolitic oxidic material and the zeolitic material.

Preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of the outlet coat (iii.2) consists of a zeolitic material. In other words, it is preferred that the outlet coat (iii.2) is essentially free, more preferably free, of a zeolitic material. Preferably the catalyst comprises the outlet coat (ill.2) at a loading in the range of from 0.75 to 1 .8 g/in ³ , more preferably in the range of from 1.1 to 1.5 g/in ³ , more preferably in the range of from 1 .2 to 1 .4 g/in ³ .

It is more preferred that the first coating according to (ii) comprises

(ii.2b) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , more preferably is in the range of from 35:1 to 150:1 , more preferably in the range of from 40:1 to 100:1 , preferably in the range of from 45:1 to 80:1 , more preferably in the range of from 48:1 to 70:1 , more preferably in the range of from 50:1 to 65:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, and that the second coating according to (ill) comprises, preferably consists of, the inlet coat (iii.1) and the outlet coat (iii.2) as defined in the foregoing.

It is preferred that the catalyst consists of the substrate according to (I), the first coating according to (ii) and the second coating according to (ill).

Further, the present invention relates to a process for preparing a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, the process comprising

(1) providing a first mixture comprising water and a NOx adsorber material comprising

(11.1 ) a first platinum group metal component;

(11.2) one or more zeolitic materials;

(2) disposing the first mixture obtained according to (1) on a substrate, comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough, calcining, obtaining a substrate having a first coating thereon;

(3) providing a second mixture comprising water and a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania;

(4) disposing the second mixture obtained according to (3) on the substrate having a first coating thereon obtained according to (2), calcining, obtaining a substrate having a first coating and a second coating thereon.

It is preferred that providing a first mixture comprising water and a NOx adsorber material according to (1) of the process comprises

(a) a first platinum group metal and

(b.1) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, or

(b.2) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein

Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, or

(b.3) a zeolitic material having a framework type LEV.

It is preferred according to a first alternative that (1) of the process comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.1) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material; wherein providing the first mixture comprises admixing the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material, more preferably the H-form of the 8-membered ring pore zeolitic material and the ammonium form of the 10-membered ring pore zeolitic material, more preferably admixing H-CHA and NH ₄ -FER; admixing, more preferably impregnating, the mixture of the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

It is preferred according to a second alternative that (1) of the process comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.2) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YOz^Os, is in the range of from 30:1 to 200:1 , wherein

Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, wherein providing the first mixture comprises admixing, more preferably impregnating, the 10-membered ring pore zeolitic material, more preferably the ammonium form of the 10-membered ring pore zeolitic material, with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

It is preferred according to a third alternative that (1) of the process comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.3) a zeolitic material having a framework type LEV, wherein providing the first mixture comprises admixing, more preferably impregnating, the zeolitic material having a framework type LEV, more preferably the ammonium form of the zeolitic material having a framework type LEV, with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

It is preferred that calcining of the process is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that calcining of the process is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that disposing the first mixture in (2) of the process comprises disposing the first mixture obtained in (1) from the inlet end toward to the outlet end of the substrate over x % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, more preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

It is preferred that, prior to calcining in (2) of the process, drying of the first mixture disposed on the substrate is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, more preferably in the range of from 100 to 120 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that, prior to calcining in (2) of the process, drying of the first mixture disposed on the substrate is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, more preferably in the range of from 0.75 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that calcining in (2) of the process is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that calcining in (2) of the process is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that (3) of the process comprises

(3.1) impregnating a source of the second platinum group metal on the non-zeolitic oxidic material and calcining; (3.2) preparing a mixture with water and the impregnated non-zeolitic oxidic material obtained according to (3.1);

(3.3) optionally adding a second non-zeolitic oxidic material, more preferably selected from the group consisting of alumina, silica-alumina, titania-alumina and manganese-alumina, more preferably silica-alumina, to the mixture obtained according to (3.2);

(3.4) adding a zeolitic material to the mixture prepared according to (3.2), or according to (3.3). In the case where the process comprises (3.1), (3.2), optionally (3.3), and (3.4), it is preferred that the zeolite material added in (3.4) comprises one or more of iron and copper, more preferably iron.

It is preferred that disposing the second mixture in (4) of the process comprises disposing the second mixture obtained in (3) from the inlet end toward to the outlet end of the substrate over y % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over y % of the substrate axial length, wherein y is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

It is preferred that, prior to calcining in (4) of the process, drying of the second mixture disposed on the substrate having a first coating thereon is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, preferably in the range of from 100 to 120 °C, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

It is preferred that, prior to calcining in (4) of the process, drying of the second mixture disposed on the substrate having a first coating thereon is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, preferably in the range of from 0.75 to 2 hours, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

It is preferred that calcining in (4) of the process is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

It is preferred that calcining in (4) of the process is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, preferably in the range of from 1 to 2 hours, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

The present invention further relates to a process for preparing a NOx adsorber catalyst for the treatment of an exhaust gas, wherein the second coating (ill) comprises, more preferably consists of (ill.1) and (ill.2), comprises

(1 ’) providing a first mixture as described in the foregoing comprising water and a NOx adsorber material comprising

(ii.1) a first platinum group metal component; (ii.2) one or more zeolitic materials;

(2’) disposing the first mixture as described in the foregoing obtained according to (1 ’) on a substrate, comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough, calcining as described in the foregoing, obtaining a substrate having a first coating thereon;

(3’) providing a mixture, preferably as the second mixture as described in the foregoing, comprising water and a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania; wherein (3’) comprises

(3’.1 ) impregnating a source of the second platinum group metal on the non-zeolitic oxidic material and calcining;

(3’.2) preparing a mixture with water and the impregnated non-zeolitic oxidic material obtained according to (3’.1 );

(3’.3) adding a zeolitic material to the mixture prepared according to (3’.2);

(4’) disposing the mixture obtained according to (3’.3) on the substrate having the first coating thereon obtained according to (2’), wherein (4’) comprises disposing the mixture obtained according to (3’.3) on the substrate having a first coating thereon obtained according to (2’) from the inlet end toward the outlet end of the substrate over y ¹ % of the substrate axial length, wherein y ¹ is in the range of from 20 to 80, more preferably in the range of from 40 to 60, more preferably in the range of from 45 to 55, calcining as described in the foregoing, obtaining a substrate having a first coating, preferably according to (ii.b), and an inlet coat thereon;

(5’) providing a mixture comprising water and a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania; wherein (5’) prefer comprises

(5’.1 ) impregnating a source of the second platinum group metal on a non-zeolitic oxidic material and calcining as described in the foregoing;

(5’.2) preparing a mixture with water and the impregnated non-zeolitic oxidic material obtained according to (5’.1 );

(6’) disposing the mixture obtained according to (5’.2) on the substrate having the first coating thereon and the inlet coat thereon obtained according to (4’), wherein (6’) comprises disposing the mixture obtained according to (5’.2) on the substrate having a first coating thereon and an inlet coat obtained according to (4’) from the outlet end toward the inlet end of the substrate over y ² % of the substrate axial length, wherein y ² is in the range of from 20 to 80, more preferably in the range of from 40 to 60, more preferably in the range of from 45 to 55, calcining as described in the foregoing, obtaining a substrate having a first coating, preferably according to (ii.b), and a second coating comprising an inlet coat and an outlet coat thereon.

Preferably y ¹ + y ² = y.

It is preferred that the process consists of (1 ’), (2’), (3’), (4’), (5’) and (6’).

Yet further, the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, preferably a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, obtainable or obtained by a process according to any one of the embodiments disclosed herein.

Yet further, the present invention relates to a method for the treatment of an exhaust gas by NOx adsorption comprising providing an exhaust gas, preferably from an internal combustion engine, more preferably from a diesel engine; contacting the exhaust gas with a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein.

Yet further, the present invention relates to a use of a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein for the treatment of an exhaust gas exiting from an internal combustion engine, more preferably a diesel engine, by NOx adsorption.

Yet further, the present invention relates to a system for the treatment of an exhaust gas, preferably exiting from an internal combustion engine, more preferably a diesel engine, the system comprising a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, the catalyst comprising an inlet end and an outlet end; a selective catalytic reduction catalyst comprising an inlet end and an outlet end; wherein the outlet end of the NOx adsorber catalyst is positioned upstream of the inlet end of the selective catalytic reduction catalyst.

It is preferred that the selective catalytic reduction catalyst comprises an 8-membered ring pore zeolitic material comprising one or more of copper and iron, more preferably copper, wherein more preferably the amount of one or more of copper and iron, calculated as CuO and FezOs, respectively, more preferably of copper, calculated as CuO, is in the range of from 1 to 10 weight-%, more preferably in the range of from 2 to 8 weight-%, based on the weight of the 8- membered ring pore zeolitic material comprising one or more of copper and iron.

It is preferred that the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KF I , ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type CHA.

The present invention is illustrated by the following second set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. The second set of embodiments may be combined with the first set of embodiments above.

!!. A further NOx adsorber catalyst for the treatment of an exhaust gas

Thus, the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, the catalyst comprises

(I) a substrate comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough;

(ii) a coating disposed on the substrate, the coating comprising a NOx adsorber material comprising a platinum group metal component and a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 10:1 to 40:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga.

It is preferred that the platinum group metal component according to (ii) comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, wherein the platinum group metal component more preferably comprises, more preferably is, palladium.

It is preferred that the platinum group metal component according to (ii) is comprised in the 10- membered ring pore zeolitic material, wherein the platinum group metal more preferably is comprised in said zeolitic material in an amount in the range of from 0.25 to 6 weight-%, more preferably in the range of from 0.5 to 4 weight-%, more preferably in the range of from 0.75 to 3 weight-%, more preferably in the range of from 0.9 to 1.5 weight-%, based on the total weight of the platinum group metal and the 10-membered ring pore zeolitic material.

It is preferred that the 10-membered ring pore zeolitic material has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of MFI, FER, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 10-membered ring pore zeolitic material has a framework type MFI. It is preferred that, in the 10-membered ring pore zeolitic material, the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 12:1 to 38:1 , more preferably in the range of from 15:1 to 35:1 , more preferably in the range of from 20:1 to 34:1 , more preferably in the range of from 25:1 to 33:1 .

It is preferred that Y comprises, more preferably is, Si.

It is preferred that X comprises, more preferably is, one or more of Al and B, more preferably Al.

It is preferred that Y is Si and X is Al.

It is preferred that the coating according to (ii) comprises the platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 10 to 150 g/ft ³ , more preferably in the range of from 40 to 100 g/ft ³ , more preferably in the range of from 50 to 80 g/ft ³ , more preferably in the range of from 55 to 70 g/ft ³ .

It is preferred that the catalyst comprises the coating according to (ii) at a loading in the range of from 0.5 to 8 g/in ³ , more preferably in the range of from 1 to 5 g/in ³ , more preferably in the range of from 1.5 to 4.5 g/in ³ , more preferably in the range of from 2 to 4 g/in ³ .

It is preferred that the NOx adsorber material consists of the platinum group metal component and the 10-membered ring pore zeolitic material.

It is preferred that from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the coating according to (ii) consist of the platinum group metal component, more preferably palladium, and the 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type MFI, wherein more preferably the coating according to (ii) consist of the platinum group metal component, more preferably palladium, and the 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type MFI.

It is preferred that the catalyst consists of a substrate according to (I) and a coating according to (ii).

Further, the present invention relates to a process for preparing a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, the process comprising

(1) providing a mixture comprising water and a NOx adsorber material comprising a first platinum group metal and a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YO2:X2Os, is in the range of from 10:1 to 40:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga;

(2) disposing the mixture obtained according to (1) on a substrate, comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough, obtaining a mixture-treated substrate;

(3) calcining the mixture- treated substrate obtained according to (2), obtaining a substrate having a coating thereon.

It is preferred that (1) of the process comprises admixing, preferably impregnating, the 10-membered ring pore zeolitic material with a source of the platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

In the case where (1) of the process comprises admixing, preferably impregnating, the 10-membered ring pore zeolitic material with a source of the platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water, it is preferred that calcining is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

Further in the case where (1) of the process comprises admixing, preferably impregnating, the 10-membered ring pore zeolitic material with a source of the platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water, it is preferred that calcining is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that disposing the mixture in (2) of the process comprises disposing the mixture obtained in (1) from the inlet end toward to the outlet end of the substrate over x % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, more preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100. It is preferred that, prior to calcining in (3) of the process, drying of the mixture-treated substrate is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, more preferably in the range of from 100 to 120 °C, the gas atmosphere more preferably being air.

It is preferred that, prior to calcining in (3) of the process, drying of the mixture-treated substrate is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, more preferably in the range of from 0.75 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that calcining in (3) of the process is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that calcining in (3) of the process is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

It is preferred that the process consists of (1 ), (2) and (3).

Yet further, the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, preferably a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, obtainable or obtained by a process according to any one of the embodiments disclosed herein.

Yet further, the present invention relates to a method for the treatment of an exhaust gas by NOx adsorption comprising providing an exhaust gas, preferably from an internal combustion engine, more preferably from a diesel engine; contacting the exhaust gas with a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein.

Yet further, the present invention relates to a use of a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein for the treatment of an exhaust gas exiting from an internal combustion engine, more preferably a diesel engine, by NOx adsorption.

Yet further, the present invention relates to a system for the treatment of an exhaust gas, preferably exiting from an internal combustion engine, more preferably a diesel engine, the system comprising a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of the embodiments disclosed herein, the catalyst comprising an inlet end and an outlet end; a selective catalytic reduction catalyst comprising an inlet end and an outlet end; wherein the outlet end of the NOx adsorber catalyst is positioned upstream of the inlet end of the selective catalytic reduction catalyst.

It is preferred that the selective catalytic reduction catalyst of the system comprises an 8-mem- bered ring pore zeolitic material comprising one or more of copper and iron, preferably copper, wherein preferably the amount of one or more of copper and iron, calculated as CuO and FezOs, respectively, more preferably of copper, calculated as CuO, is in the range of from 1 to 10 weight-%, preferably in the range of from 2 to 8 weight-%, based on the weight of the 8-mem- bered ring pore zeolitic material comprising one or more of copper and iron.

It is preferred that the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst of the system has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KFI, ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type CHA.

III. Embodiments

The present invention is illustrated by the following first set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. The first set of embodiments may be combined with the second set of embodiments below. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as “ A further preferred embodiment (4) concretizing any one of embodiments (1 ) to (3) ”, every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to “ A further preferred embodiment (4) concretizing any one of embodiments (1 ), (2) and (3) ”. Further, it is explicitly noted that the following set of embodiments is not the set of claims determining the extent of protection, but represents a suitably structured part of the description directed to general and preferred aspects of the present invention.

A NOx adsorber catalyst with a DOC function for the treatment of an exhaust gas

According to an embodiment (1), the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, the catalyst comprises

(I) a substrate comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough;

(ii) a first coating disposed on the substrate, the first coating comprising a NOx adsorber material comprising

(11.1) a first platinum group metal component;

(11.2) one or more zeolitic materials; (iii) a second coating disposed on the first coating, the second coating comprising a diesel oxidation material comprising a second platinum group metal component and a non-zeo- litic oxidic material comprising one or more of alumina, silica, zirconia and titania.

A preferred embodiment (2) concretizing embodiment (1 ) relates to said catalyst, wherein the first platinum group metal component according to (ii.1) comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, wherein the first platinum group metal component more preferably comprises, more preferably is, palladium.

A further preferred embodiment (3) concretizing embodiment (1 ) or (2) relates to said catalyst, wherein from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the NOx adsorber material comprised in the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the one or more zeolitic materials according to (ii.2).

A further preferred embodiment (4) concretizing any one of embodiments (1 ) to (3) relates to said catalyst, wherein from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.9 to 100 weight-% of the first coating according to (ii) consist of the NOx adsorber material.

A further preferred embodiment (5) concretizing any one of embodiments (1 ) to (4) relates to said catalyst, wherein the NOx adsorber material comprised in the first coating according to (ii) comprises from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ce, calculated as CeOz, wherein the NOx adsorber material comprised in the first coating according to (ii) is preferably essentially free of Ce, wherein the first coating according to (ii) more preferably is free of Ce.

A further preferred embodiment (6) concretizing any one of embodiments (1 ) to (5) relates to said catalyst, wherein the first coating according to (ii) comprises from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.001 weight-%, of Ce, calculated as CeC>2, wherein the first coating according to (ii) is preferably essentially free of Ce, wherein the first coating according to (ii) more preferably is free of Ce.

A further preferred embodiment (7) concretizing any one of embodiments (1 ) to (6) relates to said catalyst, wherein the first coating according to (ii) comprises (ii.2a) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material.

A further preferred embodiment (8) concretizing embodiment (7) relates to said catalyst, wherein the first platinum group metal component according to (ii.1) is comprised in both the 8- membered ring pore zeolitic material and the 10-membered ring pore zeolitic material according to (ii.2a), wherein the first platinum group metal according to (ii.1 ) more preferably is comprised in said zeolitic materials in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1 ) and the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material according to (ii.2a).

A further preferred embodiment (9) concretizing embodiment (7) or (8) relates to said catalyst, wherein the 8-membered ring pore zeolitic material according to (ii .2a) has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KFI, ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material according to (ii.2a) has a framework type CHA.

A further preferred embodiment (10) concretizing any one of embodiments (7) to (9) relates to said catalyst, wherein the framework structure of the 8-membered ring pore zeolitic material according to (ii.2a) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 40:1 , more preferably in the range of from 5:1 to 30:1 , more preferably in the range of from 8:1 to 20:1 , more preferably in the range of from 10:1 to 18:1 , more preferably in the range of from 12:1 to 16:1.

A further preferred embodiment (11) concretizing embodiment (10) relates to said catalyst, wherein Y comprises, more preferably is, Si.

A further preferred embodiment (12) concretizing embodiment (10) or (11) relates to said catalyst, wherein X comprises, more preferably is, one or more of Al and B, more preferably Al.

A further preferred embodiment (13) concretizing any one of embodiments (10) to (12) relates to said catalyst, wherein Y is Si and X is Al.

A further preferred embodiment (14) concretizing any one of embodiments (10) to (13) relates to said catalyst, wherein the 10-membered ring pore zeolitic material according to (ii.2a) has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of FER, TON, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER and TON, wherein more preferably the 10-membered ring pore zeolitic material according to (ii.2a) has a framework type FER. A further preferred embodiment (15) concretizing any one of embodiments (7) to (14) relates to said catalyst, wherein the framework structure of the 10-membered ring pore zeolitic material according to (ii.2a) comprises, preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 2:1 to 45:1 , preferably in the range of from 10:1 to 40:1 , more preferably in the range of from 12:1 to 30:1 , more preferably in the range of from 15:1 to 28:1 , more preferably in the range of from 18:1 to 25: 1 .

A further preferred embodiment (16) concretizing embodiment (15) relates to said catalyst, wherein Y comprises, more preferably is, Si.

A further preferred embodiment (17) concretizing embodiment (15) or (16) relates to said catalyst, wherein X comprises, more preferably is, one or more of Al and B, more preferably Al.

A further preferred embodiment (18) concretizing any one of embodiments (15) to (17) relates to said catalyst, wherein Y is Si and X is Al.

A further preferred embodiment (19) concretizing any one of embodiments (7) to (18) relates to said catalyst, wherein the weight ratio of the 10-membered ring pore zeolitic material according to (ii.2a) to the 8-membered ring pore zeolitic material according to (ii.2a) is in the range of from 10:1 to 1 :10, more preferably in the range of from 5:1 to 1 :5, more preferably in the range of from 3:1 to 1 :3, more preferably in the range of from 2:1 to 1 :2.

A further preferred embodiment (20) concretizing any one of embodiments (7) to (19) relates to said catalyst, wherein the first coating comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 175 g/ft ³ , more preferably in the range of from 40 to 150 g/ft ³ , more preferably in the range of from 70 to 140 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ . It might be alternatively be conceivable that the first coating preferably comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, preferably as elemental Pd, in the range of from 100 to 140 g/ft ³ .

A further preferred embodiment (21) concretizing any one of embodiments (7) to (20) relates to said catalyst, wherein the first coating comprises the zeolitic materials according to (ii.2a) in an amount in the range of from 80 to 99.5 weight-%, more preferably in the range of from 85 to 99 weight-%, more preferably in the range of from 90 to 99 weight-%, more preferably in the range of from 95 to 98.5 weight-%, based on the weight of the first coating.

A further preferred embodiment (22) concretizing any one of embodiments (7) to (22) relates to said catalyst, wherein from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the 8-membered ring pore zeolitic material according to (ii.2a) and the 10-membered ring pore zeolitic material according to (ii.2a), wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the 8-membered ring pore zeolitic material according to (ii.2a) and the 10-membered ring pore zeolitic material according to (ii.2a).

A further preferred embodiment (24) concretizing any one of embodiments (7) to (23) relates to said catalyst, wherein the NOx adsorber material consists of the first platinum group metal component according to (ii.1), the 8-membered ring pore zeolitic material according to (ii.2a) and the 10-membered ring pore zeolitic material according to (ii.2a).

A further preferred embodiment (25) concretizing any one of embodiments (1) to (6) relates to said catalyst, wherein the first coating according to (ii) comprises (ii.2b) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga.

A further preferred embodiment (26) concretizing embodiment (25) relates to said catalyst, wherein Y comprises, more preferably is, Si.

A further preferred embodiment (27) concretizing embodiment (25) or (26) relates to said catalyst, wherein X comprises, more preferably is, one or more of Al and B, more preferably Al.

A further preferred embodiment (28) concretizing any one of embodiments (25) to (27) relates to said catalyst, wherein Y is Si and X is Al.

A further preferred embodiment (29) concretizing any one of embodiments (25) to (28) relates to said catalyst, wherein the first platinum group metal component according to (ii.1) is comprised in the 10-membered ring pore zeolitic material according to (ii.2b), wherein the first platinum group metal according to (ii.1) more preferably is comprised in said zeolitic material in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1) and the 10-membered ring pore zeolitic material according to (ii.2b).

A further preferred embodiment (30) concretizing any one of embodiments (25) to (29) relates to said catalyst, wherein the 10-membered ring pore zeolitic material according to (ii.2b) has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER, MFI, TON, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of FER and MFI, wherein more preferably the 10-membered ring pore zeolitic material according to (ii.2b) has a framework type FER.

A further preferred embodiment (31) concretizing any one of embodiments (25) to (30) relates to said catalyst, wherein, in the 10-membered ring pore zeolitic material according to (ii.2b), the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 35:1 to 150:1 , more preferably in the range of from 40:1 to 100:1 , preferably in the range of from 45:1 to 80:1 , more preferably in the range of from 48:1 to 70:1 , more preferably in the range of from 50:1 to 65:1.

A further preferred embodiment (32) concretizing any one of embodiments (25) to (31) relates to said catalyst, wherein the first coating comprises the first platinum group metal, preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 40 to 120 g/ft ³ , more preferably in the range of from 60 to 100 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

A further preferred embodiment (33) concretizing any one of embodiments (25) to (32) relates to said catalyst, wherein the first coating comprises the 10-membered ring pore zeolitic material according to (ii.2b) in an amount in the range of from 80 to 99.75 weight-%, more preferably in the range of from 85 to 99.5 weight-%, more preferably in the range of from 90 to 99.25 weight- %, more preferably in the range of from 95 to 99 weight-%, based on the weight of the first coating.

A further preferred embodiment (34) concretizing any one of embodiments (25) to (34) relates to said catalyst, wherein from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1) and the 10-membered ring pore zeolitic material according to (ii .2b), wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1 ) and the 10-membered ring pore zeolitic material according to (ii.2b).

A further preferred embodiment (36) concretizing any one of embodiments (25) to (35) relates to said catalyst, wherein the NOx adsorber material consists of the first platinum group metal component according to (ii.1 ) and the 10-membered ring pore zeolitic material according to (ii.2b).

A further preferred embodiment (37) concretizing any one of embodiments (1 ) to (6) relates to said catalyst, wherein the first coating according to (ii) comprises (ii.2c) a zeolitic material having a framework type LEV.

A further preferred embodiment (38) concretizing embodiment (37) relates to said catalyst, wherein the first platinum group metal component according to (ii.1) is comprised in the zeolitic material having a framework type LEV according to (ii.2c), wherein the first platinum group metal according to (ii.1) more preferably is comprised in said zeolitic material in an amount in the range of from 0.5 to 10 weight-%, more preferably in the range of from 0.75 to 6 weight-%, more preferably in the range of from 1 to 4 weight-%, more preferably in the range of from 1 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the total weight of the first platinum group metal according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii.2c).

A further preferred embodiment (39) concretizing embodiment (37) or (38) relates to said catalyst, wherein the framework structure of the zeolitic material having a framework type LEV according to (ii.2c) comprises, more preferably consists of, a tetravalent element Y, a trivalent element X and oxygen, wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and X comprises one or more of Al, B, In and Ga, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 10:1 to 80:1 , more preferably in the range of from 15:1 to 70:1 , more preferably in the range of from 20:1 to 60:1 , more preferably in the range of from 22:1 to 50:1 , more preferably in the range of from 25:1 to 40:1 , more preferably in the range of from 28:1 to 39:1 , more preferably in the range of from 29:1 to 33:1.

A further preferred embodiment (40) concretizing embodiment (39) relates to said catalyst, wherein Y comprises, more preferably is, Si.

A further preferred embodiment (41) concretizing embodiment (39) or (40) relates to said catalyst, wherein X comprises, more preferably is, one or more of Al and B, more preferably AL

A further preferred embodiment (42) concretizing any one of embodiments (39) to (41) relates to said catalyst, wherein Y is Si and X is Al.

A further preferred embodiment (43) concretizing any one of embodiments (39) to (42) relates to said catalyst, wherein the first coating comprises the first platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 40 to 120 g/ft ³ , more preferably in the range of from 60 to 100 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

A further preferred embodiment (44) concretizing any one of embodiments (39) to (43) relates to said catalyst, wherein the first coating comprises the zeolitic material having a framework type LEV according to (ii.2c) in an amount in the range of from 80 to 99.75 weight-%, more preferably in the range of from 85 to 99.5 weight-%, more preferably in the range of from 90 to 99.25 weight-%, more preferably in the range of from 95 to 99 weight-%, based on the weight of the first coating.

A further preferred embodiment (45) concretizing any one of embodiments (39) to (45) relates to said catalyst, wherein from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the first coating according to (ii) consist of the first platinum group metal component according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii.2c) , wherein more preferably the first coating according to (ii) consist of the first platinum group metal component according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii .2c).

A further preferred embodiment (47) concretizing any one of embodiments (39) to (46) relates to said catalyst, wherein the NOx adsorber material consists of the first platinum group metal component according to (ii.1 ) and the zeolitic material having a framework type LEV according to (ii.2c).

A further preferred embodiment (48) concretizing any one of embodiments (1) to (47) relates to said catalyst, wherein the second platinum group metal component of the second coating according to (ill) comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum.

A further preferred embodiment (49) concretizing embodiment (48) relates to said catalyst, wherein the second platinum group metal component comprises, preferably is, platinum.

A further preferred embodiment (50) concretizing embodiment (48) relates to said catalyst, wherein the second platinum group metal component comprises, more preferably is, platinum and palladium, wherein the weight ratio of Pt to Pd, calculated as elemental Pt and Pd, respectively, more preferably is in the range of from 2:1 to 20:1 , more preferably in the range of from 3:1 to 15:1 , more preferably in the range of from 5: to 12:1 , more preferably in the range of from 7:1 to 11 :1.

A further preferred embodiment (51) concretizing any one of embodiments (1) to (50) relates to said catalyst, wherein the second coating according to (ill) comprises the second platinum group metal component, more preferably platinum or platinum and palladium, at a loading, calculated as elemental platinum group metal(s), more preferably as elemental Pd or as elemental Pt and Pd, respectively, in the range of from 15 to 200 g/ft ³ , more preferably in the range of from 20 to 150 g/ft ³ , more preferably in the range of from 30 to 100 g/ft ³ , more preferably in the range of from 40 to 80 g/ft ³ , more preferably in the range of from 50 to 70 g/ft ³ .

A further preferred embodiment (52) concretizing any one of embodiments (1) to (51 ) relates to said catalyst, wherein the non-zeolitic oxidic material of the second coating according to (ill) comprises one or more of alumina, silica, zirconia, silica-alumina, silica-zirconia, and aluminazirconia, more preferably one or more of alumina, silica and zirconia, preferably one or more of alumina and silica. A further preferred embodiment (53) concretizing embodiment (52) relates to said catalyst, wherein the non-zeolitic oxidic material of the second coating according to (ill) comprises alumina, more preferably gamma-alumina, and more preferably further comprises manganese, wherein the non-zeolitic oxidic material of the second coating according to (ill) more preferably comprises alumina and manganese, wherein the non-zeolitic oxidic material more preferably comprises the alumina in an amount in the range of from 80 to 99 weight-%, more preferably in the range of from 85 to 98 weight-%, more preferably in the range of from 90 to 97 weight-%, based on the weight of the non-zeolitic oxidic material.

A further preferred embodiment (54) concretizing embodiment (52) or (53) relates to said catalyst, wherein the non-zeolitic oxidic material of the second coating according to (ill) exhibits a BET specific surface area of greater than 75 m ² /g, more preferably greater than 100 m ² /g, more preferably determined according to Reference Example 1 .2.

A further preferred embodiment (55) concretizing any one of embodiments (52) to (54) relates to said catalyst, wherein the non-zeolitic oxidic material of the second coating according to (ill) exhibits a pore volume of greater than 0.04 cm ³ /g, more preferably greater than 0.06 cm ³ /g, more preferably determined according to Reference Example 1 .4.

A further preferred embodiment (56) concretizing any one of embodiments (1) to (55) relates to said catalyst, wherein the second coating according to (ill) further comprises a second non-zeolitic oxidic material, wherein the second non-zeolitic material more preferably comprises one or more of alumina, silica-alumina, titania-alumina, silica and titania, more preferably one or more of alumina and silica-alumina, more preferably silica-alumina.

A further preferred embodiment (57) concretizing embodiment (56) relates to said catalyst, wherein the second non-zeolitic oxidic material comprises the alumina in an amount in the range of from 80 to 99 weight-%, more preferably in the range of from 85 to 98 weight-%, more preferably in the range of from 90 to 97 weight-%, based on the weight of the second non-zeolitic oxidic material.

A further preferred embodiment (58) concretizing embodiment (56) or (57) relates to said catalyst, wherein the second non-zeolitic oxidic material of the second coating according to (ill) exhibits a BET specific surface area of greater than 75 m ² /g, more preferably greater than 100 m ² /g, more preferably determined according to Reference Example 1 .2.

A further preferred embodiment (59) concretizing any one of embodiments (56) to (58) relates to said catalyst, wherein the second non-zeolitic oxidic material of the second coating according to (ill) exhibits a pore volume of greater than 0.04 cm ³ /g, more preferably greater than 0.06 cm ³ /g, more preferably determined according to Reference Example 1.4.

A further preferred embodiment (60) concretizing any one of embodiments (1) to (59) relates to said catalyst, wherein the second coating according to (ill) further comprises a zeolitic material, more preferably a 12-membered ring pore zeolitic material, wherein the 12-membered ring pore zeolitic material has a framework type selected from the group consisting of BEA, FAU, USY, GME, MOR, OFF, a mixture of two or more thereof and a mixed type of two or more thereof, preferably selected from the group consisting of BEA, USY, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 12-membered ring pore zeolitic material has a framework type BEA.

A further preferred embodiment (61) concretizing embodiment (60) relates to said catalyst, wherein the framework structure of the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises, more preferably consists of, Si, Al and oxygen, wherein the molar ratio of Si:AI, calculated as SiO2:Al2O3, is in the range of from 2:1 to 60:1 , more preferably in the range of from 10:1 to 50:1 , more preferably in the range of from 15:1 to 40:1 , more preferably in the range of from 20:1 to 30:1 , more preferably in the range of from 22:1 to 28:1 .

A further preferred embodiment (62) concretizing embodiment (60) or (61) relates to said catalyst, wherein the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises iron, wherein the amount of iron in the zeolitic material, calculated as Fe2Os, more preferably is in the range of from 0.1 to 5 weight-%, more preferably in the range of from 0.5 to 3 weight-%, more preferably in the range of from 1 to 2 weight-%, based on the weight of the zeolitic material comprising iron.

A further preferred embodiment (63) concretizing embodiment (60) or (61) relates to said catalyst, wherein the zeolitic material, more preferably the 12-membered ring pore zeolitic material, more preferably the zeolitic material having a framework type BEA, comprises at most 0.001 weight-%, more preferably from 0 to 0.0001 weight-%, more preferably from 0 to 0.00001 weight-%, of iron, calculated as Fe2Os, more preferably of iron and copper, calculated as Fe2Os and CuO, respectively.

A further preferred embodiment (64) concretizing any one of embodiments (60) to (63) relates to said catalyst, wherein the weight ratio of the non-zeolitic material of the second coating according to (ill) to the zeolitic material of the second coating according to (ill) is in the range of from 1 :1 to 10:1 , more preferably in the range of from 2:1 to 8:1 , more preferably in the range of from 2.5:1 to 5:1.

A further preferred embodiment (65) concretizing any one of embodiments (1) to (64) relates to said catalyst, wherein the catalyst comprises the second coating according to (ill) at a loading in the range of from 0.5 to 5 g/in ³ , preferably in the range of from 0.75 to 4 g/in ³ , more preferably in the range of from 1 to 3 g/in ³ , more preferably in the range of from 1.25 to 2.5 g/in ³ . A further preferred embodiment (66) concretizing any one of embodiments (1) to (65) relates to said catalyst, wherein from 98 to 100 weight-%, preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64, wherein more preferably the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64; or wherein from 98 to 100 weight-%, preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material, a second non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64, wherein more preferably the second coating according to (ill) consist of the second platinum group metal component, the non-zeolitic oxidic material, a second non-zeolitic oxidic material and preferably a zeolitic material as defined in any one of embodiments 60 to 64.

A further preferred embodiment (67) concretizing any one of embodiments (1) to (66) relates to said catalyst, wherein the substrate according to (I) is a flow-through substrate or a wall-flow filter substrate, preferably a flow-through substrate, wherein the flow-through substrate more preferably is one or more of a cordierite flow-through substrate or a metallic flow-through substrate, more preferably a cordierite flow-through substrate.

A further preferred embodiment (68) concretizing any one of embodiments (1) to (67) relates to said catalyst, wherein the substrate is a monolith, preferably a honeycomb monolith.

A further preferred embodiment (69) concretizing any one of embodiments (1) to (68) relates to said catalyst, wherein the first coating according to (ii) is disposed on the surface of the internal walls of the substrate.

A further preferred embodiment (70) concretizing any one of embodiments (1) to (69) relates to said catalyst, wherein the first coating according to (ii) is disposed on the surface of the internal walls of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

A further preferred embodiment (71) concretizing any one of embodiments (1) to (69) relates to said catalyst, wherein the second coating according to (ill) is disposed on the first coating over y % of the substrate axial length, wherein y is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100, wherein more preferably the first coating according to (ii) is disposed on the surface of the internal walls of the substrate over x % of the substrate axial length according to embodiment 70 and wherein x = y. A further preferred embodiment (72) concretizing any one of embodiments (1) to (71 ) relates to said catalyst, wherein the catalyst consists of the substrate according to (I), the first coating according to (ii) and the second coating according to (ill).

An embodiment (73) of the present invention relates to a process for preparing a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ) to (72), the process comprising

(1) providing a first mixture comprising water and a NOx adsorber material comprising

(11.1 ) a first platinum group metal component;

(11.2) one or more zeolitic materials;

(2) disposing the first mixture obtained according to (1) on a substrate, comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough, calcining, obtaining a substrate having a first coating thereon;

(3) providing a second mixture comprising water and a diesel oxidation material comprising a second platinum group metal component and a non-zeolitic oxidic material comprising one or more of alumina, silica, zirconia and titania;

(4) disposing the second mixture obtained according to (3) on the substrate having a first coating thereon obtained according to (2), calcining, obtaining a substrate having a first coating and a second coating thereon.

A further preferred embodiment (74) concretizing embodiment (73) relates to said process, wherein providing a first mixture comprising water and a NOx adsorber material according to (1) comprises

(a) a first platinum group metal and

(b.1) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material, or

(b.2) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YOz^Os, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, or

(b.3) a zeolitic material having a framework type LEV.

A further preferred embodiment (75) concretizing embodiment (73) or (74) relates to said process, wherein (1) comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.1) an 8-membered ring pore zeolitic material and a 10-membered ring pore zeolitic material; wherein providing the first mixture comprises admixing the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material, more preferably the H-form of the 8-membered ring pore zeolitic material and the ammonium form of the 10-membered ring pore zeolitic material, more preferably admixing H-CHA and NH ₄ -FER; admixing, more preferably impregnating, the mixture of the 8-membered ring pore zeolitic material and the 10-membered ring pore zeolitic material with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

A further preferred embodiment (76) concretizing embodiment (73) or (74) relates to said process, wherein (1) comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.2) a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 30:1 to 200:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga, wherein providing the first mixture comprises admixing, more preferably impregnating, the 10-membered ring pore zeolitic material, more preferably the ammonium form of the 10-membered ring pore zeolitic material, with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

A further preferred embodiment (77) concretizing embodiment (73) or (74) relates to said process, wherein (1) comprises providing a first mixture comprising water and a NOx adsorber material comprising

(a) a first platinum group metal and

(b.3) a zeolitic material having a framework type LEV, wherein providing the first mixture comprises admixing, more preferably impregnating, the zeolitic material having a framework type LEV, more preferably the ammonium form of the zeolitic material having a framework type LEV, with a source of the first platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution, and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

A further preferred embodiment (78) concretizing any one of embodiments (73) to (77) relates to said process, wherein calcining is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air. A further preferred embodiment (79) concretizing any one of embodiments (73) to (78) relates to said process, wherein calcining is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (80) concretizing any one of embodiments (73) to (79) relates to said process, wherein disposing the first mixture in (2) comprises disposing the first mixture obtained in (1) from the inlet end toward to the outlet end of the substrate over x % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, more preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

A further preferred embodiment (81) concretizing any one of embodiments (73) to (80) relates to said process, wherein, prior to calcining in (2), drying of the first mixture disposed on the substrate is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, more preferably in the range of from 100 to 120 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (82) concretizing any one of embodiments (73) to (81) relates to said process, wherein, prior to calcining in (2), drying of the first mixture disposed on the substrate is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, more preferably in the range of from 0.75 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (83) concretizing any one of embodiments (73) to (82) relates to said process, wherein calcining in (2) is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (84) concretizing any one of embodiments (73) to (83) relates to said process, wherein calcining in (2) is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (85) concretizing any one of embodiments (73) to (84) relates to said process, wherein (3) comprises

(3.1) impregnating a source of the second platinum group metal on the non-zeolitic oxidic material and calcining;

(3.2) preparing a mixture with water and the impregnated non-zeolitic oxidic material obtained according to (3.1); (3.3) optionally adding a second non-zeolitic oxidic material, more preferably selected from the group consisting of alumina, silica-alumina, titania-alumina and manganese-alumina, more preferably silica-alumina, to the mixture obtained according to (3.2);

(3.4) adding a zeolitic material to the mixture prepared according to (3.2), or according to (3.3).

A further preferred embodiment (86) concretizing embodiment (85) relates to said process, wherein the zeolite material added in (3.4) comprises one or more of iron and copper, more preferably iron.

A further preferred embodiment (87) concretizing any one of embodiments (73) to (86) relates to said process, wherein disposing the second mixture in (4) comprises disposing the second mixture obtained in (3) from the inlet end toward to the outlet end of the substrate over y % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over y % of the substrate axial length, wherein y is in the range of from 80 to 100, preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100.

A further preferred embodiment (88) concretizing any one of embodiments (73) to (87) relates to said process, wherein, prior to calcining in (4), drying of the second mixture disposed on the substrate having a first coating thereon is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, preferably in the range of from 100 to 120 °C, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

A further preferred embodiment (89) concretizing any one of embodiments (73) to (88) relates to said process, wherein, prior to calcining in (4), drying of the second mixture disposed on the substrate having a first coating thereon is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, preferably in the range of from 0.75 to 2 hours, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

A further preferred embodiment (90) concretizing any one of embodiments (73) to (89) relates to said process, wherein calcining in (4) is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

A further preferred embodiment (91) concretizing any one of embodiments (73) to (90) relates to said process, wherein calcining in (4) is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, preferably in the range of from 1 to 2 hours, the gas atmosphere preferably comprising one or more of oxygen and nitrogen, preferably air.

A further preferred embodiment (92) concretizing any one of embodiments (73) to (91) relates to said process, wherein the process consists of (1), (2), (3) and (4). An embodiment (93) of the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, preferably a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1) to (72), obtainable or obtained by a process according to any one of embodiments (73) to (92).

An embodiment (94) of the present invention relates to a method for the treatment of an exhaust gas by NOx adsorption comprising providing an exhaust gas, preferably from an internal combustion engine, more preferably from a diesel engine; contacting the exhaust gas with a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1) to (72) and (93).

An embodiment (95) of the present invention relates to a use of a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ) to (72) and (93) for the treatment of an exhaust gas exiting from an internal combustion engine, more preferably a diesel engine, by NOx adsorption.

An embodiment (96) of the present invention relates to a system for the treatment of an exhaust gas, preferably exiting from an internal combustion engine, more preferably a diesel engine, the system comprising a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1) to (72) and (93), the catalyst comprising an inlet end and an outlet end; a selective catalytic reduction catalyst comprising an inlet end and an outlet end; wherein the outlet end of the NOx adsorber catalyst is positioned upstream of the inlet end of the selective catalytic reduction catalyst.

A preferred embodiment (97) concretizing embodiment (96) relates to said system, wherein the selective catalytic reduction catalyst comprises an 8-membered ring pore zeolitic material comprising one or more of copper and iron, more preferably copper, wherein more preferably the amount of one or more of copper and iron, calculated as CuO and FezOs, respectively, more preferably of copper, calculated as CuO, is in the range of from 1 to 10 weight-%, more preferably in the range of from 2 to 8 weight-%, based on the weight of the 8-membered ring pore zeolitic material comprising one or more of copper and iron.

A preferred embodiment (97) concretizing embodiment (96) or (97) relates to said system, wherein the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KFI, ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type CHA. The present invention is illustrated by the following second set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. The second set of embodiments may be combined with the first set of embodiments above.

A further NOx adsorber catalyst for the treatment of an exhaust gas

An embodiment (1 ’) of the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, the catalyst comprises

(I) a substrate comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough;

(ii) a coating disposed on the substrate, the coating comprising a NOx adsorber material comprising a platinum group metal component and a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YO2:X2OS, is in the range of from 10:1 to 40:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga.

A preferred embodiment (2’) concretizing embodiment (T) relates to said catalyst, wherein the platinum group metal component according to (ii) comprises one or more of palladium, platinum, rhodium, iridium, osmium and ruthenium, more preferably one or more of palladium, platinum and rhodium, more preferably one or more of palladium and platinum, wherein the platinum group metal component more preferably comprises, more preferably is, palladium.

A preferred embodiment (3’) concretizing embodiment (T) or (2’) relates to said catalyst, wherein the platinum group metal component according to (ii) is comprised in the 10-membered ring pore zeolitic material, wherein the platinum group metal more preferably is comprised in said zeolitic material in an amount in the range of from 0.25 to 6 weight-%, more preferably in the range of from 0.5 to 4 weight-%, more preferably in the range of from 0.75 to 3 weight-%, more preferably in the range of from 0.9 to 1 .5 weight-%, based on the total weight of the platinum group metal and the 10-membered ring pore zeolitic material.

A further preferred embodiment (4’) concretizing any one of embodiments (T) to (3’) relates to said catalyst, wherein the 10-membered ring pore zeolitic material has a framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of MFI, FER, MFI, MWW, AEL, HEU, AFO, a mixture of two or more thereof and a mixed type of two or more thereof, wherein more preferably the 10-membered ring pore zeolitic material has a framework type MFI.

A further preferred embodiment (5’) concretizing any one of embodiments (T) to (4’) relates to said catalyst, wherein, in the 10-membered ring pore zeolitic material, the molar ratio of Y:X, calculated as YO2:X2Os, is in the range of from 12:1 to 38:1 , more preferably in the range of from 15:1 to 35:1 , more preferably in the range of from 20:1 to 34:1 , more preferably in the range of from 25:1 to 33:1 .

A further preferred embodiment (6’) concretizing any one of embodiments (T) to (5’) relates to said catalyst, wherein Y comprises, more preferably is, Si.

A further preferred embodiment (7’) concretizing any one of embodiments (T) to (6’) relates to said catalyst, wherein X comprises, more preferably is, one or more of Al and B, more preferably Al.

A further preferred embodiment (8’) concretizing any one of embodiments (T) to (7’) relates to said catalyst, wherein Y is Si and X is Al.

A further preferred embodiment (9’) concretizing any one of embodiments (T) to (8’) relates to said catalyst, wherein the coating according to (ii) comprises the platinum group metal, more preferably palladium, at a loading, calculated as elemental platinum group metal, more preferably as elemental Pd, in the range of from 10 to 150 g/ft ³ , more preferably in the range of from 40 to 100 g/ft ³ , more preferably in the range of from 50 to 80 g/ft ³ , more preferably in the range of from 55 to 70 g/ft ³ .

A further preferred embodiment (10’) concretizing any one of embodiments (1 ’) to (9’) relates to said catalyst, wherein the catalyst comprises the coating according to (ii) at a loading in the range of from 0.5 to 8 g/in ³ , more preferably in the range of from 1 to 5 g/in ³ , more preferably in the range of from 1.5 to 4.5 g/in ³ , more preferably in the range of from 2 to 4 g/in ³ .

A further preferred embodiment (1 T) concretizing any one of embodiments (T) to (10’) relates to said catalyst, wherein the NOx adsorber material consists of the platinum group metal component and the 10-membered ring pore zeolitic material.

A further preferred embodiment (12’) concretizing any one of embodiments (1 ’) to (1 T) relates to said catalyst, wherein from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the coating according to (ii) consist of the platinum group metal component, more preferably palladium, and the 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type MFI, wherein more preferably the coating according to (ii) consist of the platinum group metal component, more preferably palladium, and the 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type MFI.

A further preferred embodiment (13’) concretizing any one of embodiments (1 ’) to (12’) relates to said catalyst, wherein the catalyst consists of a substrate according to (I) and a coating according to (ii). An embodiment (14’) of the present invention relates to a process for preparing a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ’) to (13’), the process comprising

(1) providing a mixture comprising water and a NOx adsorber material comprising a first platinum group metal and a 10-membered ring pore zeolitic material, wherein the framework structure of the zeolitic material comprises a tetravalent element Y, a trivalent element X and oxygen, wherein the molar ratio of Y:X, calculated as YC^XzOs, is in the range of from 10:1 to 40:1 , wherein Y comprises one or more of Si, Sn, Ti, Zr and Ge and wherein X comprises one or more of Al, B, In and Ga;

(2) disposing the mixture obtained according to (1) on a substrate, comprising an inlet end, an outlet end, a substrate axial length extending from the inlet end to the outlet end and a plurality of passages defined by internal walls of the substrate extending therethrough, obtaining a mixture-treated substrate;

(3) calcining the mixture- treated substrate obtained according to (2), obtaining a substrate having a coating thereon.

A preferred embodiment (15’) concretizing embodiment (14’) relates to said process, wherein (1) comprises admixing, preferably impregnating, the 10-membered ring pore zeolitic material with a source of the platinum group metal, more preferably a source of palladium, more preferably a palladium nitrate solution and calcining, obtaining the NOx adsorber material; dispersing the obtained NOx adsorber material in water.

A further preferred embodiment (16’) concretizing embodiment (15’) relates to said process, wherein calcining is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (17’) concretizing embodiment (15’) or (16’) relates to said process, wherein calcining is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (18’) concretizing any one of embodiments (14’) or (17’) relates to said process, wherein disposing the mixture in (2) comprises disposing the mixture obtained in (1 ) from the inlet end toward to the outlet end of the substrate over x % of the substrate axial length, or from the outlet end toward to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 80 to 100, more preferably in the range of from 90 to 100, more preferably in the range of from 95 to 100, more preferably in the range of from 98 to 100. A further preferred embodiment (19’) concretizing any one of embodiments (14’) or (18’) relates to said process, wherein, prior to calcining in (3), drying of the mixture-treated substrate is performed in a gas atmosphere having a temperature in the range of from 90 to 150 °C, more preferably in the range of from 100 to 120 °C, the gas atmosphere more preferably being air.

A further preferred embodiment (20’) concretizing any one of embodiments (14’) or (19’) relates to said process, wherein prior to calcining in (3), drying of the mixture-treated substrate is performed in a gas atmosphere for a duration in the range of from 0.5 to 4 hours, more preferably in the range of from 0.75 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (21 ’) concretizing any one of embodiments (14’) or (20’) relates to said process, wherein calcining in (3) is performed in a gas atmosphere having a temperature in the range of from 400 to 800 °C, more preferably in the range of from 450 to 700 °C, more preferably in the range of from 550 to 650 °C, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (22’) concretizing any one of embodiments (14’) or (21 ’) relates to said process, wherein calcining in (3) is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, more preferably in the range of from 1 to 2 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

A further preferred embodiment (23’) concretizing any one of embodiments (14’) or (22’) relates to said process, wherein the process consists of (1 ), (2) and (3).

An embodiment (24’) of the present invention relates to a NOx adsorber catalyst for the treatment of an exhaust gas, preferably a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (T) to (13’), obtainable or obtained by a process according to any one of embodiments (14’) to (23’).

An embodiment (25’) of the present invention relates to a method for the treatment of an exhaust gas by NOx adsorption comprising providing an exhaust gas, preferably from an internal combustion engine, more preferably from a diesel engine; contacting the exhaust gas with a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ’) to (13’) and (24’).

An embodiment (26’) of the present invention relates to a use of a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ’) to (13’) and (24’) for the treatment of an exhaust gas exiting from an internal combustion engine, more preferably a diesel engine, by NOx adsorption. An embodiment (27’) of the present invention relates to a system for the treatment of an exhaust gas, preferably exiting from an internal combustion engine, more preferably a diesel engine, the system comprising a NOx adsorber catalyst for the treatment of an exhaust gas according to any one of embodiments (1 ’) to (13’) and (24’), the catalyst comprising an inlet end and an outlet end; a selective catalytic reduction catalyst comprising an inlet end and an outlet end; wherein the outlet end of the NOx adsorber catalyst is positioned upstream of the inlet end of the selective catalytic reduction catalyst.

A preferred embodiment (28’) concretizing embodiment (27’) relates to said system, wherein the selective catalytic reduction catalyst comprises an 8-membered ring pore zeolitic material comprising one or more of copper and iron, preferably copper, wherein preferably the amount of one or more of copper and iron, calculated as CuO and FezOs, respectively, more preferably of copper, calculated as CuO, is in the range of from 1 to 10 weight-%, preferably in the range of from 2 to 8 weight-%, based on the weight of the 8-membered ring pore zeolitic material comprising one or more of copper and iron.

A further preferred embodiment (29’) concretizing embodiment (27’) or (28’) relates to said system, the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type selected from the group consisting of CHA, AEI, RTH, LEV, DDR, KFI, ERI, AFX, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA, AEI, RTH, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of CHA and AEI, wherein more preferably the 8-membered ring pore zeolitic material of the selective catalytic reduction catalyst has a framework type CHA.

Further, in the context of the present invention, a term “X is one or more of A, B and C”, wherein X is a given feature and each of A, B and C stands for specific realization of said feature, is to be understood as disclosing that X is either A, or B, or C, or A and B, or A and C, or B and C, or A and B and C. In this regard, it is noted that the skilled person is capable of transfer to above abstract term to a concrete example, e.g. where X is a chemical element and A, B and C are concrete elements such as Li, Na, and K, or X is a temperature and A, B and C are concrete temperatures such as 10 °C, 20 °C, and 30 °C. In this regard, it is further noted that the skilled person is capable of extending the above term to less specific realizations of said feature, e.g. “ X is one or more of A and B” disclosing that X is either A, or B, or A and B, or to more specific realizations of said feature, e.g. “X is one or more of A, B, C and D”, disclosing that X is either A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D.

Furthermore, in the context of the present invention, the term "the surface of the internal walls" is to be understood as the "naked" or "bare" or "blank" surface of the walls, i.e. the surface of the walls in an untreated state which consists - apart from any unavoidable impurities with which the surface may be contaminated - of the material of the walls. In the context of the present invention, the term “consists of’ with regard to the weight- % of one or more components indicates the weight- % amount of said component(s) based on 100 weight- % of the entity in question. For example, the wording “wherein from 0 to 0.001 weight- % of the first coating consists of X” indicates that among the 100 weight- % of the components of which said coating consists of, 0 to 0.001 weight- % is X.

In the context of the present invention, it is preferred that a platinum group metal component comprises, more preferably consists of, respective one or more platinum group metals or one or more oxides of respective one or more platinum group metals.

In the context of the present invention, a weight/loading of a platinum group metal component is calculated as the weight/loading of the respective platinum group metal as element or the sum of the weights/loadings of the respective platinum group metals as elements. For example, if a platinum group metal component is Rh, the weight of said platinum group metal component is calculated as elemental Rh. As a further example, if a platinum group metal component consists of Pt and Pd, the weight of said platinum group metal component is calculated as the sum of elemental Pt and elemental Pd.

In the context of the present invention, the definition of one or more platinum group metal components as being comprised in a zeolitic material, e.g. in an 8-membered ring pore zeolitic material, includes the possibility that the one or more platinum group metal components are impregnated onto or supported on the respective zeolitic material.

Furthermore, in the context of the present invention, the term “loading of a given compo- nent/coating/coat” (in g/in ³ or g/ft ³ ) refers to the mass of said component/coating per volume of the substrate, wherein the volume of the substrate is the volume which is defined by the crosssection of the substrate times the axial length of the substrate over which said component/coating is present. For example, if reference is made to the loading of a first coating extending over x % of the axial length of the substrate and having a loading of X g/in ³ , said loading would refer to X gram of the first coating per x% of the volume (in in ³ ) of the entire substrate.

The present invention is further illustrated by the following reference examples, comparative examples and examples.

Examples

Reference Example 1

1.1 Determination of the particle size distribution, Dv10, Dv50, Dv90 values The particle size distributions were determined by a static light scattering method using state-of- the-art equipment, wherein the optical concentration of the sample was in the range of from 5 to 10 %.

1.2 Measurement of the BET specific surface area

The BET specific surface area was determined according to DIN 66131 or DIN ISO 9277 using liquid nitrogen.

1.3 Determination of the crystall inity

The determination of the relative crystallinity of a zeolite was performed via x-ray diffraction using a test method under the jurisdiction of ASTM Committee D32 on catalysts, in particular of Subcommittee D32.05 on zeolites. The current edition was approved on March 10, 2001 and published in May 2001 , which was originally published as D 5758-95.

1.4 Determination of the total pore volume

The total pore volume was determined according to ISO 15901-2:2006.

Reference Example 2: Preparation of a NOx adsorber catalyst (blend of FER/CHA - 2:1)

A 2:1 (weight ratio) mixture of ammonium ferrierite (a zeolitic material having framework structure type FER, a SiC^AhOs molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) and Flchabazite (a zeolitic material having framework structure type CHA, a SiC^A Os molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic materials were wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours prior to attain a Pd loading of 1 .55 weight- % based on the weight of the final material (zeolitic materials + palladium). The powder from this Pd-zeolitic materials mixture was dispersed in water.

A porous uncoated flow-through cordierite honeycomb substrate (total volume 1 .85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 2.24 g/in ³ .

Reference Example 3: Preparation of a NOx adsorber catalyst (blend of FER/CHA - 1 :1)

A 1 :1 (weight ratio) mixture of ammonium ferrierite (a zeolitic material having framework structure type FER, a SiC^A C molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) and H- chabazite (a zeolitic material having framework structure type CHA, a SiC :AbO3 molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic materials were wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1 .55 weight- % based on the weight of the final material (zeolitic materials + palladium). The powder from this Pd-zeolitic materials mixture was dispersed in water. A porous uncoated flow- through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 2.24 g/in ³ .

Reference Example 4: Preparation of a NOx adsorber catalyst (blend of FER/CHA - 1 :2)

A 1 :2 (weight ratio) mixture of ammonium ferrierite (a zeolitic material having framework structure type FER, a SiC^AIzOs molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) and Flchabazite (a zeolitic material having framework structure type CHA, a SiC^AhOs molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic materials were wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1 .55 weight- % based on the weight of the final material (zeolitic materials + palladium). The powder from this Pd-zeolitic materials mixture was dispersed in water. A porous uncoated flow- through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 2.24 g/in ³ .

Reference Example 5: Preparation of a NOx adsorber catalyst (FER)

An ammonium ferrierite (a zeolitic material having framework structure type FER, a S^A^Os molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) zeolitic material was wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1.54 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-FER powder was dispersed in water. A porous uncoated flow-through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 80 g/ft ³ and the total washcoat loading was 3.0 g/in ³ .

Reference Example 6: Preparation of a NOx adsorber catalyst (CHA)

A H-chabazite (a zeolitic material having framework structure type CHA, a SiOz^hOs molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic material was wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours prior to attain a Pd loading of 1 .22 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-CHA powder was dispersed in water. A porous uncoated flow-through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 2.85 g/in ³ .

Reference Example 7: Preparation of a NOx adsorber catalyst (FER)

An ammonium ferrierite (a zeolitic material having framework structure type FER, a SiC^A Os molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) zeolitic material was wet impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1.22 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-FER powder was dispersed in water. A porous uncoated flow-through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 2.85 g/in ³ .

Comparative Example 1 : Preparation of a NOx adsorber (NA-) with a DOC function catalyst (layered catalyst - FER)

Bottom

An ammonium ferrierite (a zeolitic material having framework structure type FER, a SiC^A C molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) zeolitic material was wet impregnated with an aqueous palladium nitrate solution to attain a Pd loading of 2.31 weight- % based on the weight of the final material (zeolitic material + palladium). A porous uncoated flow-through cordierite honeycomb substrate (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches) was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom layer. The loading of palladium in the bottom coating was 120 g/ft ³ and the total bottom coating loading was 3 g/in ³ .

A high porous gamma-alumina support material comprising 5 % by weight Mn (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnOz, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with an aqueous solution of stabilized platinum complexes via a wet impregnation process. Ammonium Beta zeolitic material (a zeolitic material having framework structure type BEA, a SiC^A C molar ratio of 23 and a crystallinity vs. standard (XRD) > 90%) was added to the Pt-alumina mixture. The weight ratio of the alumina doped with Mn to the Beta zeolitic material was of 3.14:1. The substrate coated with the bottom coating was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590°C for 2 hours, forming a top coating. The loading of platinum in the top coating was 60 g/ft ³ and the total top coating loading was 1 .45 g/in ³ .

Comparative Example 2: Preparation of a NOx adsorber (NA-) with a DOC function catalyst (layered catalyst - CHA)

Bottom coating:

A H-chabazite (CHA, a S^A^Os molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic material was impregnated with an aqueous palladium nitrate solution and calcined in air at 590°C for 2 hours prior to attain a Pd loading of 3.10 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-CHA powder was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 1.85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom layer. The loading of palladium in the bottom coating was 120 g/ft ³ and the total bottom coating loading was 2.24 g/in ³ .

Top coating:

A high porous gamma-alumina support material comprising 5 % by weight Mn (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnOz, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with an aqueous solution of stabilized platinum complexes and an aqueous solution of palladium nitrate (a Pt to Pd weight ratio of 9:1) using an incipient wetness technique. A slurry containing the obtained Pt and Pd on alumina and water was prepared. An alumina support material comprising 5 % by weight of Si (AI2O3 95 weight-% with Si 5 weight-%, calculated as SIC>2, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was added to the Pt/Pd/Mn-alumina mixture in a weight ratio of 1 :1 (Mn-alumina to Si-alumina). Fe- Beta zeolite (BEA zeolitic material comprising iron in an amount of 1 .4 weight-% based on the weight of the zeolitic material, a SiC^AhOs molar ratio of 26 and a crystallinity vs. standard (XRD) > 90 %) was added to the slurry, forming a final slurry. The weight ratio of alumina (Mn- alumina to Si-alumina) to Fe-Beta zeolite was of 4.28:1 . The substrate coated with the bottom coating was coated with the final slurry on the bottom coating over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 hours, forming a top coating. The loading of platinum and palladium in the top coating was 40 g/ft ³ and the total top coating loading was 1 .95 g/in ³ .

Example 1 : Preparation of a NOx adsorber (NA-) with a DOC function catalyst (layered catalyst - FER/CHA blend)

Bottom coating (First coating): A 1 :1 (weight ratio) mixture of ammonium ferrierite (FER, a SiC^AhOs molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) and H-CHA (chabazite, a SiC^AhOs molar ratio of 14 and a crystallinity vs. standard (XRD) > 90%) zeolitic materials was wet impregnated with an aqueous palladium nitrate solution, calcined in air at 590 °C for 2 hours to attain a Pd loading of 2.31 weight- % based on the weight of the final material (zeolitic materials + palladium). The powder from this Pd-zeolitic materials mixture was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 1 .85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 120 g/ft ³ and the total bottom coating loading was 3 g/in ³ .

Top coating (second coating):

A high porous gamma-alumina support material comprising 5% by weight Mn (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnOz, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with a solution of stabilized platinum complexes via a wet impregnation process. Ammonium Beta zeolitic material (BEA, a SiO2:Al2Os molar ratio of 23 and a crystallinity vs. standard (XRD) > 90%) was added to the Pt-alumina mixture. The weight ratio of the alumina doped with Mn to the Beta zeolitic material was of 3.14:1. The substrate coated with the bottom coating was coated with the final slurry on the bottom coating over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 hours, forming the top coating. A topcoat containing this material and Beta zeolite was applied as a top layer to the bottom layer containing Pd on the mixture of FER+CHA. The top coat contained 60 g/ft ³ platinum and the top washcoat loading was 1 .45 g/in ³ .

Example 2: WLTC Evaluation of NOx adsorber catalysts of Reference Examples 2 to 6 on a diesel engine

Reference Examples 2 to 6 were tested each in a Worldwide Harmonized Light Vehicle Test Cycle (WLTC) on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to the first test the temperature of the NOx adsorber sample was increased to 650 °C for 10 min, to purge the NOx adsorber of pre-adsorbed NOx. The NOx adsorber catalyst from Reference Examples 2 to 6 were all tested with and without an selective catalytic reduction (SCR) catalyst downstream. The SCR catalyst article comprises CuCHA coated on a 3 L filter substrate. Between the NOx adsorber article and the SCR catalyst article an injector for urea dosing was applied to deliver the reductant for the SCR reaction.

Figure 1 provides the test results for exhaust sample after the NOx adsorber. All formulations adsorb NO _X in the exhaust leaving the engine up to about 800 s. Reference Example 5 shows the highest adsorption, however, after about 800 s, a high amount of NOx starts to release from NOx adsorber material. Reference Example 6 shows the lowest NOx adsorption, however, the release of NOx from this NOx adsorber material occurs more slowly. For Reference Examples 2 to 4 (using blend of CHA and FER zeolitic materials), NOx adsorption to about 800 s decreases with increasing content of CHA.

Figure 2 shows the corresponding emissions from the downstream SCR component. When the SCR catalytic article is placed after Reference Example 5, the NOx emission of the SCR catalyst is higher compared to the system comprising the NOx adsorber catalysts from Reference Examples 2 to 4. Under these conditions, the system with Reference Example 6 shows the lowest emissions.

Example 3: Testing of Reference Examples 2 to 6 - Simulated low temperature city driving cycle, NOx adsorption evaluation

Reference Examples 2 to 6 were each tested using a simulated low temperature city driving mode on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. The driving cycle was compiled from city driving mode of the New European Driving Cycle (NEDC). The average temperature of the cycle was about 170 °C. The cycle was driven twice for 1880 s. Prior to the first test the temperature of the NOx adsorber catalysts was increased to 650 °C for 10 min, to purge pre-adsorbed NOx.

Figure 3 provides the test results of the first test run. All formulations adsorb some NO _X from the exhaust leaving the engine up to about 500 s. The higher the CHA amount in the NOx adsorber the lower the NOx adsorption during the first 500 s. At the end of the first test, Reference Examples 2 (with blend of FER and CHA), 3 (with blend of FER and CHA) and 5 (with FER only) show a similar NOx adsorption and NOx release whereas Reference Example 6 shows the lowest NOx release.

Prior to the second test run, the samples were cooled to room temperature, without the high temperature preconditioning. Figure 4 provides the test results of the second test run. In the 2 ^nd test run, Reference Example 6 (with CHA only) shows no NOx adsorption as the NOx is not released during the cold city cycle. When run on this cold city cycle, Reference Example 6 would require an undesirable thermal treatment to release the stored NOx. The higher the FER amount in the NOx adsorber, the higher the NOx adsorption during the first 500 s of the second cold city cycle is found.

Reference Examples 2 (with blend of FER and CHA) and 3 (with blend of FER and CHA) provide the high NOx adsorption feature and the good thermal NOx release of Pd/FER as well as a better NOx handshake with the downstream Cu-CHA SCR catalytic article and thus lower emissions in the WLTC evaluation compared to Reference Example 5. Thus, this example illustrates that using a blend of a zeolitic material FER and a zeolitic material CHA permits to provide a better balance between NOx adsorption and NOx release compare to the use of only a zeolitic material FER (Ref. Ex. 5) or only a zeolitic material CHA (Ref. Ex. 6). Exampie 4: WLTC Evaluation of NOx adsorber catalysts of Example 1 , Comparative

Examples 1 and 2

Example 1 , Comparative Examples 1 and 2 were tested each in a Worldwide Harmonized Light Vehicle Test Cycle (WLTC) on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to the first test, the temperature of the NOx adsorber sample was increased to 650 °C for 10 min, to remove pre-adsorbed NOx. The NOx adsorber catalysts from Example 1 , Comparative Examples 1 and 2 were evaluated with and without a downstream SCR catalyst. The SCR catalyst comprises Cu-CHA coated on a 3 L filter substrate. Between the NOx adsorber + DOC catalyst and the SCR catalyst, an injector for urea dosing was applied to deliver the reductant for the SCR reaction.

Figure 5 provides the test results. The thicker lines are the emissions from the NOx adsorber catalyst samples upstream to the SCR. The thin lines show the NOx emissions downstream the SCR catalytic. All formulations adsorb NO _X in the exhaust leaving the engine up to about 800 s. Comparative Example 1 and Example 1 show the highest adsorption. Only Comparative Example 1 shows a high release of NOx after about 800 s, and therefore the highest NOx emissions from the downstream SCR catalyst. Comparative Example 2 shows the lowest NOx adsorption. Comparative Example 2 and Example 1 show the same low NOx emissions from the catalytic article. This shows that Example 1 achieves the same good NOx handshake with the SCR as Comparative Example 2, while keeping the high NOx adsorption during cold-start. In this regard, a good NOx handshake can be understood as a phenomenon where most of the NOx which is thermally released by the NA-DOC will be converted by the downstream SCR (the temperature needs to be high enough); if the NOx desorption temperature is too low the NOx will only partially be converted by the SCR (Pd/FER).

Example 5: Testing of Example 1 , Comparative Examples 1 and 2 - Simulated low temperature city driving cycle, NOx adsorption evaluation

Example 1 and Comparative Examples 1 and 2 were tested each in a simulated low temperature city driving mode on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. The driving cycle was compiled from city driving mode of the New European Driving Cycle (NEDC). The average temperature of the cycle was about 170 °C. The cycle was driven twice for 1880 s. The tests were conducted with and without an SCR catalyst downstream from the NOx adsorber-DOC from the Example 1 , Comparative Examples 1 and 2 noted above. The SCR catalyst article comprises Cu-CHA coated on a 3 L filter substrate. Between the NOx adsorber-DOC catalyst and the SCR catalyst, an injector for urea dosing was applied to deliver the reductant for the SCR reaction. Prior to the first test the temperature of the NOx adsorber-DOC catalysts was increased to 650 °C for 10 min. Figure 6 provides the test results of the first test run. All formulations adsorb NO _X in the exhaust leaving the engine up to about 500 s. The lowest emissions are achieved by Comparative Example 2 and inventive Example 1 caused by a superior handshake with the downstream SCR catalyst.

Figure 7 provides the test results of the second test run. In the 2 ^nd test run, Comparative Example 2 shows little NOx adsorption during the first 500 s. Example 1 shows in the 2 ^nd run a high NOx adsorption like Comparative Example 1. The emissions of the system comprising Example 1 and the downstream SCR catalyst are still the lowest among the 3 samples. Thus, this example shows that the inventive NOx adsorber-DOC catalyst of the present invention (Example 1 ) provides the high NOx adsorption feature and the good thermal NOx release of Pd/FER as well as better NOx handshake with the downstream Cu-CHA SCR catalyst.

Comparative Example 3: Preparation of a NOx adsorber (NA) with a DOC function catalyst (layered catalyst - FER)

Bottom coating:

An ammonium ferrierite zeolitic material (FER, a SiC^A Os molar ratio of 21 and a crystallinity vs. standard (XRD) > 80%) was impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours prior to attain a Pd loading of 1 .85 weight- % based on the weight of the zeolitic material. The powder from this Pd-zeolitic material mixture was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, diameter: 1 inch x length: 3 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 80 g/ft ³ and the bottom coating loading was 2.5 g/in ³ .

Top coating:

A high porous gamma-alumina support material comprising 5 % by weight Mn (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnOz, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with an aqueous solution of stabilized platinum complexes and an aqueous solution of palladium nitrate (a Pt to Pd weight ratio of 9:1) using an incipient wetness technique. A slurry containing the obtained Pt and Pd on alumina and water was prepared. An alumina support material comprising 5 % by weight of Si (AI2O3 95 weight-% with Si 5 weight-%, calculated as SiCb, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was added to the Pt/Pd/Mn-alumina mixture in a weight ratio of 1 :1 (Mn-alumina to Si-alumina). Fe- Beta zeolite (BEA zeolitic material comprising iron in an amount 1 .4 weight-% based on the weight of the zeolitic material, a SiC^AhCb molar ratio of 26 and a crystallinity vs. standard (XRD) > 90 %) was added to the slurry, forming a final slurry. The weight ratio of alumina (Mn- alumina + Si-alumina) to Fe-Beta zeolite was of 4.28:1. The substrate coated with the bottom coating was coated with the final slurry on the bottom coating over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 hours, forming a top coating. The loading of platinum and palladium in the top coating was 60 g/ft ³ (9:1 Pt/Pd weight ratio) and the top coating loading was 1 .9 g/in ³ .

Comparative Example 4: Preparation of a NOx adsorber (NA-) with a DOC function catalyst (layered catalyst - CHA)

Bottom coating:

A H-chabazite (CHA, a SiC^A Os molar ratio of 31 and a crystallinity vs. standard (XRD) > 90%) zeolitic material was impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours prior to attain a Pd loading of 1 .85 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-CHA powder was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, diameter: 1 inch x length: 3 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 80 g/ft ³ and the bottom coating loading was 2.5 g/in ³ .

Top coating: The top coating of Comparative Example 4 was prepared as the top coating of Comparative Example 3. The loading of platinum and palladium in the top coating was 60 g/ft ³ (9:1 Pt/Pd weight ratio) and the top coating loading was 1 .9 g/in ³ .

Example 6: Preparation of a NOx adsorber (NA) with a DOC function catalyst (layered catalyst - LEV)

Bottom coating:

An ammonium levyne zeolitic material (LEV, a SiO2:Al2Os molar ratio of 31 and a crystallinity vs. standard (XRD) > 90%) was impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1 .85 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-LEV powder was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, diameter: 1 inch x length: 3 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 80 g/ft ³ and the bottom coating loading was 2.5 g/in ³ .

Top coating: The top coating of Example 6 was prepared as the top coating of Comparative Example 3. The loading of platinum and palladium in the top coating was 60 g/ft ³ (9:1 Pt/Pd weight ratio) and the top coating loading was 1 .9 g/in ³ . Exampie 7: Preparation of a NOx adsorber (NA) with a DOC function catalyst (layered catalyst - FER)

Bottom coating:

An ammonium ferrierite zeolitic material (FER, a S^AhOs molar ratio of 53 and a crystallinity vs. standard (XRD) > 90 %) was impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours prior to attain a Pd loading of 1.85 weight- % based on the weight of the final material (zeolitic material + palladium). The powder from this Pd-zeolitic material mixture was dispersed in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 0.04 L 400 cpsi and 4 mil wall thickness, diameter: 1 inch x length: 3 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590°C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 80 g/ft ³ and the bottom coating loading was 2.5 g/in ³ .

Top coating: The top coating of Example 7 was prepared as the top coating of Comparative Example 3. The loading of platinum and palladium in the top coating was 60 g/ft ³ (9:1 Pt/Pd weight ratio) and the top coating loading was 1 .9 g/in ³ .

Example 8: Evaluation of NOx adsorber with a DOC function catalysts of Comparative Examples 3, 4 and Examples 6 and 7 on Steady State Lab Reactor

Comparative Examples 3 and 4 and Examples 6 and 7 were tested for NOx adsorption and desorption performance after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to desorption, the samples (cores of 1 x 3 inch) were exposed to a mixture of 200 ppm nitric oxide (NO), 500 ppm carbon monoxide (CO), 500 ppm propylene (C3H6, Ci basis), 7 % oxygen (O2), 5% carbon dioxide (CO2), 5 % water (H2O) and balance nitrogen (N2) for 15 minutes at 100 °C. During this period, NO was adsorbed to the Pd/zeolite. After the adsorption phase, the NO, CO and propylene were turned off and the temperature of the sample was raised to 500 °C at 20 °C/min. During this period, NO that was adsorbed to the Pd/zeolite was desorbed (desorption phase). NO desorption results for Examples 6 (Pd/LEV, SAR 31 ) and 7 (Pd/FER, SAR 53) as a function of temperature are shown in Figure 8. Results for Comparative Examples 3 (FER, SAR of 21) and 4 (CHA, SAR of 31) are also included. For both inventive examples, most desorption of NO occurs at a higher temperature relative to the results for the catalyst of Comparative Example 3 (Pd/FER with a SAR of 21) and a lower temperature relative to the results for the catalyst of Comparative Example 4 (Pd/CHA with a SAR of 31). For the inventive catalysts, the NO desorption profiles overcome the main disadvantages of Pd/CHA and Pd/FER. In particular, it can be gathered from the testing results that the catalysts of the present invention are tunable with respect to their NOx adsorption and/or desorption properties.

Example 9: Preparation of a NOx adsorber (NA) catalyst (single coating - MFI) An ammonium ZSM-5 zeolitic material (zeolitic material having framework structure type MFI, a SiO2:Al2Os molar ratio of 27 and a crystallinity vs. standard (XRD) > 90%) was impregnated with an aqueous palladium nitrate solution and calcined in air at 590 °C for 2 hours to attain a Pd loading of 1 .16 weight- % based on the weight of the final material (zeolitic material + palladium). This Pd-MFI powder was slurried in water. A porous uncoated flow-through honeycomb substrate, cordierite (total volume 0.04 L 400 cpsi and 4 mil wall thickness, diameter: 1 inch x length: 3 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air having a temperature of 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h. The loading of palladium on the coated substrate was 60 g/ft ³ and the total washcoat loading was 3.0 g/in ³ .

The catalyst of Example 9 was tested as in Example 8. NO desorption results for Example 9 (MFI, SAR 27) as a function of temperature are shown in Figure 9. Results for Reference Examples 6 (CHA, SAR 14) and 7 (FER, SAR 21) are also included. For the Pd/MFI, most desorption of NO occurs at a higher temperature relative to Pd/FER and a lower temperature relative to Pd/CHA.

Example 10: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst - FER (SIO2:Al2O3 molar ratio of 53:1)

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiO2:Al2Os molar ratio of 53:1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution to attain a Pd loading of 1 .48 weight- % based on the weight of the final material (zeolitic material + palladium). To the resulting slurry a zirconium acetate mixture was added. The amount of zirconium acetate was calculated such that the amount of zirconia in the bottom coating, calculated as ZrC>2, was 5 weight- % based on the weight of the zeolitic material.

A porous uncoated round flow-through honeycomb substrate, cordierite (total volume 1 .85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air at 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 70 g/ft ³ , the concentration of the FER in bottom coating loading was 2.7 g/in ³ and of ZrC>2 was 0.135 g/in ³ . The loading of the bottom coating was 2.9 g/in ³ .

Top coating (DOC coating):

Outlet coat:

An AI2O3 support material comprising 5 weight- % MnO2 (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnO2, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with platinum via a wet impregnation process. A slurry containing the resulting material was coated over 50 % of the substrate axial length from the outlet end towards the inlet end of the cordierite substrate carrying the Pd-FER bottom coating. The outlet coat contained 80 g/ft ³ platinum and the loading of the outlet coat was 1 .3 g/in ³ .

Inlet coat:

An alumina support material comprising 5% by weight SiOz (AI2O3 95 weight- % with Si 5 weight- %, calculated as SiOz, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with platinum and palladium in a weight ratio of 2:1 via a wet impregnation process. A Fe-Beta zeolitic material (a zeolitic material having framework structure type BEA, a SiC^AhOs molar ratio of 23:1 and a crystallinity vs. standard (XRD) > 90% and Fe content, calculated as FezOs: 4.3 weight- % based on the weight of the zeolitic material) was added to the Pt/Pd-alumina slurry. The weight ratio of the alumina doped with Si to the Beta zeolitic material was of 1/1 . A slurry containing this material and Beta zeolite was coated over 50% of the substrate axial length from the inlet end towards the outlet end of the cordierite substrate supporting already the Pd-FER bottom layer and the outlet coat. The inlet coat contained 13.3 g/ft ³ platinum and 6.7 g/ft ³ Pd. The loading of the inlet coat was 1 .41 g/in ³ . The total loading of the top coating (outlet coat + inlet coat) was 1.355 g/in ³ .

Comparative Example 5: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst - FER (SK^AbOa molar ratio of 21 :1 )

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiOz^ Os molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution to attain a Pd loading of 1 .48 weight- % based on the weight of the final material (zeolitic material + palladium). To the resulting slurry a zirconium acetate mixture was added. The amount of zirconium acetate was calculated such that the amount of zirconia in the bottom coating, calculated as ZrC>2, was 5 weight- % based on the weight of the zeolitic material.

A porous uncoated round flow-through honeycomb substrate, cordierite (total volume 1 .85 L, 400 cpsi and 4 mil wall thickness, diameter: 5.66 inches x length: 4.5 inches), was coated with the obtained slurry over 100 % of the substrate axial length. The coated substrate was dried in air at 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coating. The concentration of palladium in the bottom coating was 70 g/ft ³ , the concentration of the FER in bottom coating loading was 2.7 g/in ³ and of ZrC>2 was 0.135 g/in ³ . The loading of the bottom coating was 2.9 g/in ³ .

Top coating (DOC coating):

Outlet coat: An AI2O3 support material comprising 5 weight- % MnOz (AI2O3 95 weight- % with Mn 5 weight-%, calculated as MnC>2, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with platinum via a wet impregnation process. A slurry containing the resulting material was coated over 50 % of the substrate axial length from the outlet end towards the inlet end of the cordierite substrate carrying the Pd-FER bottom coating. The outlet coat contained 80 g/ft ³ platinum and the loading of the outlet coat was 1 .3 g/in ³ .

Inlet coat:

An alumina support material comprising 5% by weight SIC>2 (AI2O3 95 weight-% with Si 5 weight- %, calculated as SIC>2, having a BET specific surface area of greater than 100 m ² /g, and a pore volume of greater than 0.06 cm ³ /g) was impregnated with platinum and palladium in a weight ratio of 2:1 via a wet impregnation process. A Fe-Beta zeolitic material (a zeolitic material having framework structure type BEA, a SiC^AhOs molar ratio of 23:1 and a crystallinity vs. standard (XRD) > 90% and Fe content, calculated as Fe2C>3: 4.3 weight-% based on the weight of the zeolitic material) was added to the Pt/Pd-alumina slurry. The weight ratio of the alumina doped with Si to the Beta zeolitic material was of 1/1 . A slurry containing this material and Beta zeolite was coated over 50% of the substrate axial length from the inlet end towards the outlet end of the cordierite substrate supporting already the Pd-FER bottom layer and the outlet coat. The inlet coat contained 13.3 g/ft ³ platinum and 6.7 g/ft ³ Pd. The loading of the inlet coat was 1 .41 g/in ³ . The total loading of the top coating (outlet coat + inlet coat) was 1.355 g/in ³ .

Example 11 : WLTC Evaluation of NOx adsorber catalysts of Example 10 and Comparative Example 5

Example 10 and Comparative Example 5 were tested each in a Worldwide Harmonized Light Vehicle Test Cycle (WLTC) on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to the first test, the temperature of the NOx adsorber sample was increased to 650 °C for 10 min, to remove pre-adsorbed NOx. The NOx adsorber catalysts from Example 10 and Comparative Example 5 were evaluated with and without a downstream SCR catalyst. The SCR catalyst comprises Cu-CHA coated on a 3 L filter substrate. Between the NOx adsorber + DOC catalyst and the SCR catalyst, an injector for urea dosing was applied to deliver the reductant for the SCR reaction.

Figure 10 provides the test results. The solid lines are the emissions from the NOx adsorber catalyst samples upstream to the SCR. The dotted lines show the NOx emissions downstream of the SCR catalyst. The lowest emissions are achieved by inventive Example 10 caused by a superior handshake with the downstream SCR catalyst.

Example 12: Testing of Example 10 and Comparative Example 5 - Simulated low temperature city driving cycle, NOx adsorption evaluation

Example 10 and Comparative Example 5 were tested each in a simulated low temperature city driving mode on a 2 L diesel engine after hydrothermal aging at 800 °C for 16 hours in 10 % steam (wateij/air. The driving cycle was compiled from city driving mode of the New European Driving Cycle (NEDC). The average temperature of the cycle was about 170 °C. The cycle was driven twice for 1880 s. The tests were conducted with and without an SCR catalyst downstream from the NOx adsorber-DOC from the Example 10 and Comparative Example 5 noted above. The SCR catalyst article comprises Cu-CHA coated on a 3 L filter substrate. Between the NOx adsorber-DOC catalyst and the SCR catalyst, an injector for urea dosing was applied to deliver the reductant for the SCR reaction. The solid lines are the emissions from the NOx adsorber catalyst samples upstream to the SCR. The dotted lines show the NOx emissions downstream of the SCR catalyst. Prior to the first test the temperature of the NOx adsorber- DOC catalysts was increased to 650 °C for 10 min.

Figure 11 provides the test results of the first test run. The lowest emissions are achieved by inventive Example 10 caused by a superior handshake with the downstream SCR catalyst.

Figure 12 provides the test results of the second test run. The results of both the first and second runs are in good agreement the results for example 5. Thus, this example shows that the inventive NOx adsorber-DOC catalyst of the present invention (Example 10) provides the high NOx adsorption feature and the good thermal NOx release of Pd/FER (SiOz^Os molar ratio of 53:1 ) as well as better NOx handshake with the downstream Cu-CHA SCR catalyst.

Brief description of the figures

Figure 1 shows the NOx adsorption/desorption evaluation of Reference Examples 2 to 6 on a diesel engine (at the outlet of the NOx adsorber). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 2 shows the NOx adsorption/desorption evaluation of Reference Examples 2 to 6 on a diesel engine (at the outlet of the downstream SCR). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 3 shows the NOx adsorption/desorption evaluation of Reference Examples 2 to 6 (first test run). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 4 shows the NOx adsorption/desorption evaluation of Reference Examples 2 to 6 (second test run). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h. Figure 5 shows the NOx adsorption/desorption evaluation of Example 1 , Comparative Examples 1 and 2 (WLTC). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 6 shows the NOx adsorption evaluation of Example 1 , Comparative Examples 1 and 2 (Simulated low temperature city driving cycle - first test run). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 7 shows the NOx adsorption evaluation of Example 1 , Comparative Examples 1 and 2 (Simulated low temperature city driving cycle - second test run). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 8 shows the NOx desorption results relative to the temperature for Comparative Examples 3, 4 and Examples 6 and 7 (Steady State Lab Reactor). On the abscissa, the temperature is noted in °C. On the ordinate, the NO concentration in ppm is noted.

Figure 9 shows NO desorption results relative to the temperature for Example 9. On the abscissa, the temperature is noted in °C. On the ordinate, the NO concentration in ppm is noted.

Figure 10 shows the NOx adsorption/desorption evaluation of Example 10, Comparative Examples 5 (WLTC). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 11 shows the NOx adsorption evaluation of Example 10, Comparative Examples 5 (Simulated low temperature city driving cycle - first run test). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Figure 12 shows the NOx adsorption evaluation of Example 10, Comparative Examples 5 (Simulated low temperature city driving cycle - second run test). On the abscissa, the time in seconds is noted. On the left ordinate, the NOx emissions of the engine in g are noted and on the right ordinate the temperature is noted in °C as well as the speed in km/h.

Cited literature

WO 2015/085300 A1

US 2017/0096923 A1 - A. Porta et aL, “Low Temperature NOx Adsorption Study on Pd-Promoted Zeolites” in Topics in Calysis 2018, vol. 61 , p. 2021-2034 (https://doi.org/10.1007/s11244-018- 1045-8)

- Y. Zheng et aL, “Low-Temperature Pd/Zeolite Passive NOx Adsorbers: Structure, Per- formance, and Adsorption Chemistry” in J. Phys. Chem. C 2017, vol. 121 , p. 15793-

15803

- Y. Ryou et aL, “Effect of various activation conditions on the low temperature NO adsorption performance of Pd/SSZ-13 passive NOx adsorber” in Catalysis Today 2019, vol. 320, p. 175-180 (https://doi.Org/10.1016/j.cattod.2017.11.030)