NOx adsorber diesel oxidation catalyst

The present invention relates to a NOx adsorber diesel oxidation catalyst, a process for prepar ing said catalyst and a use of said catalyst. Further, the present invention relates to an exhaust gas treatment system comprising said catalyst.

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 legisla tions setting limits for NOx emissions. NOx adsorber diesel oxidation catalysts are thus used together with selective catalytic reduction catalysts.

During the treatment of an exhaust gas exiting an engine, NA-DOCs based on palladium/zeolite adsorb NOx at high efficiency rate during the so-called “cold-start” period, which is the time pe riod at the beginning of the treatment process, when the exhaust gas stream and the exhaust gas treatment system are at low temperatures (i.e., below 150 °C). Said catalysts further re lease the NOx, when downstream SCR catalyst(s) starts to convert NOx. For example, it is known in the art that Pd/FER can be used as NOx adsorber (NA). Flowever, at these low tem peratures, exhaust gas treatment systems generally do not display sufficient catalytic activity for effectively treating hydrocarbons (HC), nitrogen oxides (NOx) and/or carbon monoxide (CO) emissions. In general, catalytic components such as SCR catalyst components are very effec tive in converting NOx to N2 at temperatures above 200°C but do not exhibit sufficient activities at lower temperature regions ( <200°C) such as those found during cold-start or prolonged low- speed city driving. In order to overcome such problems, a system comprising NOx adsorber diesel oxidation catalyst was described in WO 2020/236879 A1. Flowever, there is still a need to provide a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, wherein the catalyst exhibits in particular an improved performance with respect to its NOx ad sorption and/or desorption properties.

It was therefore an object of the present invention to provide a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, wherein the catalyst exhibits in particu lar an improved performance with respect to its NOx adsorption and/or desorption properties, in particular permits to maintain good NOx adsorption and delay the NOx desorption to higher tar geted temperatures.

Surprisingly, it was found that the NOx adsorber diesel oxidation catalyst according to the pre sent invention permits to maintain high and durable NOx adsorption and delay the NOx desorp tion to higher targeted temperatures. In particular, it was possible to shift the NOx desorption temperature towards higher temperatures from about 200 °C to about 300 °C which thus permit to have higher amount of NOx converted by a downstream SCR catalyst.

Therefore, the present invention relates to a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, the catalyst comprising: (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 NOx adsorber (NA) coating disposed on the surface of the internal walls of the substrate (i), said coating comprising a platinum group metal, a zeolitic material and one or more of an alkaline earth metal and manganese;

(iii) a diesel oxidation catalyst (DOC) coating, said coating comprising a platinum group metal supported on a non-zeolitic oxidic material.

Preferably the DOC coating extends over y % of the substrate axial length, with y being in the range of from 20 to 100 and the NA coating extends over x % of the substrate axial length, more preferably from the outlet end towards the inlet end of the substrate, with x being in the range of from 40 to 100.

Preferably the DOC coating is disposed on the NA coating and/or on the surface of the sub strate axial length.

Preferably the platinum group metal comprised in the NA coating (ii) is selected from the group consisting of palladium, platinum, rhodium, iridium, osmium, ruthenium and a mixture of two or more thereof, more preferably selected from the group consisting of palladium, platinum and rhodium, more preferably selected from the group consisting of palladium and platinum, more preferably is palladium.

More preferably the platinum group metal comprised in the NA coating (ii) is palladium. More preferably the platinum group metal comprised in the NA coating (ii) is palladium and the NA coating (ii) is substantially free of, more preferably free of, platinum.

Preferably the NA coating (ii) comprises the platinum group metal at a loading, calculated as elemental platinum group metal, in the range of from 1 to 150 g/ft ³ , more preferably in the range of from 5 to 100 g/ft ³ , more preferably in the range of from 10 to 90 g/ft ³ , more preferably in the range of from 15 to 80 g/ft ³ , more preferably in the range of from 15 to 40 g/ft ³ , or more prefera bly in the range of from 50 to 80 g/ft ³ .

It is more preferred that the platinum group metal comprised in the NA coating (ii) is palladium which is present at a loading, calculated as elemental Pd, in the range of from 1 to 150 g/ft ³ , more preferably in the range of from 5 to 100 g/ft ³ , more preferably in the range of from 10 to 90 g/ft ³ , more preferably in the range of from 15 to 80 g/ft ³ , more preferably in the range of from 15 to 40 g/ft ³ , or more preferably in the range of from 50 to 80 g/ft ³ .

As to the zeolitic material comprised in the NA coating (ii), it is preferred that it is a 10- membrered ring pore zeolitic material, wherein the 10-membered ring pore zeolitic material more preferably has framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, H EU , 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, TON, MFI, MWW, AEL, H EU , 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. It is more preferred that the 10-membered ring pore zeolitic material comprised in the NA coating (ii) has a framework type FER.

Preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the framework struc ture of the 10-membered ring pore zeolitic material comprised in the NA coating (ii) consist of Si, Al, and O. In the framework structure of the 10-membered ring pore zeolitic material, the molar ratio of Si to Al, calculated as molar SiC^A Ch, more preferably is in the range of from 2:1 to 60:1 , more preferably in the range of from 2:1 to 50:1 , more preferably in the range of from 5:1 to 40:1 , more preferably in the range of from 10:1 to 35:1 , more preferably in the range of from 15:1 to 30:1 , more preferably in the range of from 18:1 to 25:1.

Preferably the NA coating (ii) comprises the zeolitic material in an amount in the range of from 0.5 to 5 g/in ³ , more preferably in the range of from 1 to 4 g/in ³ , more preferably in the range of from 1.25 to 3 g/in ³ .

Preferably the zeolitic material comprised in the NA coating (ii) supports the platinum group metal. More preferably the zeolitic material comprised in the NA coating (ii) has a framework type FER or TON and supports palladium as the platinum group metal.

Preferably the NA coating (ii) comprises an alkaline earth metal, wherein the alkaline earth met al is more preferably selected from the group consisting of barium, strontium, calcium and mag nesium, more preferably selected from the group consisting of barium, strontium and magnesi um, more preferably is barium or strontium; or wherein the alkaline earth metal is barium and strontium, wherein more preferably the ratio of the weight of Ba, calculated as the oxide, relative to the weight of Sr, calculated as the oxide, 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 3:1 to 6:1.

Preferably the zeolitic material of the NA coating (ii) has a framework type FER or TON, more preferably FER, the platinum group metal of the NA coating (ii) is palladium. More preferably the zeolitic material of the NA coating (ii) has a framework type FER or TON, more preferably FER, the platinum group metal of the NA coating (ii) is palladium and the NA coating (ii) further com prises an alkaline earth metal as defined in the foregoing.

In the context of the present invention, the alkaline earth metal comprised in the NA coating (ii) is preferably present as oxides, cations and/or carbonates.

It is preferred that the NA coating (ii) comprises the alkaline earth metal in a total amount, calcu lated as the oxide, in the range of from 0.5 to 15 weight-%, more preferably in the range of from 1 to 10 weight-%, more preferably in the range of from 1.5 to 8 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii).

According to the present invention, it is more preferred that the NA coating (ii) comprises palla dium, a 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type FER, and barium. Alternatively, it is more preferred that the NA coating (ii) com prises palladium, a 10-membered ring pore zeolitic material, more preferably a zeolitic material having a framework type FER, and strontium.

Preferably the NA coating (ii) further comprises a non-zeolitic oxidic material, wherein the non- zeolitic oxidic material is selected from the group consisting of zirconia, alumina, silica, titania, ceria, a mixed oxide comprising one or more of Zr, Al, Si, Ti, and Ce and a mixture of two or more thereof, more preferably selected from the group consisting of zirconia, alumina, ceria and titania, more preferably selected from the group consisting of zirconia, alumina and ceria, more preferably is zirconia.

It is preferred that the NA coating (ii) comprises the non-zeolitic oxidic material in an amount in the range of from 1 to 30 weight-%, more preferably in the range of from 2 to 25 weight-%, more preferably in the range of from 4 to 21 weight-%, more preferably in the range of from 4 to 8 weight-% or more preferably in the range of from 18 to 21 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii).

Preferably the NA coating (ii) comprises manganese.

Preferably the zeolitic material of the NA coating (ii) has a framework type FER or TON, more preferably FER, the platinum group metal of the NA coating (ii) is palladium and the NA coating (ii) further comprises manganese.

It is preferred that the NA coating (ii) comprises manganese in an amount calculated as Mn0 ₂ , in the range of from 0.25 to 5 weight-%, more preferably in the range of from 0.5 to 3 weight-%, more preferably in the range of from 0.75 to 1.5 weight-% based on the weight of the zeolitic material comprised in the NA coating (ii).

Preferably the NA coating (ii) comprises barium and manganese.

Alternatively, the NA coating (ii) preferably comprises strontium and manganese.

Alternatively, the NA coating (ii) preferably comprises barium, strontium and manganese.

Preferably the zeolitic material of the NA coating (ii) has a framework type FER or TON, more preferably FER, the platinum group metal of the NA coating (ii) is palladium and the NA coating (ii) further comprises manganese and an alkaline earth metal, more preferably one or more of barium and strontium, more preferably barium or strontium or barium and strontium. Preferably the NA coating (ii) further comprises an alkali metal, wherein the alkali metal is more preferably selected from the group consisting of sodium, potassium and lithium, wherein the alkali metal is more preferably sodium.

Preferably the NA coating (ii) comprises manganese and sodium.

Preferably the zeolitic material of the NA coating (ii) has a framework type FER or TON, more preferably FER, the platinum group metal of the NA coating (ii) is palladium and the NA coating (ii) further comprises manganese and an alkali metal, more preferably sodium.

Preferably the NA coating (ii) comprises the alkali metal in an amount, calculated as the oxide, in the range of from 0.1 to 4 weight-%, more preferably in the range of from 0.25 to 3 weight-%, more preferably in the range of from 0.5 to 2 weight-%, based on the weight of the zeolitic mate rial comprised in the NA coating (ii).

Preferably the NA coating (ii) comprises sodium in an amount, calculated as NaO, in the range of from 0.1 to 4 weight-%, more preferably in the range of from 0.25 to 3 weight-%, more prefer ably in the range of from 0.5 to 2 weight-%, more preferably in the range of from 0.5 to 1 weight- %, based on the weight of the zeolitic material comprised in the NA coating (ii). Alternatively, the NA coating (ii) preferably comprises potassium in an amount, calculated as K2O, in the range of from 0.1 to 4 weight-%, more preferably in the range of from 0.25 to 3 weight-%, more prefera bly in the range of from 0.5 to 2 weight-%, more preferably in the range of from 1.2 to 2 weight- %, based on the weight of the zeolitic material comprised in the NA coating (ii).

In the context of the present invention, it is preferred that the NA coating (ii) further comprises one or more of Nd, La, Ce, Pr, Sm, Y and Yb, preferably one or more of Nd and Pr, more pref erably Nd. It is preferred that the NA coating (ii) comprises the one or more of Nd, La, Ce, Pr, Sm, Y and Yb, in an amount, calculated as the oxide, in the range of from 2 to 6 weight-%, more preferably in the range of from 3 to 5 weight-%, more preferably in the range of from 4 to 5 weight-% based on the weight of the zeolitic material comprised in the NA coating (ii).

Preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, barium, and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the plat inum group metal, more preferably palladium, the zeolitic material, more preferably having a framework type FER, barium, and more preferably a non-zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, strontium and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, more preferably palladium, the zeolitic material, more preferably having a framework type FER, strontium and more preferably a non-zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, manganese, an alkaline earth metal, more preferably barium or strontium, and more preferably a non-zeolitic oxidic material as defined in the forego ing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group met al, more preferably palladium, the zeolitic material, more preferably having a framework type FER, manganese, an alkaline earth metal, more preferably barium or strontium, and more pref erably a non-zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, manganese, barium, strontium, and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight- %, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, more preferably palladium, the zeolitic material, more preferably having a framework type FER, manganese, barium, strontium and more preferably a non-zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, manganese, an alkali metal, more preferably sodium, as defined in the foregoing, and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight- %, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, more preferably palladium, the zeolitic material, more preferably having a frame work type FER, manganese, an alkali metal, more preferably sodium, as defined in the forego ing, and more preferably a non-zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, an alkaline earth metal, more preferably barium or strontium, and one or more of Nd, La, Ce, Pr, Sm, Y and Yb, and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the N A coating (ii) consists of the platinum group metal, more preferably palladium, the zeolitic material, more preferably having a framework type FER, an alkaline earth metal, more preferably barium or strontium, and one or more of Nd, La, Ce, Pr, Sm, Y and Yb, and more preferably a non- zeolitic oxidic material as defined in the foregoing.

Alternatively, preferably, the NA coating (ii) comprises palladium, the zeolitic material, more preferably having a framework type FER, manganese, and more preferably a non-zeolitic oxidic material as defined in the foregoing. More preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, more preferably palladium, the zeolitic material, more preferably having a framework type FER, manganese, and more preferably a non-zeolitic oxidic material as defined in the foregoing.

In the context of the present invention, it is preferred that the platinum group metal comprised in the DOC coating (iii) is selected from the group consisting of palladium, platinum, rhodium, iridi um, osmium, ruthenium and a mixture of two or more thereof, more preferably selected from the group consisting of palladium, platinum and rhodium, more preferably selected from the group consisting of palladium and platinum, more preferably is platinum. In this regard, it is also con ceivable that the platinum group metal comprised in the DOC coating (iii) be preferably platinum and palladium.

Preferably the DOC coating (iii) comprises the platinum group metal component at a loading, calculated as elemental platinum group metal, in the range of from 1 to 150 g/ft ³ , more prefera bly in the range of from 10 to 100 g/ft ³ , more preferably in the range of from 20 to 90 g/ft ³ , more preferably in the range of from 30 to 80 g/ft ³ , more preferably in the range of from 40 to 80 g/ft ³ .

Preferably the non-zeolitic oxidic material comprised in the DOC coating (iii) comprises one or more of alumina, silica, zirconia and titania, more preferably one or more of alumina, silica and zirconia, more preferably alumina.

More preferably from 70 to 99 weight-%, more preferably from 80 to 98 weight-%, more prefer ably from 90 to 97 weight-%, more preferably from 92 to 97 weight-%, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of alumina. It is more preferred that from 1 to 30 weight-%, more preferably from 2 to 20 weight-%, more preferably from 3 to 10 weight-%, more preferably from 3 to 8 weight-%, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of silicon, calculated as S1O2.

Alternatively, preferably from 70 to 99 weight-%, preferably from 80 to 98 weight-%, more pref erably from 90 to 97 weight-%, more preferably from 92 to 97 weight-%, of the non-zeolitic oxi dic material comprised in the DOC coating (iii) consists of alumina, and more preferably wherein from 1 to 30 weight-%, more preferably from 2 to 20 weight-%, more preferably from 3 to 10 weight-%, more preferably from 3 to 8 weight-%, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of manganese, calculated as Mn0 ₂ .

Preferably the DOC coating (iii) further comprises a zeolitic material comprising one or more of iron and copper, preferably a zeolitic material comprising iron. More preferably the DOC coat ing (iii) comprises iron in an amount, calculated as Fe203, in the range of from 1 to 10 weight-%, more preferably in the range of from 2 to 8 weight-%, more preferably in the range of from 3 to 5 weight-%, based on the weight of the zeolitic material comprising iron comprised in the DOC coating (iii). Alternatively, preferably the DOC coating (iii) further comprises a zeolitic material in its H-form. This means in the context of the present invention that the zeolitic material is not ion-exchanged with a metal, such as Cu or Fe.

In the context of the present invention, it is preferred that the zeolitic material comprised in the DOC coating (iii) is a 12-membered ring pore zeolitic material, wherein said zeolitic material more preferably has a framework type selected from the group consisting of BEA, MOR, FAU, GME, OFF a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of BEA, MOR, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group con sisting of BEA and FAU. It is more preferred that the 12-membered ring pore zeolitic material comprised in the DOC coating (iii) has a framework type BEA.

Preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the framework struc ture of the 12-membered ring pore zeolitic material comprised in the DOC coating (iii) consist of Si, Al, and O. In the framework structure of the 12-membered ring pore zeolitic material com prised in the DOC coating (iii), the molar ratio of Si to Al, calculated as molar Si02:Al203, is preferably in the range of from 2:1 to 60:1, more preferably in the range of from 2:1 to 50:1, more preferably in the range of from 5:1 to 40:1, more preferably in the range of from 10:1 to 35:1, more preferably in the range of from 15:1 to 30:1, more preferably in the range of from 20:1 to 27:1.

Preferably the weight ratio of the non-zeolitic oxidic material comprised in the DOC coating (iii) relative to the zeolitic material comprised in the DOC coating (iii) is in the range of from 1.5:1 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 6:1 , more preferably in the range of from 3:1 to 5:1.

Preferably the DOC coating (iii) comprises the non-zeolitic oxidic material in an amount in the range of from 0.75 to 3 g/in ³ , more preferably in the range of from 1 to 2 g/in ³ .

Preferably the NA coating disposed on the surface of the internal walls of the substrate (i) ex tends over x % of the substrate axial length, more preferably from the outlet end towards the inlet end, with x being in the range of from 40 to 100.

It is preferred thatx is in the range of from 98 to 100, more preferably in the range of from 99 to 100.

Preferably the DOC coating (iii) has a single coat.

Preferably the DOC coating extends over y % of the substrate axial length, more preferably from the inlet end towards the outlet end of the substrate, with y being in the range of from 20 to 100. It is more preferred that y is in the range of from 98 to 100, preferably in the range of from 99 to 100. It is more preferred that x is in the range of from 98 to 100, more preferably in the range of from 99 to 100, and that y is in the range of from 98 to 100, more preferably in the range of from 99 to 100.

Alternatively, it is preferred that x is in the range of from 40 to 60, more preferably in the range of from 45 to 55.

It is preferred that y is in the range of from 30 to 60, more preferably in the range of from 45 to 55, more preferably y = 100 - x. It is more preferred that x is in the range of from 40 to 60, more preferably in the range of from 45 to 55 and that y is in the range of from 30 to 60, more prefer ably in the range of from 45 to 55, more preferably y = 100 - x. Thus, in this configuration, the two coatings preferably do not overlap.

As to x, it is preferred that it is in the range of from 98 to 100, preferably in the range of from 99 to 100 and that y is in the range of from 20 to 40, preferably in the range of from 25 to 35.

As to x, it is preferred alternatively that it is in the range of from 40 to 90, preferably in the range of from 45 to 80.

It is preferred that y is in the range of from 50 to 100. It is more preferred that x is in the range of from 40 to 90, preferably in the range of from 45 to 80, and that y is in the range of from 50 to 100.

It is alternatively preferred that the DOC coating extends over y % of the substrate axial length from the outlet end towards the inlet end, with y being in the range of from 20 to 60, more pref erably in the range of from 20 to 40. More preferably x is in the range of from 98 to 100, more preferably in the range of from 99 to 100 and y is in the range of from 20 to 60, more preferably in the range of from 20 to 40. In this configuration, it is more preferred that the substrate accord ing to (i) is heated.

In the context of the present invention, the DOC coating (iii) preferably has a single coat.

Alternatively, it is preferred that the DOC coating (iii) comprises, more preferably consists of,

(111.1) an inlet coat comprising the platinum group metal, more preferably platinum, the non- zeolitic oxidic material and a zeolitic material as defined in the foregoing; and

(111.2) an outlet coat comprising the platinum group metal, more preferably platinum, and the non-zeolitic oxidic material; wherein the inlet coat (iii.1) extends over y1 % of the substrate axial length from the inlet end towards the outlet end of the substrate according to (i), wherein y1 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55, and wherein the outlet coat (iii.2) extends over y2 % of the substrate axial length from the outlet end towards the inlet end of the substrate according to (i), wherein y2 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55. It is preferred that the DOC coating extends over y % of the substrate axial length, more prefer ably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100.

In the context of the present invention, it is noted that the inlet coat and the outlet coat are dif ferent chemically and physically from one another. Indeed, this is obvious for the skilled person, as, should both coats be the same, they would not be distinguishable from one another.

Preferably the inlet coat (iii.1) is disposed on the NA coating, and the outlet coat (iii.2) is dis posed on the NA coating, wherein y2 is y - y1.

Preferably the inlet coat (iii.1) comprises, in addition to platinum, palladium, wherein the weight ratio of Pt to Pd, calculated as elemental Pt and Pd, respectively, more preferably is in the range of from 1:1 to 10:1, more preferably in the range of from 1.1 :1 to 8:1, more preferably in the range of from 1.5:1 to 4:1.

Preferably the inlet coat (iii.1) comprises platinum at a Pt loading, calculated as elemental Pt, and palladium at a Pd loading, calculated as elemental Pd, wherein the sum of the Pt loading and the Pd loading is in the range of from 5 to 40 g/ft ³ , more preferably in the range of from 10 to 30 g/ft ³ .

Preferably the weight ratio of the non-zeolitic oxidic material comprised in the inlet coat (iii.1) relative to the zeolitic material comprised in the inlet coat (iii.1) is in the range of from 0.25:1 to 4:1 , more preferably in the range of from 0.5:1 to 2:1 , more preferably in the range of from 0.75:1 to 1.5:1.

Preferably the outlet coat (iii.2) comprises platinum at a loading, calculated as elemental Pt, in the range of from 50 to 100 g/ft ³ , more preferably in the range of from 70 to 90 g/ft ³ .

Thus, the present invention according to a certain aspect preferably relates to a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, the catalyst comprising:

(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 NOx adsorber (NA) coating disposed on the surface of the internal walls of the substrate (i), said coating comprising a platinum group metal, more preferably palladium, a zeolitic material having a framework type FER or TON, more preferably FER, manganese and an alkaline earth metal, more preferably barium; (iii) a diesel oxidation catalyst (DOC) coating, said coating comprising a platinum group metal supported on a non-zeolitic oxidic material; wherein the DOC coating (iii) comprises, more preferably consists of,

(111.1) an inlet coat comprising the platinum group metal, more preferably platinum, more preferably palladium is comprised in the inlet coat in addition to platinum, the non- zeolitic oxidic material and a zeolitic material as defined in the foregoing, more pref erably having a framework type BEA; and

(111.2) an outlet coat comprising the platinum group metal, more preferably platinum, and the non-zeolitic oxidic material; wherein the inlet coat (iii.1 ) extends over y1 % of the substrate axial length from the inlet end towards the outlet end of the substrate according to (i), wherein y1 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55, and wherein the outlet coat (iii.2) extends over y2 % of the substrate axial length from the out let end towards the inlet end of the substrate according to (i), wherein y2 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55.

It is more preferred that the DOC coating extends over y % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100 and that the N A coating extends over x % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100.

Further, the present invention according to a further aspect preferably relates to a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, the catalyst comprising:

(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 NOx adsorber (NA) coating disposed on the surface of the internal walls of the substrate (i), said coating comprising a platinum group metal, more preferably palladium, a zeolitic material having a framework type FER or TON, more preferably FER, the NA coating fur ther comprising manganese and an alkaline earth metal or an alkali metal, more preferably manga nese is used in addition to Ba, Sr or Na; or manganese and one or more of Ba and Sr, more preferably Mn, Ba and Sr; an alkaline earth metal, more preferably Ba or Sr;

(iii) a diesel oxidation catalyst (DOC) coating, said coating comprising a platinum group metal, more preferably platinum, supported on a non-zeolitic oxidic material, more preferably alumina, more preferably the DOC coating consists of one single coat.

It is more preferred that the DOC coating extends over y % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100 and that the N A coating extends over x % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100.

Further, the present invention according to a further aspect preferably relates to a NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, the catalyst comprising:

(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 NOx adsorber (NA) coating disposed on the surface of the internal walls of the substrate (i), said coating comprising a platinum group metal, more preferably palladium, a zeolitic material having a framework type FER or TON, more preferably FER, the NA coating fur ther comprising manganese; manganese and an alkaline earth metal, more preferably Ba; or an alkaline earth metal, more preferably Ba or Sr;

(iii) a diesel oxidation catalyst (DOC) coating, said coating comprising a platinum group metal supported on a non-zeolitic oxidic material; wherein the DOC coating (iii) comprises, more preferably consists of,

(111.1) an inlet coat comprising the platinum group metal, more preferably platinum, more preferably palladium is comprised in the inlet coat in addition to platinum, the non- zeolitic oxidic material and a zeolitic material as defined in the foregoing, more pref erably having a framework type BEA; and

(111.2) an outlet coat comprising the platinum group metal, more preferably platinum, and the non-zeolitic oxidic material; wherein the inlet coat (iii.1 ) extends over y1 % of the substrate axial length from the inlet end towards the outlet end of the substrate according to (i), wherein y1 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55, and wherein the outlet coat (iii.2) extends over y2 % of the substrate axial length from the out let end towards the inlet end of the substrate according to (i), wherein y2 is in the range of from 20 to 80, more preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55.

It is more preferred that the DOC coating extends over y % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100 and that the NA coating extends overx % of the substrate axial length, more preferably from the inlet end towards the outlet end, with y being in the range of from 98 to 100, more preferably in the range of from 99 to 100.

Preferably, in the context of the present invention, the flow-through substrate (i) comprises, more preferably consists of, a ceramic substance, wherein the ceramic substance more prefer ably comprises, more preferably consists of, one or more of an alumina, a silica, a silicate, an aluminosilicate, more preferably a cordierite or a mullite, an aluminotitanate, a silicon carbide, a zirconia, a magnesia, more preferably a spinel, and a titania, more preferably one or more of a silicon carbide and a cordierite, more preferably a cordierite.

Alternatively, preferably the flow-through substrate (i) comprises, more preferably consists of, a metallic substance, wherein the metallic substance more preferably comprises, more preferably consists of, oxygen and one or more of iron, chromium and aluminum. Preferably the substrate is electrically heated.

Preferably the catalyst of the present invention consists of the substrate (i), the NA coating (ii) and the DOC coating (iii).

The present invention further relates to a process for preparing a NOx adsorber diesel oxidation catalyst (NA-DOC), preferably the NOx adsorber diesel oxidation catalyst (NA-DOC) according to the present invention and as defined in the foregoing, comprising

(a) preparing a first mixture comprising water, a source of a platinum group metal, a zeolitic material and a source of one or more of an alkaline earth metal and manganese;

(b) disposing the first mixture obtained according to (a) on the surface of the internal walls of 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 NA coating thereon;

(c) preparing a second mixture comprising water, a source of a platinum group metal and a non-zeolitic oxidic material;

(d) disposing the second mixture obtained according to (c) on the substrate having a NA coat ing thereon;

(e) calcining the substrate obtained according to (d), obtaining a substrate having a NA coat ing and a DOC coating thereon.

As to (a), it is preferred that it comprises

(a.1) admixing, more preferably impregnating, the zeolitic material, more preferably in its am monium form, with the source of a platinum group metal, more preferably a source of pal ladium, more preferably palladium nitrate, and the source of one or more of an alkaline earth metal and manganese;

(a.2) dispersing the admixed zeolitic material in water;

(a.3) more preferably adding a precursor of a non-zeolitic oxidic material, more preferably a precursor of zirconium, more preferably zirconium acetate.

Preferably the source of the one or more of an alkaline earth metal and manganese is one or more of a nitrate, an acetate and an hydroxide, wherein more preferably the source of the one or more of an alkaline earth metal and manganese are selected from the group consisting of strontium acetate, strontium nitrate, barium hydroxide, barium nitrate, manganese nitrate, man ganese acetate, and a mixture of two or more thereof, more preferably selected from the group consisting of strontium acetate, barium hydroxide, barium nitrate, manganese nitrate and a mix ture of two or more thereof.

Preferably disposing the first mixture in (b) comprises disposing the first mixture obtained in (a) from the outlet end towards to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 40 to 100; wherein more preferably x is in the range of from 98 to 100, more preferably in the range of from 99 to 100; or wherein more preferably x is in the range of from 40 to 90, more preferably in the range of from 45 to 80.

Preferably calcining according to (b) 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 pref erably 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.

Preferably calcining according to (b) 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 1.5 to 2.5 hours, the gas at mosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air. Preferably, prior to calcining according to (b), drying of the coated 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.

Preferably, prior to calcining according to (b), drying of the coated 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.

Preferably (c) comprises

(c.1) admixing, preferably impregnating, a non-zeolitic oxidic material, preferably as defined in the foregoing, with a source of a platinum group metal;

(c.2) dispersing the admixed, more preferably impregnated, non-zeolitic oxidic material in wa ter.

More preferably (c) further comprises

(c.3) admixing a zeolitic material comprising one or more of iron and copper, preferably a zeolit- ic material comprising iron, to the dispersion obtained according to (c.2), obtaining the second mixture, wherein the zeolitic material preferably is as defined in the foregoing.

Preferably disposing the second mixture in (d) comprises disposing the second mixture ob tained in (c) from the inlet end towards to the outlet end of the substrate over y % of the sub strate axial length, wherein y is in the range of from 20 to 100; wherein more preferably y is in the range of from 98 to 100, preferably in the range of from 99 to 100; or wherein y is in the range of from 30 to 60, more preferably in the range of from 45 to 55, more preferably y = 100 - x. It is also conceivable that the second mixture obtained in (c) be preferably disposed from the outlet end towards the inlet end of the substrate.

Preferably disposing the second mixture in (d) comprises disposing the second mixture ob tained in (c) from the inlet end towards to the outlet end of the substrate over y1 % of the sub strate axial length, wherein y1 is in the range of from 20 to 80, more preferably from 30 to 60, more preferably from 45 to 55.

Preferably (d) further comprising, prior to calcining according to (e),

- preparing a third mixture comprising water and a source of a platinum group metal and a non- zeolitic oxidic material;

- disposing the third mixture on the substrate from the outlet end towards to the inlet end of the substrate over y2 % of the substrate axial length, wherein y2 is in the range of from 20 to 80, more preferably from 30 to 60, more preferably from 45 to 55, more preferably y2 is 100 - y1 , and optionally drying.

Preferably calcining according to (e) 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 pref erably 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.

Preferably calcining according to (e) 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 1.5 to 2.5 hours, the gas at mosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

Preferably, prior to calcining according to (e), drying of the coated 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.

Preferably, prior to calcining according to (e), drying of the coated 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.

Preferably the process consists of (a), (b), (c), (d) and (e).

The present invention further relates to a NOx adsorber diesel oxidation catalyst (NA-DOC), preferably the NA-DOC catalyst according to the present invention and as defined in the forego ing, obtained or obtainable by a process according to the present invention and as defined in the foregoing. The present invention further relates to a use of a N Ox adsorber diesel oxidation catalyst (NA- DOC) according to the present invention and as defined in the foregoing for the NOx adsorp tion/desorption and the conversion of HC and CO.

The present invention further relates to an exhaust treatment system for the treatment of an exhaust gas, the system comprising a NOx adsorber diesel oxidation (NA-DOC) catalyst according to the present invention and as defined in the foregoing ; the system preferably further comprises one or more of a selective catalytic reduction cat alyst (SCR), a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxida tion (AM OX) catalyst, wherein the NA-DOC catalyst is preferably located upstream of the one or more of a selective catalytic reduction catalyst (SCR), a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxidation (AMOX) catalyst.

Preferably the system further comprises a selective catalytic reduction catalyst (SCR) and an ammonia oxidation (AMOX) catalyst, wherein the NA-DOC catalyst is located upstream of the selective catalytic reduction catalyst (SCR) and the SCR catalyst is located upstream of the ammonia oxidation (AMOX) catalyst, wherein more preferably no catalyst for treating the ex haust gas stream exiting the NA-DOC catalyst and upstream of the SCR catalyst is located in the exhaust gas treatment system.

Alternatively, preferably the system further comprises a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxidation (AMOX) catalyst, wherein the NA-DOC catalyst is located upstream of the selective catalytic reduction catalyst on a filter (SCRoF) and the SCRoF catalyst is located upstream of the ammonia oxidation (AMOX) catalyst, wherein more prefera bly no catalyst for treating the exhaust gas stream exiting the NA-DOC catalyst and upstream of the SCRoF catalyst is located in the exhaust gas treatment system.

Alternatively, preferably the system further comprises a selective catalytic reduction catalyst on a filter (SCRoF), a selective catalytic reduction catalyst (SCR) and an ammonia oxidation (AMOX) catalyst, wherein the NA-DOC catalyst is located upstream of the selective catalytic reduction catalyst on a filter (SCRoF), the SCRoF catalyst is located upstream of the SCR cata lyst, and the SCR catalyst is located upstream of the AMOX catalyst, wherein preferably no cat alyst for treating the exhaust gas stream exiting the NA-DOC catalyst and upstream of the SCRoF catalyst is located in the exhaust gas treatment system.

Preferably the system further comprises a first electrically heated substrate, wherein the NA- DOC catalyst is located downstream of said first electrically heated substrate.

Preferably the system further comprises a second electrically heated substrate, wherein the NA- DOC catalyst is located downstream of said second electrically heated substrate. The present invention further relates to a method for the treatment of an exhaust gas compris ing providing an exhaust gas, preferably from an internal combustion engine, more preferably from a diesel engine; contacting the exhaust gas with a NOx adsorber diesel oxidation catalyst according to the pre sent invention and as defined in the foregoing.

The present invention is further illustrated by the following set of embodiments and combina tions of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted in the context of the present invention, that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The catalyst of any one of embodiments 1 to 5", 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 "The catalyst of any one of embodiments 1, 2, 3, 4 and 5". 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 gen eral and preferred aspects of the present invention. It is noted that this is applicable as well for the second set of embodiments.

1. A NOx adsorber diesel oxidation catalyst (NA-DOC) for the treatment of an exhaust gas, the catalyst comprising:

(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 NOx adsorber (NA) coating disposed on the surface of the internal walls of the substrate (i), said coating comprising a platinum group metal, a zeolitic material and one or more of an alkaline earth metal and manganese;

(iii) a diesel oxidation catalyst (DOC) coating, said coating comprising a platinum group metal supported on a non-zeolitic oxidic material.

2. The catalyst of embodiment 1 , wherein the platinum group metal comprised in the NA coating (ii) is selected from the group consisting of palladium, platinum, rhodium, iridium, osmium, ruthenium and a mixture of two or more thereof, preferably selected from the group consisting of palladium, platinum and rhodium, more preferably selected from the group consisting of palladium and platinum, more preferably is palladium.

3. The catalyst of embodiment 1 or 2, wherein the NA coating (ii) comprises the platinum group metal at a loading, calculated as elemental platinum group metal, in the range of from 1 to 150 g/ft ³ , preferably in the range of from 5 to 100 g/ft ³ , more preferably in the range of from 10 to 90 g/ft ³ , more preferably in the range of from 15 to 80 g/ft ³ , more pref erably in the range of from 15 to 40 g/ft ³ , or more preferably in the range of from 50 to 80 g/ft ³ . 4. The catalyst of any one of embodiments 1 to 3, wherein the zeolitic material comprised in the NA coating (ii) is a 10-membrered ring pore zeolitic material, wherein the 10- membered ring pore zeolitic material preferably has framework type selected from the group consisting of FER, TON, MTT, SZR, MFI, MWW, AEL, H EU , 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, 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 comprised in the NA coating (ii) has a framework type FER.

5. The catalyst of embodiment 4, wherein from 95 to 100 weight-%, preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the framework structure of the 10-membered ring pore zeolitic material com prised in the NA coating (ii) consist of Si, Al, and O, wherein in the framework structure, the molar ratio of Si to Al, calculated as molar SiC^A Ch, is more preferably in the range of from 2:1 to 60:1 , more preferably in the range of from 2:1 to 50:1 , more preferably in the range of from 5:1 to 40:1, more preferably in the range of from 10:1 to 35:1, more prefera bly in the range of from 15:1 to 30:1, more preferably in the range of from 18:1 to 25:1.

6. The catalyst of any one of embodiments 1 to 5, wherein the NA coating (ii) comprises the zeolitic material in an amount in the range of from 0.5 to 5 g/in ³ , preferably in the range of from 1 to 4 g/in ³ , more preferably in the range of from 1.25 to 3 g/in ³ .

7. The catalyst of any one of embodiments 1 to 6, wherein the NA coating (ii) comprises an alkaline earth metal, wherein the alkaline earth metal is preferably selected from the group consisting of barium, strontium, calcium and magnesium, more preferably selected from the group consisting of barium, strontium and magnesium, more preferably is barium or strontium; or wherein the alkaline earth metal is barium and strontium, wherein more preferably the ra tio of the weight of Ba, calculated as the oxide, relative to the weight of Sr, calculated as the oxide, 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 3:1 to 6:1.

8. The catalyst of any one of embodiments 1 to 7, wherein the NA coating (ii) comprises the alkaline earth metal in a total amount, calculated as the oxide, in the range of from 0.5 to 15 weight-%, preferably in the range of from 1 to 10 weight-%, more preferably in the range of from 1.5 to 8 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii).

9. The catalyst of any one of embodiments 1 to 8, wherein the N A coating (ii) further com prises a non-zeolitic oxidic material, wherein the non-zeolitic oxidic material is selected from the group consisting of zirconia, alumina, silica, titania, ceria, a mixed oxide compris ing one or more of Zr, Al, Si, Ti, and Ce and a mixture of two or more thereof, preferably selected from the group consisting of zirconia, alumina, ceria and titania, more preferably selected from the group consisting of zirconia, alumina and ceria, more preferably is zir conia.

10. The catalyst of embodiment 10, wherein the NA coating (ii) comprises the non-zeolitic oxidic material in an amount in the range of from 1 to 30 weight-%, preferably in the range of from 2 to 25 weight-%, more preferably in the range of from 4 to 21 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii).

11. The catalyst of any one of embodiments 1 to 10, wherein the N A coating (ii) comprises manganese, wherein the NA coating (ii) preferably comprises manganese in an amount calculated as MnC>2, in the range of from 0.25 to 5 weight-%, more preferably in the range of from 0.5 to 3 weight-%, more preferably in the range of from 0.75 to 1.5 weight-% based on the weight of the zeolitic material comprised in the NA coating (ii).

12. The catalyst of any one of embodiments 7 to 11 , wherein the NA coating (ii) comprises barium and manganese.

13. The catalyst of any one of embodiments 7 to 11 , wherein the N A coating (ii) comprises strontium and manganese.

14. The catalyst of any one of embodiments 11 to 13, wherein the N A coating (ii) further com prises an alkali metal, wherein the alkali metal is preferably selected from the group con sisting of sodium, potassium and lithium, wherein the alkali metal is preferably sodium.

15. The catalyst of embodiment 14, wherein the N A coating (ii) comprises the alkali metal in an amount, calculated as the oxide, in the range of from 0.1 to 4 weight-%, more prefera bly in the range of from 0.25 to 3 weight-%, more preferably in the range of from 0.5 to 2 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii); wherein the NA coating (ii) preferably comprises sodium in an amount, calculated as NaO, in the range of from 0.1 to 4 weight-%, more preferably in the range of from 0.25 to 3 weight-%, more preferably in the range of from 0.5 to 2 weight-%, more preferably in the range of from 0.5 to 1 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii) or wherein the NA coating (ii) preferably comprises potassium in an amount, calculated as K2O, in the range of from 0.1 to 4 weight-%, more preferably in the range of from 0.25 to 3 weight-%, more preferably in the range of from 0.5 to 2 weight-%, more preferably in the range of from 1.2 to 2 weight-%, based on the weight of the zeolitic material comprised in the NA coating (ii).

16. The catalyst of any one of embodiments 1 to 10, wherein the NA coating (ii) further com prises one or more of Nd, La, Ce, Pr, Sm, Y and Yb, preferably one or more of Nd and Pr, more preferably Nd, wherein the NA coating (ii) preferably comprises the one or more of Nd, La, Ce, Pr, Sm, Y and Yb, in an amount, calculated as the oxide, in the range of from 2 to 6 weight-%, more preferably in the range of from 3 to 5 weight-%, more preferably in the range of from 4 to 5 weight-% based on the weight of the zeolitic material comprised in the NA coating (ii).

17. The catalyst of any one of embodiments 1 to 10, wherein from 99 to 100 weight-%, pref erably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, barium, and preferably a non-zeolitic oxidic ma terial as defined in embodiment 9 or 10.

18. The catalyst of any one of embodiments 1 to 10, wherein from 99 to 100 weight-%, pref erably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, strontium and preferably a non-zeolitic oxidic material as defined in embodiment 9 or 10.

19. The catalyst of any one of embodiments 1 to 13, wherein from 99 to 100 weight-%, pref erably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, manganese, an alkaline earth metal, preferably barium or strontium, and preferably a non-zeolitic oxidic material as defined in embodi ment 9 or 10; or wherein from 99 to 100 weight-%, preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, man ganese, barium, strontium, and preferably a non-zeolitic oxidic material as defined in em bodiment 9 or 10.

20. The catalyst of any one of embodiments 1 to 11 , wherein from 99 to 100 weight-%, pref erably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, manganese, an alkali metal, preferably sodium, as defined in embodiment 14 or 15, and preferably a non-zeolitic oxidic material as de fined in embodiment 9 or 10.

21. The catalyst of any one of embodiments 1 to 8 and 13, wherein from 99 to 100 weight-%, preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic ma terial, preferably having a framework type FER, an alkaline earth metal, preferably barium or strontium, and one or more of Nd, La, Ce, Pr, Sm, Y and Yb, and preferably a non- zeolitic oxidic material as defined in embodiment 9 or 10; or wherein from 99 to 100 weight-%, preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, bari um, strontium, and one or more of Nd, La, Ce, Pr, Sm, Y and Yb, and preferably a non- zeolitic oxidic material as defined in embodiment 9 or 10.

22. The catalyst of any one of embodiments 1 to 11 , wherein from 99 to 100 weight-%, pref erably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%, of the NA coating (ii) consists of the platinum group metal, preferably palladium, the zeolitic material, preferably having a framework type FER, manganese, and preferably a non-zeolitic oxidic material as defined in embodiment 9 or 10.

23. The catalyst of any one of embodiments 1 to 22, wherein the platinum group metal com prised in the DOC coating (iii) is selected from the group consisting of palladium, platinum, rhodium, iridium, osmium, ruthenium and a mixture of two or more thereof, preferably se lected from the group consisting of palladium, platinum and rhodium, more preferably se lected from the group consisting of palladium and platinum, more preferably is platinum.

24. The catalyst of any one of embodiments 1 to 23, wherein the DOC coating (iii) comprises the platinum group metal component at a loading, calculated as elemental platinum group metal, in the range of from 1 to 150 g/ft ³ , preferably in the range of from 10 to 100 g/ft ³ , more preferably in the range of from 20 to 90 g/ft ³ , more preferably in the range of from 30 to 80 g/ft ³ , more preferably in the range of from 40 to 80 g/ft ³ .

25. The catalyst of any one of embodiments 1 to 24, wherein the non-zeolitic oxidic material comprised in the DOC coating (iii) comprises one or more of alumina, silica, zirconia and titania, preferably one or more of alumina, silica and zirconia, more preferably alumina.

26. The catalyst of embodiment 25, wherein from 70 to 99 weight-%, preferably from 80 to 98 weight-%, more preferably from 90 to 97 weight-%, more preferably from 92 to 97 weight- %, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of alumi na, and preferably wherein from 1 to 30 weight-%, more preferably from 2 to 20 weight-%, more preferably from 3 to 10 weight-%, more preferably from 3 to 8 weight-%, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of silicon, calculated as S1O2.

27. The catalyst of embodiment 26, wherein from 70 to 99 weight-%, preferably from 80 to 98 weight-%, more preferably from 90 to 97 weight-%, more preferably from 92 to 97 weight- %, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of alumi na, and preferably wherein from 1 to 30 weight-%, more preferably from 2 to 20 weight-%, more preferably from 3 to 10 weight-%, more preferably from 3 to 8 weight-%, of the non-zeolitic oxidic material comprised in the DOC coating (iii) consists of manganese, calculated as Mn02.

28. The catalyst of any one of embodiments 1 to 27, wherein the DOC coating (iii) further comprises a zeolitic material comprising one or more of iron and copper, preferably a zeo- litic material comprising iron; wherein the DOC coating (iii) comprises iron in an amount, calculated as Fe203, in the range of from 1 to 10 weight-%, more preferably in the range of from 2 to 8 weight-%, more preferably in the range of from 3 to 5 weight-%, based on the weight of the zeolitic material comprising iron comprised in the DOC coating (iii).

29. The catalyst of embodiment 28, wherein the zeolitic material comprised in the DOC coat ing (iii) is a 12-membered ring pore zeolitic material, wherein said zeolitic material prefer ably has a framework type selected from the group consisting of BEA, MOR, FAU, GME, OFF a mixture of two or more thereof and a mixed type of two or more thereof, more pref erably selected from the group consisting of BEA, MOR, FAU, a mixture of two or more thereof and a mixed type of two or more thereof, more preferably selected from the group consisting of BEA and FAU, wherein more preferably the 12-membered ring pore zeolitic material comprised in the DOC coating (iii) has a framework type BEA.

30. The catalyst of embodiment 29, wherein from 95 to 100 weight-%, preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of the framework structure of the 12-membered ring pore zeolitic material com prised in the DOC coating (iii) consist of Si, Al, and O, wherein in the framework structure, the molar ratio of Si to Al, calculated as molar Si02:Al203, is more preferably in the range of from 2:1 to 60:1 , more preferably in the range of from 2:1 to 50:1 , more preferably in the range of from 5:1 to 40:1, more preferably in the range of from 10:1 to 35:1, more prefera bly in the range of from 15:1 to 30:1, more preferably in the range of from 20:1 to 27:1.

31. The catalyst of any one of embodiments 1 to 30, wherein the NA coating disposed on the surface of the internal walls of the substrate (i) extends overx % of the substrate axial length, preferably from the outlet end towards the inlet end, with x being in the range of from 40 to 100.

32. The catalyst of any one of embodiments 1 to 31 , wherein the DOC coating extends over y % of the substrate axial length from the inlet end towards the outlet end, with y being in the range of from 20 to 100.

33. The catalyst of embodiment 32, as far as it depends on embodiment 34, wherein x is in the range of from 98 to 100, preferably in the range of from 99 to 100.

34. The catalyst of embodiment 32 or 33, as far as it depends on embodiment 34, wherein y is in the range of from 98 to 100, preferably in the range of from 99 to 100. 35. The catalyst of any one of embodiments 1 to 34, wherein the DOC coating (iii) has a sin gle coat.

36. The catalyst of embodiment 35, wherein the weight ratio of the non-zeolitic oxidic material comprised in the DOC coating (iii) relative to the zeolitic material comprised in the DOC coating (iii) is in the range of from 1.5:1 to 10:1, preferably in the range of from 2:1 to 8:1, more preferably in the range of from 2.5:1 to 6:1, more preferably in the range of from 3:1 to 5:1.

37. The catalyst of embodiment 35 or 36, wherein the DOC coating (iii) comprises the non- zeolitic oxidic material in an amount in the range of from 0.75 to 3 g/in ³ , preferably in the range of from 1 to 2 g/in ³ .

38. The catalyst of any one of embodiments 1 to 34, wherein the DOC coating (iii) comprises, preferably consists of,

(111.1) an inlet coat comprising the platinum group metal, preferably platinum, the non- zeolitic oxidic material and a zeolitic material as defined in any one of embodiments 28 to 30; and

(111.2) an outlet coat comprising the platinum group metal, preferably platinum, and the non-zeolitic oxidic material; wherein the inlet coat (iii.1) extends over y1 % of the substrate axial length from the inlet end towards the outlet end of the substrate according to (i), wherein y1 is in the range of from 20 to 80, preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55, and wherein the outlet coat (iii.2) extends over y2 % of the substrate axial length from the out let end towards the inlet end of the substrate according to (i), wherein y2 is in the range of from 20 to 80, preferably in the range of from 30 to 60, more preferably in the range of from 45 to 55.

39. The catalyst of embodiment 38, as far as it depends on embodiment 35 or 37, wherein the inlet coat (iii.1) is disposed on the NA coating, and wherein the outlet coat (iii.2) is disposed on the NA coating, wherein y2 is y - y1.

40. The catalyst of embodiment 38 or 39, wherein the inlet coat (iii.1 ) comprises, in addition to platinum, palladium, wherein the weight ratio of Pt to Pd, calculated as elemental Pt and Pd, respectively, preferably is in the range of from 1 :1 to 10:1, more preferably in the range of from 1.1 :1 to 8:1, more preferably in the range of from 1.5:1 to 4:1.

41. The catalyst of embodiment 40, wherein the inlet coat (iii.1) comprises platinum at a Pt loading, calculated as elemental Pt, and palladium at a Pd loading, calculated as ele mental Pd, wherein the sum of the Pt loading and the Pd loading is in the range of from 5 to 40 g/ft ³ , preferably in the range of from 10 to 30 g/ft ³ . 42. The catalyst of any one of embodiments 38 to 41 , wherein the weight ratio of the non- zeolitic oxidic material comprised in the inlet coat (iii.1) relative to the zeolitic material comprised in the inlet coat (iii.1) is in the range of from 0.25:1 to 4:1, preferably in the range of from 0.5:1 to 2:1, more preferably in the range of from 0.75:1 to 1.5:1.

43. The catalyst of any one of embodiments 38 to 42, wherein the outlet coat (iii.2) comprises platinum at a loading, calculated as elemental Pt, in the range of from 50 to 100 g/ft ³ , preferably in the range of from 70 to 90 g/ft ³ .

44. The catalyst of embodiment 32, as far as it depends on embodiment 31 , wherein x is in the range of from 40 to 60, preferably in the range of from 45 to 55.

45. The catalyst of embodiment 32 or 44, as far as it depends on embodiment 31 , wherein y is in the range of from 30 to 60, more preferably in the range of from 45 to 55, more prefera bly y = 100 - x.

46. The catalyst of embodiment 32, as far as it depends on embodiment 31 , wherein x is in the range of from 98 to 100, preferably in the range of from 99 to 100 and wherein y is in the range of from 20 to 40, preferably in the range of from 25 to 35.

47. The catalyst of embodiment 32, as far as it depends on embodiment 31 , wherein x is in the range of from 40 to 90, preferably in the range of from 45 to 80.

48. The catalyst of embodiment 32 or 47, as far as it depends on embodiment 34, wherein y is in the range of from 50 to 100.

49. The catalyst of any one of embodiments 1 to 32 and 35 to 37, wherein the DOC coating extends over y % of the substrate axial length from the outlet end towards the inlet end, with y being in the range of from 20 to 60, preferably in the range of from 20 to 40; wherein preferably x is in the range of from 98 to 100, preferably in the range of from 99 to 100 and y is in the range of from 20 to 60, preferably in the range of from 20 to 40.

50. The catalyst of any one of embodiments 1 to 49, wherein the substrate (i) is a flow through substrate or a wall-flow filter substrate, preferably a flow-through substrate.

51. The catalyst of embodiment 50, wherein the flow-through substrate (i) comprises, prefera bly consists of, a ceramic substance, wherein the ceramic substance preferably compris es, more preferably consists of, one or more of an alumina, a silica, a silicate, an alumino silicate, preferably a cordierite or a mullite, an aluminotitanate, a silicon carbide, a zirco- nia, a magnesia, preferably a spinel, and a titania, more preferably one or more of a sili con carbide and a cordierite, more preferably a cordierite; or wherein the flow-through substrate (i) comprises, preferably consists of, a metallic sub stance, wherein the metallic substance preferably comprises, more preferably consists of, oxygen and one or more of iron, chromium and aluminum; wherein the substrate is preferably electrically heated. The catalyst of any one of embodiments 1 to 51 , consisting of the substrate (i) the NA coating (ii) and the DOC coating (iii). Process for preparing a NOx adsorber diesel oxidation catalyst (NA-DOC), preferably ac cording to any one of embodiments 1 to 52, comprising

(a) preparing a first mixture comprising water, a source of a platinum group metal, a ze- olitic material and a source of one or more of an alkaline earth metal and manga nese;

(b) disposing the first mixture obtained according to (a) on the surface of the internal walls of 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 sub strate having a NA coating thereon;

(c) preparing a second mixture comprising water, a source of a platinum group metal and a non-zeolitic oxidic material;

(d) disposing the second mixture obtained according to (c) on the substrate having a NA coating thereon;

(e) calcining the substrate obtained according to (d), obtaining a substrate having a NA coating and a DOC coating thereon. The process of embodiment 53, wherein (a) comprises

(a.1) admixing, preferably impregnating, the zeolitic material, preferably in its ammonium form, with the source of a platinum group metal, preferably a source of palladium, more preferably palladium nitrate, and the source of one or more of an alkaline earth metal and manganese;

(a.2) dispersing the admixed zeolitic material in water;

(a.3) preferably adding a precursor of a non-zeolitic oxidic material, more preferably a precursor of zirconium, more preferably zirconium acetate. The process of embodiment 53 or 54, wherein the source of the one or more of an alka line earth metal and manganese is one or more of a nitrate, an acetate and an hydroxide, wherein preferably the source of the one or more of an alkaline earth metal and manga nese are selected from the group consisting of strontium acetate, strontium nitrate, barium hydroxide, barium nitrate, manganese nitrate, manganese acetate, and a mixture of two or more thereof, more preferably selected from the group consisting of strontium acetate, barium hydroxide, barium nitrate, manganese nitrate and a mixture of two or more thereof. The process of any one of embodiments 53 to 55, wherein disposing the first mixture in (b) comprises disposing the first mixture obtained in (a) from the outlet end towards to the inlet end of the substrate over x % of the substrate axial length, wherein x is in the range of from 98 to 100, preferably in the range of from 99 to 100; or wherein x is in the range of from 40 to 90, preferably in the range of from 45 to 80.

57. The process of any one of embodiments 53 to 56, wherein calcining according to (b) 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 more preferably comprising one or more of oxygen and nitro gen, more preferably air.

58. The process of any one of embodiments 53 to 57, wherein calcining according to (b) is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, prefera bly in the range of from 1.5 to 2.5 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

59. The process of any one of embodiments 53 to 58, wherein, prior to calcining according to (b), drying of the coated substrate 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 more preferably being air.

60. The process of any one of embodiments 53 to 59, wherein, prior to calcining according to (b), drying of the coated substrate 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 at mosphere more preferably comprising one or more of oxygen and nitrogen, more prefera bly air.

61. The process of any one of embodiments 53 to 60, wherein (c) comprises

(c.1) admixing, preferably impregnating, a non-zeolitic oxidic material, preferably as de fined in any one of embodiments 25 to 27, with a source of a platinum group metal; (c.2) dispersing the admixed, preferably impregnated, non-zeolitic oxidic material in wa ter.

62. The process of embodiment 61 , wherein (c) further comprises

(c.3) admixing a zeolitic material comprising one or more of iron and copper, preferably a zeolitic material comprising iron, to the dispersion obtained according to (c.2), ob taining the second mixture, wherein the zeolitic material preferably is as defined in embodiment 29 or 30.

63. The process of any one of embodiments 53 to 62, wherein disposing the second mixture in (d) comprises disposing the second mixture obtained in (c) from the inlet end towards to the outlet end of the substrate over y % of the substrate axial length, wherein y is in the range of from 98 to 100, preferably in the range of from 99 to 100 or wherein y is in the range of from 30 to 60, more preferably in the range of from 45 to 55, more preferably y = 100 - x.

64. The process of any one of embodiments 53 to 63, wherein disposing the second mixture in (d) comprises disposing the second mixture obtained in (c) from the inlet end towards to the outlet end of the substrate over y1 % of the substrate axial length, wherein y1 is in the range of from 20 to 80, preferably from 30 to 60, more preferably from 45 to 55.

65. The process of embodiment 64, wherein (d) further comprising, prior to calcining accord ing to (e),

- preparing a third mixture comprising water and a source of a platinum group metal and a non-zeolitic oxidic material;

- disposing the third mixture on the substrate from the outlet end towards to the inlet end of the substrate over y2 % of the substrate axial length, wherein y2 is in the range of from 20 to 80, preferably from 30 to 60, more preferably from 45 to 55, more preferably y2 is

100 - y1 , and optionally drying.

66. The process of any one of embodiments 53 to 65, wherein calcining according to (e) 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 more preferably comprising one or more of oxygen and nitro gen, more preferably air.

67. The process of any one of embodiments 53 to 66, wherein calcining according to (e) is performed in a gas atmosphere for a duration in the range of from 0.5 to 5 hours, prefera bly in the range of from 1.5 to 2.5 hours, the gas atmosphere more preferably comprising one or more of oxygen and nitrogen, more preferably air.

68. The process of any one of embodiments 53 to 67, wherein, prior to calcining according to (e), drying of the coated substrate 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 more preferably being air.

69. The process of any one of embodiments 53 to 68, wherein prior to calcining according to (e), drying of the coated substrate 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 at mosphere more preferably comprising one or more of oxygen and nitrogen, more prefera bly air.

70. The process of any one of embodiments 53 to 69 consisting of (a), (b), (c), (d) and (e).

71. A NOx adsorber diesel oxidation catalyst (NA-DOC) obtained or obtainable by a process according to any one of embodiments 53 to 70. 72. Use of a NOx adsorber diesel oxidation catalyst (NA-DOC) according to any one of em bodiments 1 to 52 and 71 for the NOx adsorption/desorption and the conversion of HC and CO.

73. An exhaust treatment system for the treatment of an exhaust gas, the system comprising a NOx adsorber diesel oxidation (NA-DOC) catalyst according to any one of embodiments 1 to 52 and 71 ; the system preferably further comprises one or more of a selective catalytic reduction cat alyst (SCR), a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxidation (AM OX) catalyst, wherein the NA-DOC catalyst is preferably located upstream of the one or more of a se lective catalytic reduction catalyst (SCR), a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxidation (AMOX) catalyst.

74. The system of embodiment 73, wherein the system further comprises a selective catalytic reduction catalyst (SCR) and an ammonia oxidation (AMOX) catalyst, wherein the NA- DOC catalyst is located upstream of the selective catalytic reduction catalyst (SCR) and the SCR catalyst is located upstream of the ammonia oxidation (AMOX) catalyst, wherein preferably no catalyst for treating the exhaust gas stream exiting the NA-DOC catalyst and upstream of the SCR catalyst is located in the exhaust gas treatment system.

75. The system of embodiment 73, wherein the system further comprises a selective catalytic reduction catalyst on a filter (SCRoF) and an ammonia oxidation (AMOX) catalyst, where in the NA-DOC catalyst is located upstream of the selective catalytic reduction catalyst on a filter (SCRoF) and the SCRoF catalyst is located upstream of the ammonia oxidation (AMOX) catalyst, wherein preferably no catalyst for treating the exhaust gas stream exit ing the NA-DOC catalyst and upstream of the SCRoF catalyst is located in the exhaust gas treatment system.

76. The system of embodiment 73, wherein the system further comprises a selective catalytic reduction catalyst on a filter (SCRoF), a selective catalytic reduction catalyst (SCR) and an ammonia oxidation (AMOX) catalyst, wherein the NA-DOC catalyst is located upstream of the selective catalytic reduction catalyst on a filter (SCRoF), the SCRoF catalyst is lo cated upstream of the SCR catalyst, and the SCR catalyst is located upstream of the AMOX catalyst, wherein preferably no catalyst for treating the exhaust gas stream exiting the NA-DOC catalyst and upstream of the SCRoF catalyst is located in the exhaust gas treatment system.

77. The system of embodiment 73, wherein the system further comprises a first electrically heated substrate, wherein the NA-DOC catalyst is located downstream of said first electri cally heated substrate. 78. The system of embodiment 77, wherein the system further comprises a second electrically heated substrate, wherein the NA-DOC catalyst is located downstream of said second electrically heated substrate.

79. A method for the treatment of an exhaust gas 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 diesel oxidation catalyst according to any one of embodiments 1 to 52 and 71 .

In the context of the present invention, the term “loading of a given component/coating”

(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 cross-section 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 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 coating per x % of the volume (in in ³ ) of the entire substrate.

Further, 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.

Furthermore, 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 fea ture, 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 con crete 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 fea ture, 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.

In the context of the present invention, the alkaline earth metal in the NA coating is preferably present as oxide, cation and/or carbonate.

The present invention is further illustrated by the following 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 Sym- patec HELOS 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 crystallinity

The determination of the relative crystallinity of a zeolite was performed via x-ray diffraction us ing 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.

Comparative Example 1 : Preparation of a NOx adsorber diesel oxidation catalyst - FER

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al203 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 0.8 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 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 slur ry 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 concentra tion of palladium in the bottom coating was 20 g/ft ³ and the concentration of the FER in bottom coating loading was 1.5 g/in ³ . The loading of the bottom coating was 1.51 g/in ³ .

Top coating (DOC coating):

An alumina support material comprising 5% by weight S1O2 was impregnated with platinum via a wet impregnation process. A Fe-Beta zeolitic material (a zeolitic material having framework structure type BEA, a SiC^A Ch 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 ma terial) was added to the Pt-alumina slurry. The weight ratio of the alumina doped with Si to the Beta zeolitic material was of 4.2/1. A slurry containing this material and Beta zeolite was coated over 100% of the cordierite substrate containing already the Pd/FER bottom layer. The coated substrate was dried in air at 120°C for 60 min and calcined in air at 590°C °C for 2 hours. The top layer contained 60 g/ft ³ platinum. The loading of the top coating was 1.9 g/in ³ .

Examples 1 to 3: Preparation of a NOx-adsorber Diesel oxidation catalyst - FER with Ba additive

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al2C>3 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution and barium hydroxide to attain a Pd loading of 0.77 weight-% based on the weight of the final material (zeolitic material + palladium) and the following weight-% based Ba loadings:

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 flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, core with diameter: 1 inch x length: 3 inches), was coated with the ob tained slurry over 100 % of the substrate axial length. The coated substrate was dried in air hav ing 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 20 g/ft ³ and the con centration of the FER in bottom coating loading was 1.5 g/in ³ . The loading of the bottom coating was 1.61 g/in ³ (Ex. 1), 1.64 g/in ³ (Ex. 2) and 1.69 g/in ³ (Ex. 3).

Top coating (DOC coating):

The slurries for preparing the top coating of Examples 1-3 were prepared as the slurry for pre paring the top coating of Comparative Example 1. The slurry for each of Examples 1-3 was coated over 100% of the cordierite substrate containing already the Ba/Pd/FER bottom coating. The top coating contained 60 g/ft ³ platinum. The loading of the top coating was 1.9 g/in ³ .

Examples 4 to 6: Preparation of a NOx-adsorber Diesel oxidation catalyst - FER with Sr additive Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si0 ₂ :Al ₂ 0 ₃ molar ratio of 21:1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution and strontium acetate to attain a Pd loading of 0.77 weight- % based on the weight of the final material (zeolitic material + palladi- um)and the following Sr content:

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 Zr0 ₂ , was 5 weight- % based on the weight of the zeolitic material.

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 slur ry over 100 % of the substrate axial length. The coated substrate was dried in air having a tem perature 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 20 g/ft ³ and the concentration of the FER in bottom coating loading was 1.5 g/in ³ . The loading of the bottom coating was 1.61 g/in ³ (Ex. 4), 1.64 g/in ³ (Ex. 5) and 1.69 g/in ³ (Ex. 6).

Top coating (DOC coating): The slurries for preparing the top coating of Examples 4-6 were prepared as the slurry for pre paring the top coating of Comparative Example 1. The slurry for each of Examples 1-3 was coated over 100% of the cordierite substrate containing already the Sr/Pd/FER bottom coating. The top coating contained 60 g/ft ³ platinum. The loading of the top coating was 1.9 g/in ³ . Table 1

Example 7: Evaluation of N Ox-adsorber Diesel oxidation catalyst of Comparative Example

1 and of Examples 2 to 6 on a Lab Reactor

The catalysts of Examples 2 to 6 and of Comparative Example 1 were tested for NOx adsorp tion and desorption performance after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to desorption, the cores were exposed to a mixture of 200 ppm nitric oxide (NO), 500 ppm carbon monoxide (CO), 500 ppm propylene (C ₃ H ₆ , Ci basis), 7 % oxygen (0 ₂ ), 5% carbon dioxide (C0 ₂ ), 5 % water (H ₂ 0) and balance nitrogen (N ₂ ) for 15 minutes at 100 °C. During this period, NO was adsorbed to the Pd/FER. After the adsorption phase, the NO, CO and propylene were turned off and the temperature of the sample was raised to 500 °C at 60K/min. During this period, NO that was adsorbed to the Pd/FER was desorbed (desorption phase). The temperature of the NOx adsorption and the amount of desorbed NOx was evaluat ed. NO desorption curves for the Comparative Example 1 and Examples 2-6 as a function of temperature are shown in Figure 1. The amount of desorbed NOx is shown in Table 1.

Table 2 Amount of desorbed NOx for Comparative Example 1 and Examples 2-6

As may be taken from Figure 1 , namely the NOx desorption curves of the tested samples, it can be concluded that the additive Sr and Ba permit the desired increase of the NOx desorption temperature. Indeed, such additives permit to reduce the first peak desorption temperature (about 200 °C) and increase the second peak desorption temperature (about 300 °C).The high er the amount of the additive the higher the increase of the NOx desorption. It is noted that the increase of the additive can also result in a slight decrease in the adsorption capacity which can be seen in Table 1 but in any case the adsorption capacity obtained by the catalysts according to the present invention are good. The amount of desorbed NOx relates to the previously ad sorbed NOx at 100°C.

Comparative Example 2: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst - FER

Bottom coating (NA coating): An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al2C>3 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 coat ing. 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 AI ₂ O ₃ support material comprising 5 weight-% MnC>2 (AI ₂ O ₃ 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 pro cess. 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 S1O2 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>2:Al203 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 mate rial and Beta zeolite was coated over 50% of the substrate axial length from the inlet end to wards 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 8A: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst - FER with Mn additive

Bottom coating (NA coating): An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si02:Al203 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution and Manganese nitrate to attain a Pd loading of 1.48 weight-% based on the weight of the zeolitic material + palladium and 1 weight- % Mn0 ₂ loading based on the FER amount. 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 Zr0 ₂ , was 5 weight-% based on the weight of the zeolitic ma terial.

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 its 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 coat ing. The concentration of palladium in the bottom coating was 70 g/ft ³ and 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 about 2.927 g/in ³ .

Top coating (DOC coating):

The top coating of Example 8A was prepared as the top coating of Comparative Example 2 and covers the bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.355 g/in ³ .

Example 8: Preparation of high Pd containing a NOx-adsorber Diesel oxidation catalyst -

FER with Ba additive

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si02:Al203 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution and barium hydroxide to attain a Pd loading of 1.48 weight-% based on the weight of the final material (zeolitic material + palladium) and 6.8 weight-% BaO loading based on the FER amount. 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 Zr0 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 its 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 coat ing. 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 about 3.084 g/in ³ .

Top coating (DOC coating): The top coating of Example 8 was prepared as the top coating of Comparative Example 2 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.355 g/in ³ .

Example 9: Preparation of high Pd containing a NOx-adsorber Diesel oxidation catalyst -

FERwith Sr additive

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al2C>3 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution and strontium acetate to attain a Pd loading of 1.48 weight-% based on the weight of the final material zeolitic material + palladium) and 6.8 weight-% SrO loading based on the FER amount. 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 its 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 coat ing. 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 about 2.9 g/in ³ .

Top coating DOC(second coating):

The top coating of Example 9 was prepared as the top coating of Comparative Example 2 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.355 g/in ³ .

Example 10: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FERwith Mn and Ba additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al2C>3 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, Barium hydroxide and Manganese ni trate to attain a Pd loading of 1.48 weight-% based on the weight of the final material (zeolitic material + palladium), 4.3 weight-% BaO and 1 weight-% MnC>2 loading based on the FER amount. To the resulting slurry a zirconium acetate mixture was added. The amount of zirconi um 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 coat ing. 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 Zr0 ₂ was 0.135 g/in ³ . The loading of the bottom coating was 3.11 g/in ³ .

Top coating (DOC coating):

The top coating of Example 8 was prepared as the top coating of Comparative Example 2 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.355 g/in ³ .

Table 3

Example 11 : Evaluation of NOx adsorber Diesel oxidation catalyst Comparative Example 2 and Examples 8A, 8 to 10 on a Lab Reactor

Cores having a diameter of 1 inch and a length of 3 inches were drilled out from the coated substrates of Comparative Example 2, Examples 8A and 8 -10 to be tested on a Lab reactor. These cores 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 cores were ex posed 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/FER. After the adsorption phase, the NO, CO and propylene were turned off and the tem- perature of the sample was raised to 500 °C at 20 °C/min. During this period, NO that was ad sorbed to the P d/zeolite was desorbed (desorption phase). The temperature of NOx adsorption and the amount of desorbed NOx was evaluated. NO desorption curves for Comparative Exam- pie 2, Reference Example 2 and Examples 8 -10 as a function of temperature are shown in Fig ure 2. The amount of desorbed NOx is shown in Table 4. The amount of desorbed NOx relates to the previously adsorbed NOx at 100°C.

Table 4 Amount of desorbed NOx for Comparative Example 2, Examples 8A and 8-10

As may be taken from Figure 2, namely the NOx desorption curves, it can be concluded that the additive Mn, Sr and Ba as well as Ba + Mn cause the desired increase of the NOx desorption temperature also with high Pd loading. The optimum NOx desorption window is achieved for the Example 10, the combination of the additives Ba and Mn. The adsorption capacity is only slight ly reduced for Example 10.

Example 12: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FERwith Mn and Na additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si02:A 03 molar ratio of 21:1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, sodium nitrate and manganese nitrate to attain a Pd loading of 1.59 weight- % based on the weight of the final material (zeolitic materi al + palladium), 0.7 weight- % NaO and 1 weight- % MnO _å loading based on the FER amount. 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 0.04 L , 400 cpsi and 4 mil wall thickness, core of 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 at 110 °C for 1 h and subsequently calcined in air at 590 °C for 2 h, forming a bottom coat ing. The concentration of palladium in the bottom coating was 70 g/ft ³ , the concentration of the FER in bottom coating loading was 2.5 g/in ³ and of Zr0 ₂ was 0.125 g/in ³ . The loading of the bottom coating was 2.71 g/in ³ .

Top coating (DOC coating):

The top coating of Example 12 was prepared as the top coating of Example 1-3 and covers the aforementioned bottom coating over 100 % of the substrate axial length, except that the plati num loading was of 50 g/ft ³ . The total loading of the top coating was 1.9 g/in ³ . Example 13: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FER with Mn and Sr additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al2C>3 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, strontium acetate and manganese ni trate to attain a Pd loading of 1.59 weight-% based on the weight of the final material (zeolitic material + palladium), 3 weight-% SrO and 1 weight-% MnC>2 loading based on the FER amount. To the resulting slurry a zirconium acetate mixture was added. The amount of zirconi um 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 0.04 L, 400 cpsi and 4 mil wall thickness, core of 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 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 2.5g/in ³ and of ZrC>2 was 0.125 g/in ³ . The loading of the bottom coating was 2.76 g/in ³ .

Top coating (DOC coating):

The top coating of Example 13 was prepared as the top coating of Example 12 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ .

Example 14: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FER with Mn and Ba additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a SiC>2:Al203 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, barium hydroxide and manganese ni trate to attain a Pd loading of 1.59 weight-% based on the weight of the final material (zeolitic material + palladium), 4.3 weight-% BaO and 1 weight-% MnC>2 loading based on the FER amount. To the resulting slurry a zirconium acetate mixture was added. The amount of zirconi um acetate was calculated such that the amount of zirconia in the bottom coating, calculated as ZrC>2, was 20 weight-% based on the weight of the zeolitic material. A porous uncoated round flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, core of 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 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 2.2 g/in ³ and of Z1Ό2 was 0.44 g/in ³ . The loading of the bottom coating was 2.64 g/in ³ .

Top coating (DOC coating): The top coating of Example 14 was prepared as the top coating of Example 12 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ .

Table 5

Example 15: Evaluation of NOx adsorber Diesel oxidation catalyst of Comparative Example

2 and Examples 8A and 12-14 on a Lab Reactor

Comparative Example 2 and Examples 8A and 12-14 were tested for NOx adsorption and de- sorption performance after hydrothermal aging at 800 °C for 16 hours in 10 % steam (water)/air. Prior to desorption, the cores 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 diox ide (CO2), 5 % water (H2O) and balance nitrogen (N2) for 15 minutes at 100 °C. During this peri od, NO was adsorbed to the Pd/FER. 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 P d/zeolite was desorbed (desorption phase). The tem perature of NOx adsorption and the amount of desorbed NOx was evaluated. NO desorption curves for Comparative Example 2 and Examples 8A and 12-14 as a function of temperature are shown in Figure 3. The amount of desorbed NOx is shown in T able 6. The amount of de- sorbed NOx relates to the previously adsorbed NOx at 100°C.

Table 6 Amount of desorbed NOx for Comparative Example 2 and Examples 8A and 12-14 Example 14 0.51

As may be taken from Figure 3, namely the NOx desorption curves, it can be concluded that the additive Mn, Ba + Mn, Na + Mn and Sr + Mn permit the desired increase of the NOx desorption temperature also with high Pd loading. The optimum NOx desorption windows are obtained with the catalysts according to the present invention.

Comparative Example 3: Preparation of high Pd containing a NOx adsorber diesel oxidation catalyst - CHA with Mn and Ba additives

Bottom coating (NA coating):

The bottom coating of Comparative Example 3 was prepared as the bottom coating of Example 14 except that an ammonium CHA zeolitic material (a zeolitic material having framework struc ture type CHA, a Si0 ₂ :Al ₂ 0 ₃ molar ratio of 14:1 and a crystallinity vs. standard (XRD) = 81%) is used to replace the ammonium ferrierite zeolitic material from Example 14. The concentration of palladium in the bottom coating was 70 g/ft ³ , the concentration of the CHA in the bottom coating loading was 2.2 g/in ³ and of Zr0 ₂ was 0.44 g/in ³ . The loading of the bottom coating was 2.64 g/in ³ .

Top coating (DOC coating):

The top coating of Comparative Example 3 was prepared as the top coating of Example 14 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ .

Comparative Example 4: Preparation of high Pd containing a NOx adsorber diesel oxidation catalyst - BEAwith Mn and Ba additives

Bottom coating (NA coating):

The bottom coating of Comparative Example 4 was prepared as the bottom coating of Example 14 except that an ammonium BEA zeolitic material (a zeolitic material having framework struc ture type BEA, a Si0 ₂ :Al ₂ 0 ₃ molar ratio of 14:1 and a crystallinity vs. standard (XRD) > 80 %) is used to replace the ammonium ferrierite zeolitic material from Example 14. The concentration of palladium in the bottom coating was 70 g/ft ³ , the concentration of the BEA in the bottom coating loading was 2.2 g/in ³ and of Zr0 ₂ was 0.44 g/in ³ . The loading of the bottom coating was 2.64 g/in ³ .

Top coating (DOC coating):

The top coating of Comparative Example 3 was prepared as the top coating of Example 14 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ .

Table 7

Example 16: Evaluation of NOx adsorber diesel oxidation catalyst of Comparative Exam ples 3 and 4 and Example 14

Comparative Examples 3 and 4 and Example 14 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 cores were exposed to a mixture of 200 ppm nitric oxide (NO), 500 ppm carbon monoxide (CO), 500 ppm propylene (C ₃ H ₆ , Ci basis), 7 % oxygen (0 ₂ ), 5% carbon dioxide (C0 ₂ ), 5 % water (H ₂ 0) and balance nitrogen (N ₂ ) for 15 minutes at 100 °C. During this period, NO was adsorbed to the P d/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 60 K/min. During this period, NO that was adsorbed to the Pd/zeolite was desorbed (desorption phase). The tempera ture of NOx adsorption and the amount of desorbed NOx was evaluated. NO desorption curves for Comparative Examples 3 and 4 and Example 14 as a function of temperature are shown in Figure 4. The amount of desorbed NOx is shown in Table 8. The amount of desorbed NOx re lates to the previously adsorbed NOx at 100°C.

Table 8 Amount of desorbed NOx for Comparative Examples 3 and 4 and Example 14

As may be taken from Figure 4, namely the NOx desorption curves, it can be concluded that the catalyst according to the present invention permits the desired increase of the NOx desorption temperature also with high Pd loading compared to the catalysts representative of the prior art, namely the catalysts of Comparative Examples 3 and 4. The optimum NOx desorption windows are clearly obtained with the catalyst according to the present invention.

Example 17: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FERwith Mn and Ba additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si0 ₂ :AI ₂ 0 ₃ molar ratio of 21:1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, barium hydroxide and manganese ni trate to attain a Pd loading of 1.14 weight-% based on the weight of the final material (zeolitic material + palladium), 4.3 weight-% BaO and 1 weight-% MnC>2 loading based on the FER amount. To the resulting slurry a zirconium acetate mixture was added. The amount of zirconi um 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 0.04 L, 400 cpsi and 4 mil wall thickness, core of 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 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 50 g/ft ³ , the concentration of the FER in bottom coating loading was 2.5 g/in ³ and of ZrC>2 was 0.125 g/in ³ . The loading of the bottom coating was 2.8 g/in ³ .

Top coating (DOC coating):

The top coating of Example 17 was prepared as the top coating of Example 12 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ .

Example 18: Preparation of high Pd containing a NOx adsorber Diesel oxidation catalyst -

FER with Mn, Ba and Sr additives

Bottom coating (NA coating):

An ammonium ferrierite zeolitic material (a zeolitic material having framework structure type FER, a Si02:Al203 molar ratio of 21 :1 and a crystallinity vs. standard (XRD) > 80%) was wet impregnated with an aqueous palladium nitrate solution, barium hydroxide, strontium acetate and manganese nitrate to attain a Pd loading of 1.14 weight-% based on the weight of the final material (zeolitic material + palladium), 2 weight-% BaO, 0.5% weight-% SrO and 1 weight-% MnC>2 loading based on the FER amount. 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 Zr0 ₂ , was 5 weight-% based on the weight of the zeolitic ma terial. A porous uncoated round flow-through honeycomb substrate, cordierite (total volume 0.04 L, 400 cpsi and 4 mil wall thickness, core of 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 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 50 g/ft ³ , the concentration of the FER in bottom coating loading was 2.5 g/in ³ and of ZrC>2 was 0.125 g/in ³ . The loading of the bottom coating was 2.75 g/in ³ .

Top coating (DOC coating):

The top coating of Example 17 was prepared as the top coating of Example 12 and covers the aforementioned bottom coating over 100 % of the substrate axial length. The total loading of the top coating was 1.9 g/in ³ . Table 9

Example 19: Evaluation of NOx adsorber Diesel oxidation catalyst of Examples 17 and 18 on a Lab Reactor

The catalysts of Examples 17 and 18 were tested as defined in Example 16.

Table 10 Amount of desorbed NOx for Examples 17 and 18

As may be taken from Figure 5, namely the NOx desorption curves, it can be concluded that the additives Mn + Ba + Sr and Mn + Ba permit the desired increase of the NOx desorption temper ature also with medium Pd loading.

Brief description of the figures

Figure 1 shows the NOx desorption curves obtained with the catalysts of Comparative Ex ample 1 and of Examples 1 to 6.

Figure 2 shows the NOx desorption curves obtained with the catalysts of Comparative Ex ample 2 and of Examples 8A and 8 to 10.

Figure 3 shows the NOx desorption curves obtained with the catalysts of Comparative Ex ample 2 and of Examples 12 to 14.

Figure 4 shows the NOx desorption curves obtained with the catalysts of Comparative Ex amples 3 and 4 and of Example 14.

Figure 5 shows the NOx desorption curves obtained with the catalysts of Examples 17 and 18.

Cited literature

-WO 2020/0236879