TECHNICAL FIELD

The present invention relates to a process for the reforming of ammonia, and more specifically to a process for the reforming of ammonia employing a Ru-containing catalyst at low temperatures and elevated pressure.

INTRODUCTION

NH3 is seen as an energy vector of the future, able to store chemically significant amounts of H2. So, sustainable NH3 might be produced on a large scale from regenerative energy sources. The reforming of NH3 (see equation 1 below) on site, where the H2 is needed, might be the last step in closing an H2 value chain based on renewable electricity.

(1 ) 2 NH ₃ N ₂ + 3 H ₂

For enhancing the decomposition of ammonia to nitrogen and hydrogen, the use of supported Ru catalysts have been discussed. Thus, by way of example, K. Lamb et. al. in Int. J. of Hydrogen Energy 2019, 44, 3726-3736 studies the kinetics of ammonia decomposition over LiOH- promoted RU/AI2O3. A. Di Carlo et al. in Int. J. of Hydrogen Energy2f \ , 39, 808-814, on the other hand, studies ammonia decomposition over a commercial RU/AI2O3 catalyst at different operative pressures and temperatures, wherein it is noted that greater dissociation rates are achieved at lower pressures.

T.A. Le et al. in Korean J. Chem. Eng. 2021 , 38(6), 1087-1103 discusses developments of ruthenium and nickel catalysts for CO _x -free H2 generation by ammonia decomposition. Said document however indicates that alkaline earth metal oxide supports and in particular basic supports such as MgO or neutral supports such as carbon nanotubes would provide better results than amphoteric supports such as CT2O3 and TiO2 or acidic supports such a AI2O3, ZrO2, or SiO ₂ .

M. Miyamoto et al. in Int. J. of Hydrogen Energy 2018, 43, 730-738 relates to the doping of ZrO2 supports for increasing their basicity using La, and their use in reactions for the production of hydrogen. Similarly, B. Lorenzut et al. in ChemCatChem2(Y\ Q, 2, 1096 - 1106, discloses the use of lanthanum-stabilized zirconia, and indicates that basic oxides would be more efficient as supports for Ru catalysts as compared to acidic oxides. Z. Wang et al. in Int. J. of Hydrogen EnergyTQV , 44, 7300-7307, for its part, relates to a Ba-modified ZrC>2 support for Ru, and its use for ammonia decomposition. Ru supported on ZrC>2 has also found use as a catalyst in other reactions. Thus, WO 2015/086639 A2 relates to a Ru/ZrO2 catalyst applied in the hydrogenation of aromatic compounds whereas WO 2018/046393 A1 relates to a Ru/ZrO2 catalyst applied in the hydrogenation of nitriles.

On the other hand, S.-F. Yin et al. in Applied Catalysis B Environmental 2004, 48, 237-241 relates to the use of carbon nanotubes (CNTs) as a support for Ru nanoparticles in the generation of hydrogen by ammonia decomposition, wherein the order of activities for different supports is indicated to rank as follows: Ru/CNTs > Ru/MgO > Ru/activated carbon > Ru/ZrO2 = RU/AI2O3.

To have direct access to H2 at elevated pressure (10-50 bara), the NHs-reforming itself must however also be conducted at these pressures. Accordingly, there remains a need for an improved and cost-efficient process for NHs-reforming which allows for the direct provision of H2 under the conditions required for its further reaction.

In this regard, S. Sayas et al. in Catai. Sci. Techno! 2020, 10, 5027-5035 studies high pressure ammonia decomposition on Ru-K/CaO catalysts at pressures of up to 40 bar. As for T.A. Le et al. in Korean J. Chem. Eng. 2021 , 38(6), 1087-1103, S. Sayas et al. teaches that the nature of the support would have been shown to strongly influence the catalytic performance of Ru-based catalysts, wherein among the use of basic supports like MgO and La2Os, neutral supports such as carbon nanotubes, and acidic supports such as AI2O3, the use of basic and neutral supports generally results in better catalytic properties.

There, however, remains the need for a highly effective process for the decomposition of ammonia at high pressures. Furthermore, there remains the need for a process for the decomposition of ammonia which is highly active at low temperatures, in particular when used in applications involving high pressure. In addition thereto, there remains the need for a process employing an ammonia decomposition catalyst which displays a high hydrothermal resistance, in particular when used under high pressure conditions, in view of water which may be present during the reaction, in particular in view of the small amounts which are present in industrial grade ammonia for its stabilization.

DETAILED DESCRIPTION

Thus, a highly efficient process for the high pressure (> 10 bar) decomposition of ammonia employing a low temperature (200 to 750 °C, preferably 200 to 650 °C, more preferably 200 to 600 °C) has surprisingly been found, which may furthermore be employed in the presence of small amounts of water as are present in industrial grade ammonia.

Therefore, the present invention relates to a process for the reforming of ammonia, wherein the process comprises (i) providing a reactor containing a catalyst comprising Ru and one or more support materials, wherein Ru is supported on the one or more support materials, wherein the one or more support materials display a BET surface area of 20 m ² /g or more, wherein the BET surface area is preferably determined according to ISO 9277:2010, and wherein the catalyst contains 1 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the catalyst;

(ii) preparing a feed gas stream comprising NH3;

(iii) feeding the feed gas stream prepared in (ii) into the reactor provided in (i) and contacting the feed gas stream with the catalyst, wherein contacting is performed at a pressure of greater than 10 bara, and at a temperature in the range of from 200 to 750 °C;

(iv) removing an effluent gas stream from the reactor, the effluent gas stream comprising H2 and N2.

Within the meaning of the present invention, the BET surface area of the one or more support materials refers to the BET surface area of the one or more support materials which is not loaded with any element and/or compound. Furthermore within the meaning of the present invention, in instances wherein the catalyst comprises more than one support material, the BET surface area refers to the BET surface area of each of the one or more support materials, such that each of the more than one support materials displays a BET surface area within the ranges of surface areas as defined in the present invention.

According to the present invention, the catalyst in (i) preferably contains substantially no Ni and Co.

Thus, it is preferred that in (i), the catalyst contains 0.5 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the catalyst, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, and more preferably 0.001 wt.-% or less.

In particular, it is preferred that in (i), the reactor contains 1 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the total contents of the reactor, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, and more preferably 0.001 wt.-% or less.

The following two preferred alternatives apply with respect to the BET surface area of the one or more support materials.

According to a first alternative, it is preferred that in (i), the one or more support materials display a BET surface area in the range of from 30 to 800 m ² /g, more preferably of from 40 to 500 m ² /g, more preferably of from 50 to 300 m ² /g, more preferably of from 60 to 200 m ² /g, more preferably of from 70 to 100 m ² /g, and more preferably of from 75 to 80 m ² /g. According to a second alternative, it is preferred that in (i), the one or more support materials display a BET surface area in the range of from greater than 20 to 150 m ² /g, more preferably of from 21 to 100 m ² /g, more preferably of from 22 to 70 m ² /g, more preferably of from 23 to 50 m ² /g, more preferably of from 24 to 40 m ² /g, and more preferably of from 25 to 35 m ² /g.

It is preferred that in (i), the one or more support materials display a pore volume in the range of from 0.2 to 3 ml/g, more preferably of from 0.4 to 1.5 ml/g, more preferably of from 0.6 to 1 ml/g, and more preferably of from 0.8 to 0.85 ml/g, wherein the pore volume is preferably determined according to ISO 15901-2:2022.

Within the meaning of the present invention, the pore volume of the one or more support materials refers to the pore volume of the one or more support materials which is not loaded with any element and/or compound. Furthermore within the meaning of the present invention, in instances wherein the catalyst comprises more than one support material, the pore volume refers to the pore volume of each of the one or more support materials, such that each of the more than one support materials displays a pore volume within the ranges of pore volumes as defined in the present invention.

It is preferred that in (i), the catalyst displays a BET surface area in the range of 20 to 800 m ² /g, preferably of from 30 to 500 m ² /g, more preferably of from 40 to 300 m ² /g, more preferably of from 50 to 200 m ² /g, more preferably of from 60 to 100 m ² /g, and more preferably of from 70 to 75 m ² /g, wherein the BET surface area is preferably determined according to ISO 9277:2010.

It is preferred that in (i), the catalyst displays a pore volume in the range of 0.1 to 2 ml/g, more preferably of from 0.15 to 1.2 ml/g, more preferably of from 0.2 to 0.8 ml/g, more preferably of from 0.25 to 0.5 ml/g, and more preferably of from 0.3 to 0.35 ml/g, wherein the pore volume is preferably determined according to ISO 15901-2:2022.

It is preferred that in (i), from 90 to 100 wt.-% of Ru calculated as the element, and based on 100 wt.-% of Ru contained in the catalyst, is supported on the one or more support materials comprised in the catalyst, more preferably of from 95 to 100 wt.-%, more preferably of from 99 to 100 wt.-%, more preferably of from 99.5 to 100 wt.-%, and more preferably of from 99.9 to 100 wt.-%.

It is preferred that in (i), Ru is supported on the one or more support materials by an impregnation technique employing an aqueous solution of one or more ruthenium salts, wherein the one or more ruthenium salts preferably comprise Ru(NO)(NOs)3, wherein more preferably RU(NO)(NOS)3 is employed as the one or more ruthenium salts.

It is preferred that in (i), the one or more support materials are selected from the group consisting of metal oxides, wherein the metal of the metal oxides is preferably selected from the group consisting of Al, Si, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, alkaline earth metals, and rare earth metals, including combinations of two or more thereof, more preferably from the group consist- ing of Al, Si, Ti, Zr, Mg, Ca, La, Ce, Pr, and Nd, including combinations of two or more thereof, more preferably from the group consisting of Al, Ti, Zr, Mg, Ca, and La, including combinations of two or more thereof, and more preferably from the group consisting of Al, Zr, and Mg, including combinations of two or more thereof, wherein more preferably the one or more support materials comprise one or more metal oxides selected from the group consisting of AI2O3, ZrC>2, and spinels, including mixtures of two or more thereof, preferably from the group consisting of ZrO ₂ and spinels, including mixtures of two or more thereof, wherein more preferably the one or more support materials comprise ZrO ₂ and/or MgAhC , preferably ZrC>2, wherein more preferably the one or more support materials consist of ZrO ₂ and/or MgAhC , preferably of ZrC>2.

In the case where in (i), the one or more support materials comprise ZrC>2, it is preferred that the ZrO ₂ comprises one or more crystalline phases and/or is amorphous, wherein the one or more crystalline phases of ZrO ₂ are selected from the group consisting of the monoclinic, tetragonal, and cubic phases of ZrC>2, including mixtures of two or three thereof.

It is preferred that in (i), the one or more support materials contain substantially no CaO and/or MgO, more preferably substantially no CaO and MgO, more preferably substantially no alkaline earth metal oxide, more preferably substantially no Ca and/or Mg, more preferably substantially no Ca and Mg, and more preferably substantially no alkaline earth metal.

It is preferred that in (i), the one or more support materials contain substantially no AI2O3 and/or SiO2, more preferably substantially no AI2O3 and SiO2, more preferably substantially no Al and/or Si, and more preferably substantially no Al and Si

It is preferred that in (i), the one or more support materials contain substantially no carbon nanotubes, more preferably substantially no elemental carbon, and more preferably substantially no carbon.

Within the meaning of the present invention, the term “substantially no” as employed in the present patent application indicates that the element or compound in question is contained in the component in question in an amount of 1 wt.-% or less based on 100 wt.-% of the component in question, preferably of 0.5 wt.-% or less, more preferably of 0.1 wt.-% or less, more preferably of 0.05 wt.-% or less, more preferably of 0.01 wt.-% or less, more preferably of 0.005 wt.-% or less, and more preferably of 0.001 wt.-% or less.

It is preferred that in (i), the catalyst comprises Ru in an amount in the range of from 0.5 to 15 wt.-% based on 100 wt.-% of the total amount of the one or more support materials, more preferably of from 1 to 10 wt.-%, more preferably of from 2 to 8 wt.-%, more preferably of from 3 to 6.5 wt.-%, more preferably of from 4 to 6 wt.-%, and more preferably of from 4.5 to 5.5 wt.-%.

It is preferred that in (i), from 95 to 100 wt.-% of the catalyst consists of Ru and the one or more support materials, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.

It is preferred that in (i), the catalyst further comprises one or more alkali metal and/or alkaline earth metal hydroxides, wherein the one or more alkali metal and/or alkaline earth metal hydroxides are supported on the one or more support materials supporting Ru, wherein the alkali metal and/or alkaline earth metal hydroxides are preferably selected from the group consisting of Mg(OH)2, Ca(OH)2, Ba(OH)2, Sr(OH)2, LiOH, NaOH, and KOH, including mixtures of two or more thereof, more preferably from the group consisting of Mg(OH)2, Ca(OH)2, LiOH, NaOH, and KOH, including mixtures of two or more thereof, more preferably from the group consisting of LiOH, NaOH, and KOH, including mixtures of two or more thereof, wherein more preferably the catalyst further comprises KOH and/or LiOH, preferably KOH.

In the case where the catalyst further comprises one or more alkali metal hydroxides, it is preferred that the catalyst comprises the one or more alkali metal hydroxides in an amount in the range of from 0.5 to 15 wt.-% based on 100 wt.-% of the total amount of the one or more support materials, more preferably of from 1 to 10 wt.-%, more preferably of from 2 to 8 wt.-%, more preferably of from 3 to 6.5 wt.-%, more preferably of from 4 to 6 wt.-%, and more preferably of from 4.5 to 5.5 wt.-%.

Further in the case where the catalyst further comprises one or more alkali metal hydroxides, it is preferred that from 95 to 100 wt.-% of the catalyst consists of Ru, the one or more alkali metal hydroxides, and the one or more support materials, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.

It is preferred that in (i), the catalyst is in the form of a molding and/or in powder form, more preferably in the form of a molding, and more preferably in the form of extrudates or tablets.

In the case where in (i), the catalyst is in the form of extrudates, it is preferred that the extrudates have a diameter in the range of from 0.5 to 10 mm, more preferably of from 1 to 7 mm, more preferably of from 1 .5 to 5 mm, more preferably of from 2 to 4 mm, and more preferably of from 2.5 to 3.5 mm.

Further in the case where in (i), the catalyst is in the form of extrudates, it is preferred that the extrudates are split, and the catalyst is in the form of extrudates of a split sieve fraction in the range of from 50 pm to 2.5 mm, more preferably of from 100 pm to 1 .5 mm, more preferably of from 200 pm to 1 mm, more preferably of from 250 to 700 pm, and more preferably of from 300 to 500 pm.

In the case where in (i) the catalyst is in the form of tablets, it is preferred that the tablets have a four-hole cross-section, more preferably a four-hole cross-section and four flutes. It is preferred that contacting is performed at a pressure in the range of from 11 to 50 bara, more preferably of from 15 to 45 bara, more preferably of from 15 to 40 bara, more preferably of from 18 to 35 bara, more preferably of from 19 to 31 bara, more preferably of from 20 to 28 bara, and more preferably of from 20 to 25 bara.

It is preferred that contacting is performed at a temperature in the range of from 200 to 650 °C, more preferably of from 250 to 600 °C, more preferably of from 300 to 550 °C, more preferably of from 350 to 520 °C, more preferably of from 400 to 500 °C, and more preferably of from 430 to 470 °C.

It is preferred that the feed gas stream prepared in (ii) comprises from 1 to 100 vol.-% of NH3, more preferably from 3 to 99.99 vol.-%, more preferably from 5 to 99.95 vol.-%, more preferably from 10 to 99.9 vol.-%, more preferably from 15 to 99.9 vol.-%, more preferably from 20 to 99.8 vol.-%, more preferably from 30 to 99.7 vol.-%, more preferably from 40 to 99.6 vol.-%, and more preferably from 50 to 99.5 vol.-%.

It is preferred that the feed gas stream prepared in (ii) comprises from 0 to 50 vol.-% of N2, more preferably from 0.01 to 30 vol.-%, more preferably from 0.03 to 15 vol.-%, more preferably from 0.05 to 5 vol.-%, more preferably from 0.1 to 1 vol.-%, more preferably from 0.12 to 0.5 vol.-%, and more preferably from 0.14 to 0.16 vol. -%.

It is preferred that the feed gas stream prepared in (ii) comprises from 0 to 75 vol.-% of H2, more preferably from 0 to 60 vol.-%, more preferably from 0 to 50 vol.-%, more preferably from 0 to 40 vol.-%, more preferably from 0 to 35 vol.-%, and more preferably from 0 to 30 vol.-%.

It is preferred that the feed gas stream prepared in (ii) comprises from 100 to 50,000 ppmv of H2O, more preferably from 200 to 30,000 ppmv, more preferably from 500 to 25,000 ppmv, more preferably from 500 to 20,000 ppmv, more preferably from 500 to 15,000 ppmv, more preferably from 750 to 15,000 ppmv, more preferably from 1 ,000 to 11 ,000 ppmv, more preferably from 1 ,000 to 10,000 ppmv, more preferably from 2,000 to 8,000 ppmv, more preferably from 3,000 to 7,500 ppmv, more preferably from 4,500 to 7,000 ppmv, more preferably from 5,000 to 6,500 ppmv.

It is preferred that the total amount of NH3, N2, and H2 comprised in the feed gas stream prepared in (ii) is in the range from 90 to 100 wt.-%, more preferably from 95 to 99.95 vol.-%, more preferably from 98 to 99.9 vol.-%, more preferably from 99 to 99.85 vol.-%, and more preferably from 99.7 to 99.8 vol.-%.

It is preferred that after (i) and prior to (iii) the catalyst contained in the reactor provided in (i) is reduced in an atmosphere comprising hydrogen.

In the case where after (i) and prior to (iii) the catalyst contained in the reactor provided in (i) is reduced in an atmosphere comprising hydrogen, it is preferred that the reduction is conducted at a temperature in the range of from 20 to 100 °C, more preferably of from 24 to 50 °C, more preferably of from 26 to 35 °C, and more preferably of from 28 to 32 °C.

Further in the case where after (i) and prior to (iii) the catalyst contained in the reactor provided in (i) is reduced in an atmosphere comprising hydrogen, it is preferred that the reduction is conducted in an atmosphere comprising from 1 to 50 vol.-% H2, more preferably from 2 to 20 vol.- %, more preferably from 3 to 10 vol.-%, and more preferably from 4 to 6 vol-%.

Further in the case where after (i) and prior to (iii) the catalyst contained in the reactor provided in (i) is reduced in an atmosphere comprising hydrogen, it is preferred that the atmosphere comprises from 50 to 99 vol.-% of an inert gas, more preferably of from 80 to 98 vol.-%, more preferably of from 90 to 97 vol.-%, and more preferably from 94 to 96 vol.-%. Furthermore, it is preferred that the inert gas comprises one or more gases selected from the group consisting of noble gases, CO2, and nitrogen, more preferably from the group consisting of He, Ar, Ne, and N2, CO2, wherein more preferably the inert gas comprises CO2, N2, or CO2 and N2, wherein more preferably the inert gas comprises N2, wherein more preferably the inert gas is N2.

It is preferred that the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO.

The following three preferred alternatives apply with respect to the composition of the gas stream prepared in (ii) in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO.

According to a first alternative, it is preferred that the feed gas stream prepared in (ii) further comprises CO2 and one or more hydrocarbons, and wherein the feed gas stream more preferably comprises 5 vol.-% or less of H2O, more preferably 3 vol.-% or less, more preferably 1 vol.- % or less, more preferably 0.5 vol.-% or less, more preferably 0.1 vol.-% or less, more preferably 0.05 vol.-% or less, and more preferably 0.01 vol.-% or less of H2O.

According to a second alternative, it is preferred that the feed gas stream prepared in (ii) further comprises H2O and one or more hydrocarbons, and wherein the feed gas stream preferably comprises 5 vol.-% or less of CO2, more preferably 3 vol.-% or less, more preferably 1 vol.-% or less, more preferably 0.5 vol.-% or less, more preferably 0.1 vol.-% or less, more preferably 0.05 vol.-% or less, and more preferably 0.01 vol.-% or less of CO2.

According to a third alternative, it is preferred that the feed gas stream prepared in (ii) further comprises CO2, H2O, and one or more hydrocarbons. Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the one or more hydrocarbons are selected from the group consisting of alkanes and mixtures thereof, preferably of C1-C10 alkanes and mixtures thereof, more preferably of C3-C9 alkanes and mixtures thereof, more preferably of C4-C8 alkanes and mixtures thereof, more preferably of C5-C7 alkanes and mixtures thereof, more preferably of C6 alkanes and mixtures thereof.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that contacting is performed at a pressure in the range of from greater than 10 to 50 bara, more preferably of from 12 to 45 bara, more preferably of from 15 to 40 bare, more preferably of from 18 to 35 bara, and more preferably of from 20 to 30 bara.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed gas stream prepared in (ii) comprises from 0.1 to 75 vol.- % of NH3, more preferably from 0.3 to 60 vol.-%, more preferably from 0.5 to 50 vol.-%, more preferably from 0.8 to 40 vol.-%, and more preferably from 1 to 30 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed gas stream prepared in (ii) comprises from 10 to 70 vol.- % of the one or more hydrocarbons, more preferably from 12 to 60 vol.-%, and more preferably from 15 to 50 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed gas stream prepared in (ii) comprises from 0 to 75 vol.-% of H2O, more preferably from 0.5 to 70 vol.-%, more preferably from 1 to 68 vol.-%, more preferably from 3 to 66 vol.-%, more preferably from 5 to 64 vol.-%, more preferably from 8 to 62 vol.-%, and more preferably from 10 to 60 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed gas stream prepared in (ii) comprises from 0 to 60 vol.-% of CO2, more preferably from 1 to 58 vol.-%, more preferably from 3 to 56 vol.-%, more prefera- bly from 5 to 54 vol.-%, more preferably from 8 to 52 vol.-%, and more preferably from 10 to 50 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed stream displays an H2O : C molar ratio of H2O to carbon contained in the one or more hydrocarbons in the range of from 0 to 4, more preferably of from 0.1 to 3, more preferably of from 0.3 to 2.5, more preferably of from 0.4 to 2, and more preferably of from 0.5 to 1.6

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed stream displays a CO2 : C molar ratio of CO2 to carbon contained in the one or more hydrocarbons in the range of from 0 to 4, more preferably of from 0.1 to 3, more preferably of from 0.2 to 2, and more preferably of from 0.3 to 1 .5.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the feed stream displays an NH3 : C molar ratio of NH3 to carbon contained in the one or more hydrocarbons in the range of from 0 to 5, more preferably of from 0 to 4, more preferably of from 0.001 to 3, more preferably of from 0.005 to 2, and more preferably of from 0.01 to 1.

It is preferred that the feed stream is fed into the reactor at a gas hourly space velocity in the range of from 500 to 20,000 IT ¹ , more preferably of from 500 to 16,000 IT ¹ , more preferably of from 700 to 14,000 IT ¹ , more preferably of from 800 to 12,000 IT ¹ , more preferably of from 900 to 10,000 IT ¹ , more preferably of from 1 ,000 to 8,000 IT ¹ , and more preferably of from 3,000 to 5,000 IT ¹ .

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the effluent gas stream removed in (iv) further comprises CO2.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the effluent gas stream removed in (iv) displays an H2 : CO molar ratio of >2. Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the effluent gas stream removed in (iv) displays a stoichiometry number R in the range of from 0.1 to 3, wherein R is defined according to formula (I): wherein c(H2), c(CO2), and c(CO) stand for the molar concentration of H2, CO2, and CO in the effluent gas stream, respectively.

The following three alternatives apply with respect to the stoichiometry number R of the effluent gas stream removed in (iv).

According to a first alternative, it is preferred that the effluent gas stream removed in (iv) displays a stoichiometry number R in the range of from 0.1 to 3, wherein R is defined according to formula (I), it is preferred that the stoichiometry number R is in the range of from 1 to 2.5, more preferably of from 1 .3 to 2.2.

According to a second alternative, it is preferred that the effluent gas stream removed in (iv) displays a stoichiometry number R > 2. Further, it is preferred according to the second alternative that the effluent gas stream removed in (iv) displays an H2 : CO molar ratio of >2.

According to a third alternative, it is preferred that the stoichiometry number R is in the range of 0.5 to 3, preferably of from 1 to 2.2, and more preferably of 1 .3 to 1 .7.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the effluent gas stream removed in (iv) comprises from 10 to 90 vol.-% of H2, more preferably from 20 to 80 vol.-%, more preferably from 30 to 70 vol.-%, more preferably from 40 to 65 vol.-%, and more preferably from 45 to 60 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO, it is preferred that the effluent gas stream removed in (iv) comprises from 1 to 70 vol.-% of CO, more preferably from 3 to 50 vol.-%, more preferably from 5 to 40 vol.-%, more preferably from 10 to 35 vol.-%, and more preferably from 15 to 30 vol.-%.

Further in the case where the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further com- prises CO, it is preferred that the effluent gas stream removed in (iv) comprises from 1 to 50 vol.-% of CO2, more preferably from 3 to 45 vol.-%, more preferably from 5 to 40 vol.-%, more preferably from 8 to 35 vol.-%, more preferably from 10 to 30 vol.-%, and more preferably from 12 to 25 vol.-%.

It is preferred that the effluent gas stream removed in (iv) is employed in a process for the production of methanol, for the production of dimethyl ether, or for the production of methanol and dimethylether.

It is preferred that the effluent gas stream removed in (iv) is employed in a process for the production of hydrocarbons, more preferably according to the Fischer-Tropsch process.

It is preferred that the effluent gas stream removed in (iv) is employed in a process for the production of alcohols, more preferably of alkanols, more preferably of C1 to C10 alkanols, more preferably of C2 to C8 alkanols, more preferably of C2 to C6 alkanols, more preferably of C2 to C4 alkanols, more preferably of C2 alkanols, and more preferably of ethanol.

It is preferred that at an initial stage of the process, the feed gas stream prepared in (ii) and fed into the reactor in (iii) further comprises H2 for reducing the catalyst.

In the case where at an initial stage of the process, the feed gas stream prepared in (ii) and fed into the reactor in (iii) further comprises H2 for reducing the catalyst, it is preferred that the feed gas stream prepared in (ii) and fed into the reactor in (iii) further comprises from 0.5 to 80 vol.-% of H2, more preferably from 1 to 70 vol.-%, more preferably from 2 to 60 vol.-%, more preferably from 5 to 50 vol.-%, more preferably from 15 to 40 vol.-%.

The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", 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 process of any one of embodiments 1 , 2, 3, and 4". Further, it is explicitly noted that the following set of embodiments is not the set of claims determining the extent of protection, but represents a suitably structured part of the description directed to general and preferred aspects of the present invention.

1 . A process for the reforming of ammonia, wherein the process comprises

(i) providing a reactor containing a catalyst comprising Ru and one or more support materials, wherein Ru is supported on the one or more support materials, wherein the one or more support materials display a BET surface area of 20 m ² /g or more, wherein the BET surface area is preferably determined according to ISO 9277:2010, and wherein the catalyst contains 1 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the catalyst;

(ii) preparing a feed gas stream comprising NH3;

(iii) feeding the feed gas stream prepared in (ii) into the reactor provided in (i) and contacting the feed gas stream with the catalyst, wherein contacting is performed at a pressure of greater than 10 bara, and at a temperature in the range of from 200 to 750 °C;

(iv) removing an effluent gas stream from the reactor, the effluent gas stream comprising H2 and N2.

2. The process of embodiment 1 , wherein in (i), the catalyst contains 0.5 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the catalyst, preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.- % or less, more preferably 0.005 wt.-% or less, and more preferably 0.001 wt.-% or less.

3. The process of embodiment 1 , wherein in (i), the reactor contains 1 wt.-% or less of Ni and Co calculated as the respective element and based on 100 wt.-% of the total contents of the reactor, preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less, more preferably 0.05 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.005 wt.-% or less, and more preferably 0.001 wt.-% or less.

4. The process of any of embodiments 1 to 3, wherein in (i), the one or more support materials display a BET surface area in the range of from 30 to 800 m ² /g, preferably of from 40 to 500 m ² /g, more preferably of from 50 to 300 m ² /g, more preferably of from 60 to 200 m ² /g, more preferably of from 70 to 100 m ² /g, and more preferably of from 75 to 80 m ² /g.

5. The process of any of embodiments 1 to 3, wherein in (i), the one or more support materials display a BET surface area in the range of from greater than 20 to 150 m ² /g, preferably of from 21 to 100 m ² /g, more preferably of from 22 to 70 m ² /g, more preferably of from 23 to 50 m ² /g, more preferably of from 24 to 40 m ² /g, and more preferably of from 25 to 35 m ² /g.

6. The process of any of embodiments 1 to 5, wherein in (i), the one or more support materials display a pore volume in the range of from 0.2 to 3 ml/g, preferably of from 0.4 to 1.5 ml/g, more preferably of from 0.6 to 1 ml/g, and more preferably of from 0.8 to 0.85 ml/g, wherein the pore volume is preferably determined according to ISO 15901-2:2022.

7. The process of any of embodiments 1 to 6, wherein in (i), the catalyst displays a BET surface area in the range of 20 to 800 m ² /g, preferably of from 30 to 500 m ² /g, more preferably of from 40 to 300 m ² /g, more preferably of from 50 to 200 m ² /g, more preferably of from 60 to 100 m ² /g, and more preferably of from 70 to 75 m ² /g, wherein the BET surface area is preferably determined according to ISO 9277:2010.

8. The process of any of embodiments 1 to 7, wherein in (i), the catalyst displays a pore volume in the range of 0.1 to 2 ml/g, preferably of from 0.15 to 1.2 ml/g, more preferably of from 0.2 to 0.8 ml/g, more preferably of from 0.25 to 0.5 ml/g, and more preferably of from 0.3 to 0.35 ml/g, wherein the pore volume is preferably determined according to ISO 15901-2:2022. The process of any of embodiments 1 to 8, wherein in (i), from 90 to 100 wt.-% of Ru calculated as the element, and based on 100 wt.-% of Ru contained in the catalyst, is supported on the one or more support materials comprised in the catalyst, preferably of from 95 to 100 wt.-% , more preferably of from 99 to 100 wt.-% , more preferably of from 99.5 to 100 wt.-% , and more preferably of from 99.9 to 100 wt.-%. The process of any of embodiments 1 to 9, wherein in (i), Ru is supported on the one or more support materials by an impregnation technique employing an aqueous solution of one or more ruthenium salts, wherein the one or more ruthenium salts preferably comprise RU(NO)(NOS)3, wherein more preferably Ru(NO)(NOs)3 is employed as the one or more ruthenium salts. The process of any of embodiments 1 to 10, wherein in (i), the one or more support materials are selected from the group consisting of metal oxides, wherein the metal of the metal oxides is preferably selected from the group consisting of Al, Si, Ti, Zr, Hf, V, Nb, Ta, Cr, Mo, W, Mn, alkaline earth metals, and rare earth metals, including combinations of two or more thereof, more preferably from the group consisting of Al, Si, Ti, Zr, Mg, Ca, La, Ce, Pr, and Nd, including combinations of two or more thereof, more preferably from the group consisting of Al, Ti, Zr, Mg, Ca, and La, including combinations of two or more thereof, and more preferably from the group consisting of Al, Zr, and Mg, including combinations of two or more thereof, wherein more preferably the one or more support materials comprise one or more metal oxides selected from the group consisting of AI2O3, ZrC>2, and spinels, including mixtures of two or more thereof, preferably from the group consisting of ZrO ₂ and spinels, including mixtures of two or more thereof, wherein more preferably the one or more support materials comprise ZrO ₂ and/or MgAhC , preferably ZrC>2, wherein more preferably the one or more support materials consist of ZrO ₂ and/or MgAhC , preferably of ZrC>2. The process of embodiment 11 , wherein the ZrO ₂ comprises one or more crystalline phases and/or is amorphous, wherein the one or more crystalline phases of ZrO ₂ are selected from the group consisting of the monoclinic, tetragonal, and cubic phases of ZrC>2, including mixtures of two or three thereof. The process of any of embodiments 1 to 12, wherein in (i), the one or more support materials contain substantially no CaO and/or MgO, preferably substantially no CaO and MgO, more preferably substantially no alkaline earth metal oxide, more preferably substantially no Ca and/or Mg, more preferably substantially no Ca and Mg, and more preferably substantially no alkaline earth metal. 14. The process of any of embodiments 1 to 13, wherein in (i), the one or more support materials contain substantially no AI2O3 and/or SiC>2, preferably substantially no AI2O3 and SiC>2, more preferably substantially no Al and/or Si, and more preferably substantially no Al and Si.

15. The process of any of embodiments 1 to 14, wherein in (i), the one or more support materials contain substantially no carbon nanotubes, preferably substantially no elemental carbon, and more preferably substantially no carbon.

16. The process of any of embodiments 1 to 15, wherein in (i), the catalyst comprises Ru in an amount in the range of from 0.5 to 15 wt.-% based on 100 wt.-% of the total amount of the one or more support materials, preferably of from 1 to 10 wt.-%, more preferably of from 2 to 8 wt.-%, more preferably of from 3 to 6.5 wt.-%, more preferably of from 4 to 6 wt.-%, and more preferably of from 4.5 to 5.5 wt.-%.

17. The process of any of embodiments 1 to 16, wherein in (i), from 95 to 100 wt.-% of the catalyst consists of Ru and the one or more support materials, preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.

18. The process of any of embodiments 1 to 17, wherein in (i), the catalyst further comprises one or more alkali metal and/or alkaline earth metal hydroxides, wherein the one or more alkali metal and/or alkaline earth metal hydroxides are supported on the one or more support materials supporting Ru, wherein the alkali metal and/or alkaline earth metal hydroxides are preferably selected from the group consisting of Mg(OH)2, Ca(OH)2, Ba(OH)2, Sr(OH)2, LiOH, NaOH, and KOH, including mixtures of two or more thereof, more preferably from the group consisting of Mg(OH)2, Ca(OH)2, LiOH, NaOH, and KOH, including mixtures of two or more thereof, more preferably from the group consisting of LiOH, NaOH, and KOH, including mixtures of two or more thereof, wherein more preferably the catalyst further comprises KOH and/or LiOH, preferably KOH.

19. The process of embodiment 18, wherein the catalyst comprises the one or more alkali metal hydroxides in an amount in the range of from 0.5 to 15 wt.-% based on 100 wt.-% of the total amount of the one or more support materials, preferably of from 1 to 10 wt.-%, more preferably of from 2 to 8 wt.-%, more preferably of from 3 to 6.5 wt.-%, more preferably of from 4 to 6 wt.-%, and more preferably of from 4.5 to 5.5 wt.-%.

20. The process of embodiment 18 or 19, wherein from 95 to 100 wt.-% of the catalyst consists of Ru, the one or more alkali metal hydroxides, and the one or more support materials, preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%. The process of any of embodiments 1 to 20, wherein in (i), the catalyst is in the form of a molding and/or in powder form, preferably in the form of a molding, and more preferably in the form of extrudates or tablets. The process of embodiment 21 , wherein the extrudates have a diameter in the range of from 0.5 to 10 mm, preferably of from 1 to 7 mm, more preferably of from 1 .5 to 5 mm, more preferably of from 2 to 4 mm, and more preferably of from 2.5 to 3.5 mm. The process of embodiment 21 or 22, wherein the extrudates are split, and the catalyst is in the form of extrudates of a split sieve fraction in the range of from 50 pm to 2.5 mm, preferably of from 100 pm to 1 .5 mm, more preferably of from 200 pm to 1 mm, more preferably of from 250 to 700 pm, and more preferably of from 300 to 500 pm. The process of embodiment 21 , wherein the tablets have a four-hole cross-section, preferably a four-hole cross-section and four flutes. The process of any of embodiments 1 to 24, wherein contacting is performed at a pressure in the range of from 11 to 50 bara, preferably of from 15 to 45 bara, more preferably of from 15 to 40 bara, more preferably of from 18 to 35 bara, more preferably of from 19 to 31 bara, more preferably of from 20 to 28 bara, and more preferably of from 20 to 25 bara. The process of any of embodiments 1 to 25, wherein contacting is performed at a temperature in the range of from 200 to 650 °C, preferably of from 250 to 600 °C, more preferably of from 300 to 550 °C, and more preferably of from 350 to 520 °C, and more preferably of from 400 to 500 °C, and more preferably of from 430 to 470 °C. The process of any of embodiments 1 to 26, wherein the feed gas stream prepared in (ii) comprises from 1 to 100 vol.-% of NH3, preferably from 3 to 99.99 vol.-%, more preferably from 5 to 99.95 vol.-%, more preferably from 10 to 99.9 vol.-%, more preferably from 15 to 99.9 vol.-%, more preferably from 20 to 99.8 vol.-%, more preferably from 30 to 99.7 vol.- %, more preferably from 40 to 99.6 vol.-%, and more preferably from 50 to 99.5 vol.-%. The process of any of embodiments 1 to 27, wherein the feed gas stream prepared in (ii) comprises from 0 to 50 vol.-% of N2, preferably from 0.01 to 30 vol.-%, more preferably from 0.03 to 15 vol.-%, more preferably from 0.05 to 5 vol.-%, more preferably from 0.1 to 1 vol.-%, more preferably from 0.12 to 0.5 vol.-%, and more preferably from 0.14 to 0.16 vol.-%. The process of any of embodiments 1 to 28, wherein the feed gas stream prepared in (ii) comprises from 0 to 75 vol.-% of H2, preferably from 0 to 60 vol.-%, more preferably from 0 to 50 vol.-%, more preferably from 0 to 40 vol.-%, more preferably from 0 to 35 vol.-%, and more preferably from 0 to 30 vol.-%. 30. The process of any of embodiments 1 to 29, wherein the feed gas stream prepared in (ii) comprises from 100 to 50,000 ppmv of H2O, preferably from 200 to 30,000 ppmv, more preferably from 500 to 25,000 ppmv, more preferably from 500 to 20,000 ppmv, more preferably from 500 to 15,000 ppmv, more preferably from 750 to 15,000 ppmv, more preferably from 1 ,000 to 11 ,000 ppmv, more preferably from 1 ,000 to 10,000 ppmv, more preferably from 2,000 to 8,000 ppmv, more preferably from 3,000 to 7,500 ppmv, more preferably from 4,500 to 7,000 ppmv, more preferably from 5,000 to 6,500 ppmv.

31 . The process of any of embodiments 1 to 30, wherein the total amount of NH3, N2, and H2 comprised in the feed gas stream prepared in (ii) is in the range from 90 to 100 wt.-%, preferably from 95 to 99.95 vol.-%, more preferably from 98 to 99.9 vol.-%, more preferably from 99 to 99.85 vol.-%, and more preferably from 99.7 to 99.8 vol.-%.

32. The process of any of embodiments 1 to 31 , wherein after (i) and prior to (iii) the catalyst contained in the reactor provided in (i) is reduced in an atmosphere comprising hydrogen.

33. The process of embodiment 32, wherein the reduction is conducted at a temperature in the range of from 20 to 100 °C, preferably of from 24 to 50 °C, more preferably of from 26 to 35 °C, and more preferably of from 28 to 32 °C.

34. The process of embodiment 32 or 33, wherein the reduction is conducted in an atmosphere comprising from 1 to 50 vol.-% H2, preferably from 2 to 20 vol.-%, more preferably from 3 to 10 vol.-%, and more preferably from 4 to 6 vol-%.

35. The process of any of embodiments 32 to 34, wherein the atmosphere comprises from 50 to 99 vol.-% of an inert gas, preferably of from 80 to 98 vol.-%, more preferably of from 90 to 97 vol.-%, and more preferably from 94 to 96 vol.-%.

36. The process of any of embodiments 1 to 35, wherein the process is for the reforming of ammonia and hydrocarbons, wherein the feed gas stream prepared in (ii) further comprises one or more hydrocarbons, and one or more of CO2 and H2O, and wherein the effluent gas stream removed in (iv) further comprises CO.

37. The process of embodiment 36, wherein the feed gas stream prepared in (ii) further comprises CO2 and one or more hydrocarbons, and wherein the feed gas stream preferably comprises 5 vol.-% or less of H2O, more preferably 3 vol.-% or less, more preferably 1 vol.-% or less, more preferably 0.5 vol.-% or less, more preferably 0.1 vol.-% or less, more preferably 0.05 vol.-% or less, and more preferably 0.01 vol.-% or less of H2O.

38. The process of embodiment 36, wherein the feed gas stream prepared in (ii) further comprises H2O and one or more hydrocarbons, and wherein the feed gas stream preferably comprises 5 vol.-% or less of CO2, more preferably 3 vol.-% or less, more preferably 1 vol.-% or less, more preferably 0.5 vol.-% or less, more preferably 0.1 vol.-% or less, more preferably 0.05 vol.-% or less, and more preferably 0.01 vol.-% or less of CO2.

39. The process of embodiment 36, wherein the feed gas stream prepared in (ii) further comprises CO2, H2O, and one or more hydrocarbons.

40. The process of any of embodiments 36 to 39, wherein the one or more hydrocarbons are selected from the group consisting of alkanes and mixtures thereof, preferably of C1-C10 alkanes and mixtures thereof, more preferably of C3-C9 alkanes and mixtures thereof, more preferably of C4-C8 alkanes and mixtures thereof, more preferably of C5-C7 alkanes and mixtures thereof, more preferably of C6 alkanes and mixtures thereof.

41 . The process of any of embodiments 36 to 40, wherein contacting is performed at a pressure in the range of from greater than 10 to 50 bara, preferably of from 12 to 45 bara, more preferably of from 15 to 40 bara, more preferably of from 18 to 35 bara, and more preferably of from 20 to 30 bara.

42. The process of any of embodiments 36 to 41 , wherein the feed gas stream prepared in (ii) comprises from 0.1 to 75 vol.-% of NH3, preferably from 0.3 to 60 vol.-%, more preferably from 0.5 to 50 vol.-%, more preferably from 0.8 to 40 vol.-%, and more preferably from 1 to 30 vol.-%.

43. The process of any of embodiments 36 to 42, wherein the feed gas stream prepared in (ii) comprises from 10 to 70 vol.-% of the one or more hydrocarbons, preferably from 12 to 60 vol.-%, and more preferably from 15 to 50 vol.-%.

44. The process of any of embodiments 36 to 43, wherein the feed gas stream prepared in (ii) comprises from 0 to 75 vol.-% of H2O, preferably from 0.5 to 70 vol.-%, more preferably from 1 to 68 vol.-%, more preferably from 3 to 66 vol.-%, more preferably from 5 to 64 vol.-%, more preferably from 8 to 62 vol.-%, and more preferably from 10 to 60 vol.-%.

45. The process of any of embodiments 36 to 44, wherein the feed gas stream prepared in (ii) comprises from 0 to 60 vol.-% of CO2, preferably from 1 to 58 vol.-%, more preferably from 3 to 56 vol.-%, more preferably from 5 to 54 vol.-%, more preferably from 8 to 52 vol.-%, and more preferably from 10 to 50 vol.-%.

46. The process of any of embodiments 36 to 45, wherein the feed stream displays an H2O : C molar ratio of H2O to carbon contained in the one or more hydrocarbons in the range of from 0 to 4, preferably of from 0.1 to 3, more preferably of from 0.3 to 2.5, more preferably of from 0.4 to 2, and more preferably of from 0.5 to 1.6 47. The process of any of embodiments 36 to 46, wherein the feed stream displays a CO2 : C molar ratio of CO2 to carbon contained in the one or more hydrocarbons in the range of from 0 to 4, preferably of from 0.1 to 3, more preferably of from 0.2 to 2, and more preferably of from 0.3 to 1 .5.

48. The process of any of embodiments 36 to 47, wherein the feed stream displays an NH3 : C molar ratio of NH3 to carbon contained in the one or more hydrocarbons in the range of from 0 to 5, preferably of from 0 to 4, more preferably of from 0.001 to 3, more preferably of from 0.005 to 2, and more preferably of from 0.01 to 1.

49. The process of any of embodiments 1 to 48, wherein the feed stream is fed into the reactor at a gas hourly space velocity in the range of from 500 to 20,000 IT ¹ , preferably of from 500 to 16,000 IT ¹ , more preferably of from 700 to 14,000 IT ¹ , more preferably of from 800 to 12,000 IT ¹ , more preferably of from 900 to 10,000 IT ¹ , more preferably of from 1 ,000 to 8,000 IT ¹ , and more preferably of from 3,000 to 5,000 IT ¹ .

50. The process of any of embodiments 36 to 49, wherein the effluent gas stream removed in (iv) further comprises CO2.

51 . The process of any of embodiments 36 to 50, wherein the effluent gas stream removed in (iv) displays a stoichiometry number R in the range of from 0.1 to 3, wherein R is defined according to formula (I): wherein c(H2), c(CC>2), and c(CO) stand for the molar concentration of H2, CO2, and CO in the effluent gas stream, respectively.

52. The process of embodiment 51 , wherein the stoichiometry number R is in the range of from 1 to 2.5, preferably of from 1 .3 to 2.2.

53. The process of embodiment 51 , wherein R > 2.

54. The process of any of embodiments 36 to 50 and 53, wherein the effluent gas stream removed in (iv) displays an H2 : CO molar ratio of >2.

55. The process of embodiment 51 , wherein the stoichiometry number R is in the range of 0.5 to 3, preferably of from 1 to 2.2, and more preferably of 1 .3 to 1 .7.

56. The process of any of embodiments 36 to 55, wherein the effluent gas stream removed in

(iv) comprises from 10 to 90 vol.-% of H2, preferably from 20 to 80 vol.-%, more preferably from 30 to 70 vol.-%, more preferably from 40 to 65 vol.-%, and more preferably from 45 to 60 vol.-%. The process of any of embodiments 36 to 56, wherein the effluent gas stream removed in (iv) comprises from 1 to 70 vol.-% of CO, preferably from 3 to 50 vol.-%, more preferably from 5 to 40 vol.-%, more preferably from 10 to 35 vol.-%, and more preferably from 15 to 30 vol.-%. The process of any of embodiments 36 to 57, wherein the effluent gas stream removed in (iv) comprises from 1 to 50 vol.-% of CO2, preferably from 3 to 45 vol.-%, more preferably from 5 to 40 vol.-%, more preferably from 8 to 35 vol.-%, more preferably from 10 to 30 vol.-%, and more preferably from 12 to 25 vol.-%. The process of any of embodiments 1 to 58, wherein the effluent gas stream removed in (iv) is employed in a process for the production of methanol, for the production of dimethyl ether, or for the production of methanol and dimethylether. The process of any of embodiments 1 to 59, wherein the effluent gas stream removed in (iv) is employed in a process for the production of hydrocarbons, preferably according to the Fischer-Tropsch process. The process of any of embodiments 1 to 60, wherein the effluent gas stream removed in (iv) is employed in a process for the production of alcohols, preferably of alkanols, more preferably of C1 to C10 alkanols, more preferably of C2 to C8 alkanols, more preferably of C2 to C6 alkanols, more preferably of C2 to C4 alkanols, more preferably of C2 alkanols, and more preferably of ethanol. The process of any of embodiments 1 to 61 , wherein at an initial stage of the process, the feed gas stream prepared in (ii) and fed into the reactor in (iii) further comprises H2 for reducing the catalyst. The process of embodiment 62, wherein the feed gas stream prepared in (ii) and fed into the reactor in (iii) further comprises from 0.5 to 80 vol.-% of H2, preferably from 1 to 70 vol.-%, more preferably from 2 to 60 vol.-%, more preferably from 5 to 50 vol.-%, more preferably from 15 to 40 vol.-%. The process of embodiment 35, wherein the inert gas comprises one or more gases selected from the group consisting of noble gases, CO2, and nitrogen gas, preferably from the group consisting of He, Ar, Ne, and N2, CO2, wherein more preferably the inert gas comprises CO2, N2, or CO2 and N2, wherein more preferably the inert gas comprises N2, wherein more preferably the inert gas is N2. DESCRIPTION OF THE FIGURES

Figure 1 displays the results of NH3 reforming at a GHSV of 2000 IT ¹ , p(NH3)=30 bara and cofeeding of 10,000 ppm-vol of H2O. The catalysts were tested between 350 and 650 °C. The results obtained for 5 wt.-% of Ru on ZrO2, without (Catalyst from Example 1) and with (Catalyst from Example 2) 5 wt.-% KOH promotion is shown, as well as the results obtained with the Mg-AI-spinel support loaded with 2.5 wt.% Ru and promoted with 4.5 wt.% LiOH according to Example 3.

Figure 2 displays the results of NH3 reforming for the catalyst according to Example 2 at GHSV of 8000 IT ¹ , p(NH3)=10 bara and co-feeding of 5,000 ppm-vol of H2O. The catalyst was tested between 300 and 600 °C.

Figure 3 displays the XRD pattern of the catalyst of Example 3, wherein the Mg,AI-spinel structure is clearly identified as constituting support material.

EXPERIMENTAL SECTION

The present invention is further illustrated by the following examples.

Example 1 : Preparation of Ru (5 wt.-%) supported on ZrOz

Ru supported on Zr©2 was prepared according to Example 8 of WO 2015/086639 by impregnation of a ruthenium salt solution onto a zirconium oxide powder (D9-89, BASF, BET surface area: 78 m ² /g, pore volume: 0.84 ml/g), for obtaining Ru supported on ZrO2 at a loading of 5 wt.-%. The catalyst was then extruded to form extrudates having a diameter of 3 mm.

Example 2: Preparation of Ru (5 wt.-%) and KOH (5 wt.-%) supported on ZrOz

A 5 g sample of the 5 wt.-% Ru on ZrO2 extrudates as obtained from example 1 was subject to impregnation with a KOH solution. To this effect, 5 g of the extrudates obtained from Example 1 were split to form fractions in the range of 315 to 500 microns, which was then impregnated via incipient wetness impregnation with 0.25 g of KOH dissolved in 1 .65 ml of water. The sample was then dried at 120°C and subsequently calcined under inert atmosphere at 500°C for 2 hours.

Example 3: Preparation of Ru (2.5 wt.-%) and LiOH (4.5 wt.-%) supported on MgAhO4 spinel

A hydrotalcite precursor (Pural MG30 from Sasol) was calcined at 950 °C for 1 hour and used as support. 10 g of the support as split fractions of 315-500 microns were impregnated with 1 .41 g of RU(NO)(NOS)3 solution (19.7 wt.-% Ru in the solution), wherein prior to impregnation the solution was further mixed with 9.5 g of water and 1.38 g of Li(NOs). The solution was then impregnated on the support, dried at 120 °C for 2 h and calcined at 500 °C for 2 h under synthetic air consisting of 21 vol.-%C>2 and 79 vol.-% N2.

Example 4: Catalytic tests in NH3-reforming under high pressure

Prior to testing, the catalysts were activated in a reducing atmosphere of 5 % H2 in Ar at a temperature of 30 °C (dwell time 1 h, heating rate 2 °C/min). After activating the catalysts, the feed was applied (see tables below, NH3 + H2O + 5 vol.-% of Ar). In the respective tests, the pressure / NH3) was set to 1 , 10, 30, and 50 bara. The gas hourly space velocity (GHSV) with respect to the NH3 content was set to 2,000, 4,000, 8,000, or 16,000 IT ¹ . The temperatures were varied between 300 and 650 °C.

A 650 °C dwell time of 36 h served as an aging step to monitor the stability of the catalysts. The reference conversion at 450 °C was then measured after said aging step. As may be taken from the results shown in Table 1 , the deactivation was below 10 % of the initial activity.

Table 1 : Results from catalyst testing demonstrating the stability of the Ru/ZrC>2 system.

Table 2 shows the results from the experiment at a gas hourly space velocity (GHSV) of 2,000 h’ ¹ at p(NH3)=30 bara for the catalysts from Example 1-3, respectively. The H2O content in the feed was set 10,000 ppmvol. The temperature was increased in steps of 50 °C. The NH3- conversion is given in %. As may be taken from the results from testing displayed in Figure 1 , at 550 °C the catalysts approached equilibrium conversion, wherein the most active catalyst from Example 2 approaches equilibrium conversion already at 450 °C. Table 2: Results for the conversion of ammonia over the Ru-based catalysts of Examples 1 to 3.

Table 3 shows the NH3 conversion at a GHSV of 2,000 h’ ¹ at two reference temperatures at / NH ₃ )= 30 and 50 bara. The water content in the feed was set to 10,000 ppmv.

Table 3: Results for the conversion of ammonia at 30 and 50 bara (NH3) of the catalysts of Examples 1 and 2.

Table 4 shows the NH3 conversion of the most active 5 wt.-% Ru on ZrO ₂ promoted with 5 wt.-% of KOH. The experiments were conducted at 1 , 10 and 30 bara of ammonia / NH ₃ ). The temperatures were varied between 300 and 600 °C at a GHSV of 8000 IT ¹ . The water content in the feed was set to 5000 ppmv. As may be taken from the results from testing displayed in Figure 2, equilibrium conversion was reached by the catalyst according to Example 2 at 450°C, wherein almost 80% of NH3 conversion was already reached at 400 °C.

Table 4: Results for the catalyst of Example 2 in the conversion of ammonia at 400 °C and 1 , 10, and 30 bara of p(NH3) and at 10 bara and various temperatures.

Thus, as may be taken from the results obtained from the testing of the respective catalysts, a process is provided by the present invention which surprisingly affords a highly effective decomposition of ammonia at high pressures. Furthermore and quite unexpectedly, the process affords a highly effective decomposition at low temperatures despite the high pressure involved. In addition thereto, it has quite unexpectedly been found that the inventive process also affords a highly effective process despite the harsh hydrothermal conditions under high pressure due to water present during the ammonia decomposition reaction when using industrial grade ammonia which contains small amounts of water for stabilization purposes.

Example 5: Preparation of Ru (5 wt.-%) and KOH (5 wt.-%; corresponding to 3.5 wt.-% K) supported on MgAhO4 spinel

A hydrotalcite precursor (Pural MG30 from Sasol) was calcined at a temperature in the range of from 850 to 980 °C and for a duration in the range of 1 to 3 h, then used as support. 93 g of the support as molding were impregnated with 27 g of Ru(NO)(NOs)3 solution (19.7 wt.-% Ru in the solution). After drying at 180 °C for 4 h, the Ru containing molding were impregnated with 5.105 g of K(OH). The resulting material was then dried at 120 °C for 2 h and calcined at 500 °C for 2 h under synthetic air consisting of 21 vol.-% O2 and 79 vol.-% N2.

Example 6: Catalytic tests in NHs-reforming under high pressure

Prior to testing, the catalyst according to Example 4 was activated in a reducing atmosphere of 5 % H2 in Ar at a temperature of 30 °C (dwell time 1 h, heating rate 2 °C/min). After activating the catalyst, the feed was applied (see tables below, NH3 + H2O + 5 vol.-% of Ar). In the respective test, the pressure / NH3) was set to 30 bara. The gas hourly space velocity (GHSV) with respect to the NH3 content was set to 4,000 IT ¹ . The temperatures were varied between 300 and 650 °C. Table 5 shows the results from the experiment. The H2O content in the feed was set 5,000 vol- ume-ppm (ppmvol). The temperature was increased in steps of 50 °C. The NH ₃ -conversion is given in %. As may be taken from the results from testing displayed in Table 5, at 500 °C the catalyst approached equilibrium conversion.

Table 5: Results for the conversion of ammonia over the Ru-based catalyst of Example 5.

As for the testing of the catalysts of Examples 1-3, it may be taken from the results obtained from the testing of the catalyst of Example 5 that a process is provided by the present invention which surprisingly affords a highly effective decomposition of ammonia at high pressures. Furthermore and quite unexpectedly, the process affords a highly effective decomposition at low temperatures despite the high pressure involved. In addition thereto, it has quite unexpectedly been found that the inventive process also affords a highly effective process despite the harsh hydrothermal conditions under high pressure due to water present during the ammonia decomposition reaction when using industrial grade ammonia which contains small amounts of water for stabilization purposes.

Cited prior art:

- K. Lamb et. al. in int. J. of Hydrogen EnergylQ Q, 44, 3726-3736

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