TECHNICAL FIELD

The present invention relates to a process for hydroisomerization of alkanes, in particular of one or more of n-butane and n-pentane, wherein a catalyst is used comprising a zeolitic material wherein the framework of the zeolitic material comprises YO2 and X2O3, wherein Y is a tetravalent element and X is a trivalent element, wherein the zeolitic material has a molar ratio of Y:X in the range of from 1 :1 to 19:1 , and wherein the zeolitic material comprises one or more platinum group metals which are supported on the zeolitic material.

INTRODUCTION

Branched alkanes are often used as blending components for gasoline, since they can contribute to the octane number. Such branched alkanes are typically synthesized by hydroisomerization of alkanes, in particular n-butane and n-pentane. It is known to use bifunctional catalysts for the hydroisomerization of n-butane and n-pentane, for instance a catalyst comprising a zeolitic material impregnated with one or more of Pt and Pd, wherein the metal facilitates hydrogenation of alkenes and/or dehydrogenation of alkanes, and wherein the acidity properties of the zeolitic material facilitate skeletal hydroisomerization of alkanes by protonation of alkenes on the acid sites to give carbocations.

Li et al. in AppL CataL A 2017, vol. 537, p. 59-65 disclose a study on catalytic properties of Pt/WO _x -ZrC>2 and Pt/ZSM-22 with respect to skeletal isomerization of n-pentane. The used Pt/ZSM-22 catalyst comprises 0.5 weight-% Pt and the ZSM-22 has a Si/AI molar ratio of 36. The selectivity towards isopentane is reported as being well above 95 %.

Ye et al. in Journal of Catalysis 2018, vol. 360, p. 152-159 disclose a study on the effects of zeolite particle size and internal grain boundaries on Pt/Beta catalyzed isomerization of n- pentane. In particular, n-pentane hydroisomerization was tested over bifunctional Pt/Beta catalysts, by comparing the catalytic performance of four as-synthesized Pt/Beta samples that possess a Pt loading of 0.5 weight-%.

Tamizhdurai et al. in Microporous and Mesoporous Materials 2019, vol. 287, p. 192-202 disclose a study on the effect of acidity and porosity changes of Pt-containing dealuminated mordenite on n-pentane, n-hexane and light naphtha isomerization. As best performing catalyst in the isomerization of n-hexane as well as of n-pentane a zeolitic material having a MOR framework structure type, a silica to alumina ratio of 40, and comprising approximately 0.5 weight-% of Pt is reported. Zhao et al. in Progress in Reaction Kinetics and Mechanism 2020, vol. 45, p. 1-11 report on La- Ni-S2O8 ² 7ZrO2-Al2C>3 suitable as catalytic material for n-pentane isomerization. A selectivity towards isopentane of 88 % is reported for said catalytic material.

Lee et al. in J. Chin. Chem. Soc. 2021 , vol. 68, p. 409-420 disclose a study on the isomerization of n-pentane over Pt promoted tungstated zirconia supported on SBA-15 prepared by supercritical impregnation.

C.M. Lopez et aL, “n-Pentane Hydroisomerization of Pt Containing HZSM-5, HBEA and SAPO- 11 ” in CATALYSIS LETTERS; KLUVER ACADEMIC PUBLISHERS - PLENUM PUBLISHERS, NE, vol. 122, no. 3 - 4, March 14, 2008, p. 267 - 273 relates to a study of reactions of n-pentane on Pt-containing zeolites including H-ZSM-5.

P. Sazama et aL, “Superior activity of non-interacting close acidic protons in AL-rich Pt/H-*BEA zeolite in isomerization of n-hexane”, Applied Catalysis A: General, Elsevier, Amsterdam, NL, vol. 533, January 3 2017, p. 28 - 37 relates to a study of a relation between the local arrangement of active sites and skeletal isomerization of n-hexane in order to adapt the structure of zeolite catalysts to increase the reaction rates. A combination of synthesis of zeolites of *BEA structural topology with unique density and distribution of strongly acid sites is employed.

J. Moravkova et aL, “The effect of the nanoscale intimacy of platinum and acid centres on the hydroisomerization of short-chain alkanes”, Applied Catalysis A: General, Elsevier, Amsterdam, NL, vol. 6343, February 11 2022, 118535 concerns the analysis of the effect of the nanoscale intimacy of Pt metal and Bronsted acid sites on the hydroisomerization of n-pentane and n- hexane using a series of zeolite/binder composite catalysts with Pt located outside or inside of the zeolite crystal and with Pt dispersed in the zeolite crystal and its vicinity on the binder.

A hydroisomerization according to conventional methods has several drawbacks, in particular with respect to the yield of alkanes which is limited at high temperatures because of thermodynamic constraints. Additionally, side product formation, including coke formation and cracking of the alkane, further limits the hydroisomerization yield. Further, deactivation of the catalyst takes place due to coke formation, heavy (side-)products retention in the pores of the catalyst, diffusion limitations and mass transfer limitations because of the microporous structure of the catalyst.

Thus, there was a need to provide an improved process for the hydroisomerization of alkanes avoiding the disadvantages discussed above.

DETAILED DESCRIPTION

Therefore, it was an object of the present invention to provide a novel process for the hydroisomerization of one or more alkanes. In particular, it was an object of the present invention to provide a process for hydroisomerization of alkanes exhibiting a high conversion rate, while exhibiting a high selectivity towards the desired isomer, e. g. a selectivity towards isobutane or isopentane when n-butane and n-pentane are used as starting material respectively, and a low selectivity towards side-products. In addition thereto, it was an object of the present invention to provide in particular a process for the hydroisomerization of one or more alkanes wherein catalyst deactivation, especially coke formation, is reduced.

Surprisingly, it has been found that an improved process can be provided using a catalyst comprising a zeolitic material, wherein the framework of the zeolitic material comprises YO2 and X2O3, wherein Y is a tetravalent element and X is a trivalent element, wherein the zeolitic material has a molar ratio of Y:X in the range of from 1 :1 to 19:1 , and wherein the zeolitic material comprises one or more platinum group metals which are supported on the zeolitic material. It was surprisingly found that said process permits a hydroisomerization of one or more alkanes at high conversion rates. Further, it was found that a high selectivity towards the desired isomer can be achieved such that it can be prepared in high yields, whereby a comparatively low selectivity towards side-product was found. The process according to the present invention was also found to achieve said benefits at comparatively low temperatures. Thus, it has surprisingly been found that the formation of undesired by-products, in particular of one or more of methane, ethane and propane, can be suppressed. In addition thereto, it has surprisingly been found that dimerization reactions can be suppressed by the process according to the present invention.

Therefore, the present invention relates to a process for hydroisomerization of one or more alkanes, the process comprising

(i) providing a catalyst comprising a zeolitic material, wherein the framework of the zeolitic material comprises YO2 and X2O3, wherein Y is a tetravalent element and X is a trivalent element, wherein the zeolitic material has a molar ratio of Y:X in the range of from 1 :1 to 19:1 , wherein the zeolitic material comprises one or more platinum group metals which are supported on the zeolitic material;

(ii) contacting a feed stream comprising H2 and one or more alkanes with the catalyst according to (i), for obtaining a product stream.

It is preferred that the zeolitic material exhibits a molar ratio of Y to X in the range of from 1 to 16, more preferably in the range of from 2 to 14, more preferably in the range of from 3 to 13, more preferably in the range of from 4 to 12, more preferably in the range of from 4 to 11 .

It is preferred that the zeolitic material has a 3-dimensional pore structure.

It is preferred that the zeolitic material comprises a mor composite building unit. Within the meaning of the present application the term „mor composite building unit" refers to the mor (t- tes) composite building unit as described in van Koningsveld, H., “Compendium of Zeolite Framework Types: Building Schemes and Type Characteristics”, Elsevier Science 2007. It is preferred that the zeolitic material comprising the one or more platinum group metals exhibits a ratio of the Bronsted acid site density to the Lewis acid site density in the range of from 1.4:1 to 20:1 , more preferably in the range of from 1.4:1 to 15:1 , more preferably in the range of from 1.5:1 to 10:1 , more preferably in the range of from 1.6:1 to 8:1 , more preferably in the range of from 1.6:1 to 6:1 , more preferably in the range of from 1.7:1 to 4.7:1 , more preferably in the range of from 1.8:1 to 4.4:1 , more preferably in the range of from 2.0:1 to 4.4:1 , more preferably in the range of from 2.5:1 to 4.4:1 , more preferably in the range of from 3.0:1 to 4.4:1 , more preferably in the range of from 3.3:1 to 4.4:1 , more preferably in the range of from 3.6:1 to 4.4:1 , more preferably in the range of from 3.9:1 to 4.4:1 , more preferably in the range of from 4.0:1 to 4.4:1 , wherein the Bronsted acid site density and the Lewis acid site density are preferably determined according to Reference Example 1.

It is preferred that the zeolitic material comprising the one or more platinum group metals exhibits a Bronsted acid site density in the range of from 100 to 5000 pmol/g, more preferably in the range of from 150 to 3000 pmol/g, more preferably in the range of from 200 to 2500 pmol/g, more preferably in the range of from 300 to 2000 pmol/g, more preferably in the range of from 400 to 1700 pmol/g, more preferably in the range of from 500 to 1500 pmol/g, more preferably in the range of from 550 to 1400 pmol/g, more preferably in the range of from 600 to 1300 pmol/g, more preferably in the range of from 610 to 1290 pmol/g, more preferably in the range of from 700 to 1280 pmol/g, more preferably in the range of from 800 to 1280 pmol/g, more preferably in the range of from 900 to 1270 pmol/g, more preferably in the range of from 1000 to 1270 pmol/g, more preferably in the range of from 1100 to 1260 pmol/g, more preferably in the range of from 1200 to 1260 pmol/g, preferably determined as described in Reference Example 1.

Within the meaning of the present invention, the Bronsted acid site density of a given zeolitic material refers to the Bronsted acid site density of the zeolitic material comprising one or more platinum group metals. Same applies accordingly with regard to the Lewis acid site density of a given zeolitic material according to the present invention.

It is preferred that the zeolitic material comprising the one or more platinum group metals exhibits a Lewis acid site density in the range of from 50 to 800 pmol/g, more preferably in the range of from 160 to 700 pmol/g, more preferably in the range of from 190 to 600 pmol/g, more preferably in the range of from 210 to 500 pmol/g, more preferably in the range of from 230 to 450 pmol/g, more preferably in the range of from 250 to 400 pmol/g, more preferably in the range of from 260 to 380 pmol/g, more preferably in the range of from 270 to 360 pmol/g, more preferably in the range of from 280 to 350 pmol/g, more preferably in the range of from 280 to 330 pmol/g, more preferably in the range of from 280 to 310 pmol/g, more preferably in the range of from 280 to 300 pmol/g, preferably determined as described in Reference Example 1.

It is preferred that Y comprised in the zeolitic material is selected from the group consisting of Si, Sn, Ti, Zr, Ge, and mixtures of two or more thereof, more preferably from the group consisting of Si, Ti, Zr, and mixtures of two or more thereof, wherein Y is more preferably Si. It is preferred that X comprised in the zeolitic material is selected from the group consisting of B, Al, Ga, In, and mixtures of two or more thereof, more preferably from the group consisting of Al, Ga, and a mixture thereof, wherein X is more preferably Al.

It is preferred that the zeolitic material has a framework structure containing rings with 10 T- atoms, with 12 T-atoms, or with 10 and 12 T-atoms, wherein the zeolitic material more preferably has a framework structure containing rings with 12 T-atoms.

It is preferred that the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, more preferably from the group consisting of BEA, MFI, MSE, and intergrowth structure types of two or more thereof, wherein the zeolitic material preferably has a BEA or MSE framework structure type.

In the case where the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, it is preferred according to a first alternative that the zeolitic material having a BEA framework structure type is obtained from an organotemplate mediated synthesis or obtained from an organotemplate-free synthesis, preferably obtained from an organo- template-free synthesis.

Further in the case where the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, it is preferred according to a second alternative that the zeolitic material has a BEA framework structure type, and wherein the zeolitic material is selected from the group consisting of zeolite beta, Tschernichite, [B-Si-O]-*BEA, CIT-6, [Ga-Si-O]-*BEA, Beta polymorph B, SSZ-26, SSZ-33, Beta polymorph A, [Ti-Si-O]-*BEA, pure silica beta, and mixtures of two or more thereof, more preferably from the group consisting of zeolite beta, CIT- 6, Beta polymorph B, SSZ-26, SSZ-33, Beta polymorph A, pure silica beta, and mixtures of two or more thereof, wherein the zeolitic material having a BEA framework structure type more preferably is zeolite beta.

In the case where the zeolitic material has a BEA framework structure type, and wherein the zeolitic material is selected from the group consisting of zeolite beta, Tschernichite, [B-Si-O]- *BEA, CIT-6, [Ga-Si-O]-*BEA, Beta polymorph B, SSZ-26, SSZ-33, Beta polymorph A, [Ti-Si-O]- *BEA, pure silica beta, and mixtures of two or more thereof, it is preferred that the zeolite beta is obtained from an organotemplate mediated synthesis or obtained from an organotemplate-free synthesis, more preferably obtained from an organotemplate-free synthesis.

Further in the case where the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, it is preferred according to a third alternative that the zeolitic material has a MSE framework structure type, and wherein the zeolitic material is selected from the group consisting of UZM-35, MCM-68, AI-MCM-68, YNU-2, AI-YNU-3, and mixtures of two or more thereof, wherein the zeolitic material having a MSE framework structure type more preferably is UZM-35 or MCM-68, more preferably UZM-35.

Further in the case where the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, it is preferred according to a third alternative that the zeolitic material has a MFI framework structure type, and wherein the zeolitic material is selected from the group consisting of Silicalite, ZSM-5, [Fe-Si-O]-MFI, [Ga-Si-O]-MFI, [As-Si-O]-MFI, AMS-1 B, AZ-1 , Bor-C, Encilite, Boralite C, FZ-1 , LZ-105, Mutinaite, NU-4, NU-5, TS-1 , TSZ, TSZ-III, TZ- 01 , USC-4, USI-108, ZBH, ZKQ-1 B, ZMQ-TB, MnS-1 , FeS-1 , and mixtures of two or more thereof, more preferably from the group consisting of Silicalite, ZSM-5, AMS-1 B, AZ-1 , Encilite, FZ-1 , LZ-105, Mutinaite, NU-4, NU-5, TS-1 , TSZ, TSZ-III, TZ-01 , USC-4, USI-108, ZBH, ZKQ- 1 B, ZMQ-TB, and mixtures of two or more thereof, wherein the zeolitic material having an MFI framework structure type more preferably is one or more of Silicalite and ZSM-5, preferably ZSM-5.

It is preferred that the one or more platinum group metals are selected from the group consisting of Ru, Os, Rh, Ir, Pd, Pt, and mixtures of two or more thereof, more preferably from the group consisting of Pd, Pt, and a mixture thereof, wherein the one or more platinum group metals more preferably is Pt.

It is preferred that the zeolitic material comprises the one or more platinum group metals, preferably Pt, in an amount in the range of from 0.1 to 5 weight-%, preferably in the range of from 0.2 to 2.5 weight-%, more preferably in the range of from 0.3 to 0.8 weight-%, more preferably in the range of from 0.4 to 0.6 weight-%, calculated as sum of the one or more platinum group metals as elements and based on the weight of the zeolitic material.

It is preferred that the zeolitic material comprises the one or more platinum group metals in elemental form and/or as counter-ion at an ion exchange site of the framework structure of the zeolitic material, wherein more preferably the zeolitic material comprises the one or more platinum group metals in elemental form.

It is preferred that the zeolitic material comprises the one or more platinum group metals in the form of nanoparticles, wherein the nanoparticles more preferably have an average particle size in the range of from 10 to 30 angstrom, preferably in the range of from 15 to 25 angstrom, more preferably in the range of from 18 to 22 angstrom, preferably determined according to Reference Example 3.

It is preferred that providing the catalyst according to (i) comprises

(1.1 ) providing a zeolitic material;

(1.2) supporting one or more platinum group metals on the zeolitic material according to (i.1 ); (1.3) optionally washing the zeolitic material obtained in (i.2) with water, preferably with deionized water;

(1.4) optionally drying the zeolitic material obtained in (i.2) or (i.3) in a gas atmosphere;

(1.5) optionally shaping the zeolitic material obtained in (i.2), (i.3), or (i.4);

(1.6) optionally calcining the zeolitic material obtained in (i.2), (i.3), (i.4), or (i.5) in a gas atmosphere;

(1.7) optionally subjecting the one or more platinum group metals supported on the zeolitic material obtained in (i.2), (i.3), (i.4), (i.5), or (i.6) to a reduction procedure in a gas atmosphere comprising H2; to obtain the catalyst.

In the context of the present invention, supporting a platinum group metal on a zeolitic material can be understood as supporting said platinum group metal into the pores of the porous structure of the zeolitic material and optionally on the surface of the zeolitic material.

It is preferred that providing the catalyst according to (i) comprises

(i.1 ’) providing a zeolitic material;

(i.2’) shaping the zeolitic material provided in (i.1 ’);

(i.3’) supporting one or more platinum group metals on the zeolitic material obtained in (i.2’);

(i.4’) optionally washing the zeolitic material obtained in (i.3’) with water, preferably with deionized water;

(i.5’) optionally drying the zeolitic material obtained in (i.3’) or (i.4’) in a gas atmosphere;

(i.6’) optionally calcining the zeolitic material obtained in (i.3’), (i.4’), or (i.5’) in a gas atmosphere;

(i.7’) optionally subjecting the one or more platinum group metals supported on the zeolitic material obtained in (i.3’), (i.4’), (i.5’), or (i.6’) to a reduction procedure in a gas atmosphere comprising H2; to obtain the catalyst.

In the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that shaping according to (i.5) or (i.2’) comprises pelletizing, tableting, or extruding.

Further in the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that providing the zeolitic material according to (i.1 ) or (i.1 ’) comprises preparing the zeolitic material by an organotem- plate mediated synthesis or by an organotemplate-free synthesis, more preferably by an organ- otemplate-free synthesis. It is preferred that supporting the one or more platinum group metals on the zeolitic material according to (i.2) or (i.3’) comprises subjecting the zeolitic material to one or more ion-exchange procedures using an aqueous solution of the one or more platinum group metals.

In the case where supporting the one or more platinum group metals on the zeolitic material according to (i.2) or (i.3’) comprises subjecting the zeolitic material to one or more ion-exchange procedures using an aqueous solution of the one or more platinum group metals, it is preferred that the one or more platinum metals comprise, preferably consist of, Pt, and wherein the aqueous solution of the one or more platinum group metals comprises one or more of an ammine stabilized hydroxo Pt(ll) complex, hexachloroplatinic acid, potassium hexachloroplatinate, plati- num(ll) nitrate, and ammonium hexachloroplatinate, more preferably one or more of tetraammineplatinum chloride, preferably tetraammineplatinum chloride hydrate, platinum(ll) nitrate, and tetraammineplatinum nitrate, preferably tetraammineplatinum nitrate hydrate, wherein the aqueous solution of the one or more platinum group metals more preferably comprises tetraammineplatinum chloride, more preferably tetraammineplatinum chloride hydrate.

Further in the case where the process further comprises (i.1 ), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that drying the zeolitic material in a gas atmosphere according to (i.4) or (i.5’) is performed at a temperature of the gas atmosphere in the range of from 30 to 200 °C, preferably in the range of from 35 to 160 °C, more preferably in the range of from 40 to 120 °C, more preferably in the range of from 40 to 80 °C, more preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C.

Further in the case where the process further comprises (i.1 ), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that the gas atmosphere in (i.4) or (i.5’) comprises one or more of N2 and O2, wherein the gas atmosphere more preferably comprises, more preferably consists of, air.

Further in the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that drying the zeolitic material in a gas atmosphere according to (i.4) or (i.5’) is performed for a duration in the range of from 1 to 28 h, preferably in the range of from 2 to 24 h, more preferably in the range of from 5 to 20 h, more preferably in the range of from 8 to 16 h, more preferably in the range of from 10 to 14 h.

Further in the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally (i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that calcining the zeolitic material in a gas atmosphere comprising O2 according to (i.6) or (i.6’) is performed at a temper- ature of the gas atmosphere in the range of from 300 to 500 °C, more preferably in the range of from 350 to 450 °C, more preferably in the range of from 375 to 425 °C.

Further in the case where the process further comprises (i.1 ), (i.2), optionally (i.3), optionally

(i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that the gas atmosphere comprising O2 in (i.6) or (i.6’) further comprises one or more of N2 and Ar, wherein the gas atmosphere comprising O2 in (i.6) or (i.6’) preferably comprises air, wherein preferably from 95 to 100 volume-%, preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume- %, of the gas atmosphere comprising O2 consists of O2. Alternatively, it is preferred that from 1 to 25 volume-%, preferably from 1 .5 to 22 volume-%, more preferably from 2.0 to 5 volume-%, of the gas atmosphere comprising O2 in (i.6) or (i.6’) consists of O2.

Further in the case where the process further comprises (i.1 ), (i.2), optionally (i.3), optionally

(i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1 ’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that calcining the zeolitic material in a gas atmosphere according to (i.6) or (i.6’) is performed for a duration in the range of from 2 to 6 h, more preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h.

Further in the case where the process further comprises (i.1 ), (i.2), optionally (i.3), optionally

(i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that subjecting the one or more platinum group metals supported on the zeolitic material to a reduction procedure in a gas atmosphere comprising H2 according to (i.7) or (i.7’) is performed at a temperature of the gas atmosphere in the range of from 300 to 500 °C, more preferably in the range of from 350 to 450 °C, more preferably in the range of from 375 to 425 °C.

Further in the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally

(i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that the gas atmosphere comprising H2 in (i.7) or (i.7’) further comprises one or more of nitrogen and argon, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the gas atmosphere comprising H2 in (i.7) or (i.7’) consists of H2. Alternatively, it is preferred that from 1 to 50 volume-%, more preferably from 3 to 30 volume-%, more preferably from 4 to 25 volume-%, of the gas atmosphere comprising H2 in (i.7) or (i.7’) consists of H2.

Further in the case where the process further comprises (i.1), (i.2), optionally (i.3), optionally

(i.4), optionally (i.5), optionally (i.6), and optionally (i.7), or (i.1’), (i.2’), optionally (i.3’), optionally (i.4’), optionally (i.5’), optionally (i.6’), and optionally (i.7’), it is preferred that subjecting the one or more platinum group metals supported on the zeolitic material to a reduction procedure in a gas atmosphere comprising H2 according to (i.7) or (i.7’) is performed for a duration in the range of from 2 to 6 h, more preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h.

It is preferred that the catalyst is provided in (i) in a fixed-bed or in a fluidized bed, preferably in a fixed bed.

It is preferred that the catalyst consists of the zeolitic material and the one or more platinum group metals.

It is preferred that the one or more alkanes comprise, preferably consist of, (C4-C2o)alkanes, preferably (C4-Cis)alkanes, more preferably (C4-Ci2)alkanes, more preferably (C4-Cw)alkanes, more preferably (C4-Cs)alkanes, more preferably (C4-Ce)alkanes, more preferably (C4- Cs)alkanes, wherein the one or more alkanes are preferably linear, wherein the one or more alkanes more preferably comprise, preferably consist of, one or more of n-hexane, n-pentane and n-butane.

It is preferred that the one or more alkanes comprise, preferably consist of, n-butane, and wherein the product stream comprises isobutane.

It is preferred that the one or more alkanes comprise, preferably consist of, n-pentane, and wherein the product stream comprises isopentane.

It is preferred that the contacting according to (ii) is effected at a temperature in the range of from 240 to 395 °C, more preferably in the range of from 260 to 385 °C, more preferably in the range of from 270 to 375 °C, more preferably in the range of from 280 to 365 °C, more preferably in the range of from 290 to 355 °C, more preferably in the range of from 300 to 350 °C, more preferably in the range of from 305 to 345 °C.

It is preferred that the contacting according to (ii) is effected at a total pressure in the range of from 0.5 to 1.5 bar(abs), more preferably in the range of from 0.8 to 1.2 bar(abs), more preferably in the range of from 0.9 to 1.1 bar(abs), wherein the total pressure is more preferably 1 bar(abs), wherein the total pressure is calculated as sum of the partial pressure of H2 and the partial pressure of the one or more alkanes. Alternatively, it is preferred, in particular with respect to large scale processes, that the contacting according to (ii) is effected at a total pressure in the range of from 1 to 60 bar(abs), more preferably in the range of from 5 to 55 bar(abs), more preferably in the range of from 10 to 50 bar(abs), wherein the total pressure is calculated as sum of the partial pressure of H2 and the partial pressure of the one or more alkanes.

It is preferred that the contacting according to (ii) is effected at a partial pressure of the one or more alkanes in the range of from 0.07 to 0.32 bar(abs), more preferably in the range of from 0.12 to 0.27 bar(abs), more preferably in the range of from 0.14 to 0.25 bar(abs). It is preferred that the contacting according to (ii) is effected at a partial pressure of the one or more alkanes in the range of from 0.68 to 0.93 bar(abs), more preferably in the range of from 0.73 to 0.88 bar(abs), more preferably in the range of from 0.75 to 0.86 bar(abs).

It is preferred that the feed stream comprising H2 and one or more alkanes according to (ii) has a weight hourly space velocity in the range of from 0.1 to 30 IT ¹ , more preferably in the range of from 1 to 20 IT ¹ , more preferably in the range of from 3 to 15 IT ¹ , more preferably in the range of from 3.5 to 14 IT ¹ . Alternatively, it is preferred, in particular with respect to large scale processes, that the feed stream comprising H2 and one or more alkanes according to (ii) has a weight hourly space velocity in the range of from 0.1 to 10 IT ¹ , more preferably in the range of from 0.25 to 6 IT ¹ , more preferably in the range of from 0.5 to 4 IT ¹ .

It is preferred that the feed stream comprising H2 and one or more alkanes according to (ii) has a molar ratio of H2, calculated as molar amount of H2, to the one or more alkanes, calculated as sum of the molar amounts of the one or more alkanes, 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 4:1 to 6:1 , more preferably in the range of from 4.6:1 to 5.8:1 , more preferably in the range of from 4.8:1 to 5.67:1 . Alternatively, it is preferred, in particular with respect to large scale processes, that the feed stream comprising H2 and one or more alkanes according to (ii) has a molar ratio of H2, calculated as molar amount of H2, to the one or more alkanes, calculated as sum of the molar amounts of the one or more alkanes, in the range of from 1 :10 to 20:1 , more preferably in the range of from 1 :5 to 10:1 , more preferably in the range of from 1 :2 to 4:1.

It is preferred that from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the feed stream comprising H2 and one or more alkanes according to (ii) consists of H2 and the one or more alkanes.

It is preferred that the process further comprises

(iii) treating the catalyst obtained in (ii), (i .2), (i.3), (i.4), (i.5), (i.6), (i.7), (i.3’), (i.4’), (i.5’), (i .6’), or (i.7’) with a gas atmosphere comprising O2;

(iv) treating the catalyst obtained in (iii) with a gas atmosphere comprising H2; for regenerating the catalyst.

In the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iii) with a gas atmosphere comprising O2 is performed at a temperature of the gas atmosphere comprising O2 in the range of from 450 to 650 °C, more preferably in the range of from 500 to 600 °C, more preferably in the range of from 525 to 575 °C.

Further in the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iii) with a gas atmosphere comprising O2 is performed for a duration in the range of from 1 to 20 h, preferably in the range of from 1.5 to 16 h, more preferably in the range of from 2 to 6 h, more preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h. Further in the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iii) with a gas atmosphere comprising O2 comprises heating of the gas atmosphere comprising O2 with a heating rate in the range of from 0.5 to 1 .5 °C/minute, more preferably in the range of from 0.9 to 1.1 °C/minute.

Further in the case where the process further comprises (iii) and (iv), it is preferred that the gas atmosphere comprising O2 according to (iii) further comprises one or more of N2 and Ar, wherein the gas atmosphere comprising O2 in (i.6) or (i.6’) preferably comprises air, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-% of the gas atmosphere comprising O2 according to (iii) consists of O2. Alternatively, it is preferred that from 1 to 25 volume-%, preferably from 1 .5 to 22 volume-%, more preferably from 2.0 to 5.0 volume-%, of the gas atmosphere comprising O2 according to (iii) consists of O2.

Further in the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iv) with a gas atmosphere comprising H2 is performed at a temperature of the gas atmosphere comprising H2 in the range of from 300 to 700 °C, more preferably in the range of from 400 to 600 °C, more preferably in the range of from 450 to 550 °C, more preferably in the range of from 475 to 525 °C.

Further in the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iv) with a gas atmosphere comprising H2 is performed for a duration in the range of from 1 to 10 h, more preferably in the range of from 2 to 6 h, more preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h.

Further in the case where the process further comprises (iii) and (iv), it is preferred that treating the catalyst according to (iv) with a gas atmosphere comprising H2 comprises heating of the gas atmosphere comprising H2 with a heating rate in the range of from 0.5 to 1.5 °C/minute, more preferably in the range of from 0.9 to 1.1 °C/minute.

Further in the case where the process further comprises (iii) and (iv), it is preferred that the gas atmosphere comprising H2 according to (iv) further comprises one or more of N2 and Ar, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-% of the gas atmosphere comprising H2 according to (iv) consists of H2. Alternatively, it is preferred that from 1 to 50 volume-%, more preferably from 3 to 30 vol- ume-%, more preferably from 4 to 25 volume-%, of the gas atmosphere comprising H2 according to (iv) consists of H2.

The unit bar(abs) refers to an absolute pressure wherein 1 bar equals 10 ⁵ Pa.

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 hydroisomerization of one or more alkanes, the process comprising

(i) providing a catalyst comprising a zeolitic material, wherein the framework of the zeolitic material comprises YO2 and X2O3, wherein Y is a tetravalent element and X is a trivalent element, wherein the zeolitic material has a molar ratio of Y:X in the range of from 1 :1 to 19:1 , wherein the zeolitic material comprises one or more platinum group metals which are supported on the zeolitic material;

(ii) contacting a feed stream comprising H2 and one or more alkanes with the catalyst according to (i), for obtaining a product stream.

2. The process of embodiment 1 , wherein the zeolitic material exhibits a molar ratio of Y to X in the range of from 1 to 16, preferably in the range of from 2 to 14, more preferably in the range of from 3 to 13, more preferably in the range of from 4 to 12, more preferably in the range of from 4 to 11 .

3. The process of embodiment 1 or 2, wherein the zeolitic material has a 3-dimensional pore structure.

4. The process of any one of embodiments 1 to 3, wherein the zeolitic material comprises a mor composite building unit.

5. The process of any one of embodiments 1 to 4, wherein the zeolitic material comprising the one or more platinum group metals exhibits a ratio of the Bronsted acid site density to the Lewis acid site density in the range of from 1 .4:1 to 20:1 , preferably in the range of from 1.4:1 to 15:1 , more preferably in the range of from 1.5:1 to 10:1 , more preferably in the range of from 1.6:1 to 8:1 , more preferably in the range of from 1.6:1 to 6:1 , more preferably in the range of from 1 .7:1 to 4.7:1 , more preferably in the range of from 1 .8:1 to 4.4:1 , more preferably in the range of from 2.0:1 to 4.4:1 , more preferably in the range of from 2.5:1 to 4.4:1 , more preferably in the range of from 3.0:1 to 4.4:1 , more preferably in the range of from 3.3:1 to 4.4:1 , more preferably in the range of from 3.6:1 to 4.4:1 , more preferably in the range of from 3.9:1 to 4.4:1 , more preferably in the range of from 4.0:1 to 4.4:1 , wherein the Bronsted acid site density and the Lewis acid site density are preferably determined according to Reference Example 1 . 6. The process of any one of embodiments 1 to 5, wherein the zeolitic material comprising the one or more platinum group metals exhibits a Bronsted acid site density in the range of from 100 to 5000 pmol/g, preferably in the range of from 150 to 3000 pmol/g, more preferably in the range of from 200 to 2500 pmol/g, more preferably in the range of from 300 to 2000 pmol/g, more preferably in the range of from 400 to 1700 pmol/g, more preferably in the range of from 500 to 1500 pmol/g, more preferably in the range of from 550 to 1400 pmol/g, more preferably in the range of from 600 to 1300 pmol/g, more preferably in the range of from 610 to 1290 pmol/g, more preferably in the range of from 700 to 1280 pmol/g, more preferably in the range of from 800 to 1280 pmol/g, more preferably in the range of from 900 to 1270 pmol/g, more preferably in the range of from 1000 to 1270 pmol/g, more preferably in the range of from 1100 to 1260 pmol/g, more preferably in the range of from 1200 to 1260 pmol/g, preferably determined as described in Reference Example 1.

7. The process of any one of embodiments 1 to 6, wherein the zeolitic material comprising the one or more platinum group metals exhibits a Lewis acid site density in the range of from 50 to 800 pmol/g, preferably in the range of from 160 to 700 pmol/g, more preferably in the range of from 190 to 600 pmol/g, more preferably in the range of from 210 to 500 pmol/g, more preferably in the range of from 230 to 450 pmol/g, more preferably in the range of from 250 to 400 pmol/g, more preferably in the range of from 260 to 380 pmol/g, more preferably in the range of from 270 to 360 pmol/g, more preferably in the range of from 280 to 350 pmol/g, more preferably in the range of from 280 to 330 pmol/g, more preferably in the range of from 280 to 310 pmol/g, more preferably in the range of from 280 to 300 pmol/g, preferably determined as described in Reference Example 1.

8. The process of any one of embodiments 1 to 7, wherein Y comprised in the zeolitic material is selected from the group consisting of Si, Sn, Ti, Zr, Ge, and mixtures of two or more thereof, preferably from the group consisting of Si, Ti, Zr, and mixtures of two or more thereof, wherein Y is more preferably Si.

9. The process of any one of embodiments 1 to 8, wherein X comprised in the zeolitic material is selected from the group consisting of B, Al, Ga, In, and mixtures of two or more thereof, preferably from the group consisting of Al, Ga, and a mixture thereof, wherein X is more preferably AL

10. The process of any one of embodiments 1 to 9, wherein the zeolitic material has a framework structure containing rings with 10 T-atoms, with 12 T-atoms, or with 10 and 12 T- atoms, wherein the zeolitic material preferably has a framework structure containing rings with 12 T-atoms.

11 . The process of any one of embodiments 1 to 10, wherein the zeolitic material has a framework structure type selected from the group consisting of BEA, FAU, FER, ITH, MFI, MOR, MSE, MWW, YFI, and intergrowth structure types of two or more thereof, preferably from the group consisting of BEA, MFI, MSE, and intergrowth structure types of two or more thereof, wherein the zeolitic material preferably has a BEA or MSE framework structure type.

12. The process of embodiment 11 , wherein the zeolitic material having a BEA framework structure type is obtained from an organotemplate mediated synthesis or obtained from an organotemplate-free synthesis, preferably obtained from an organotemplate-free synthesis.

13. The process of embodiment 11 , wherein the zeolitic material has a BEA framework structure type, and wherein the zeolitic material is selected from the group consisting of zeolite beta, Tschernichite, [B-Si-O]-*BEA, CIT-6, [Ga-Si-O]-*BEA, Beta polymorph B, SSZ-26, SSZ-33, Beta polymorph A, [Ti-Si-O]-*BEA, pure silica beta, and mixtures of two or more thereof, more preferably from the group consisting of zeolite beta, CIT-6, Beta polymorph B, SSZ-26, SSZ-33, Beta polymorph A, pure silica beta, and mixtures of two or more thereof, wherein the zeolitic material having a BEA framework structure type more preferably is zeolite beta.

14. The process of embodiment 13, wherein the zeolite beta is obtained from an organotemplate mediated synthesis or obtained from an organotemplate-free synthesis, preferably obtained from an organotemplate-free synthesis.

15. The process of embodiment 11 , wherein the zeolitic material has a MSE framework structure type, and wherein the zeolitic material is selected from the group consisting of UZM- 35, MCM-68, AI-MCM-68, YNU-2, AI-YNU-3, and mixtures of two or more thereof, wherein the zeolitic material having a MSE framework structure type preferably is UZM-35 or MCM-68, more preferably UZM-35.

16. The process of embodiment 11 , wherein the zeolitic material has a MFI framework structure type, and wherein the zeolitic material is selected from the group consisting of Sili- calite, ZSM-5, [Fe-Si-O]-MFI, [Ga-Si-O]-MFI, [As-Si-O]-MFI, AMS-1 B, AZ-1 , Bor-C, En- cilite, Boralite C, FZ-1 , LZ-105, Mutinaite, NU-4, NU-5, TS-1 , TSZ, TSZ-III, TZ-01 , USC-4, USI-108, ZBH, ZKQ-1 B, ZMQ-TB, MnS-1 , FeS-1 , and mixtures of two or more thereof, preferably from the group consisting of Silicalite, ZSM-5, AMS-1 B, AZ-1 , Encilite, FZ-1 , LZ-105, Mutinaite, NU-4, NU-5, TS-1 , TSZ, TSZ-III, TZ-01 , USC-4, USI-108, ZBH, ZKQ-

1 B, ZMQ-TB, and mixtures of two or more thereof, wherein the zeolitic material having an MFI framework structure type more preferably is one or more of Silicalite and ZSM-5, preferably ZSM-5.

17. The process of any one of embodiments 1 to 16, wherein the one or more platinum group metals are selected from the group consisting of Ru, Os, Rh, Ir, Pd, Pt, and mixtures of two or more thereof, preferably from the group consisting of Pd, Pt, and a mixture thereof, wherein the one or more platinum group metals more preferably is Pt. 18. The process of any one of embodiments 1 to 17, wherein the zeolitic material comprises the one or more platinum group metals, preferably Pt, in an amount in the range of from 0.1 to 5 weight-%, preferably in the range of from 0.2 to 2.5 weight-%, more preferably in the range of from 0.3 to 0.8 weight-%, more preferably in the range of from 0.4 to 0.6 weight-%, calculated as sum of the one or more platinum group metals as elements and based on the weight of the zeolitic material.

19. The process of any one of embodiments 1 to 18, wherein the zeolitic material comprises the one or more platinum group metals in elemental form and/or as counter-ion at an ion exchange site of the framework structure of the zeolitic material, wherein preferably the zeolitic material comprises the one or more platinum group metals in elemental form.

20. The process of any one of embodiments 1 to 19, wherein the zeolitic material comprises the one or more platinum group metals in the form of nanoparticles, wherein the nanoparticles preferably have an average particle size in the range of from 10 to 30 angstrom, preferably in the range of from 15 to 25 angstrom, more preferably in the range of from 18 to 22 angstrom, preferably determined according to Reference Example 3.

21 . The process of any one of embodiments 1 to 20, wherein providing the catalyst according to (i) comprises

(1.1) providing a zeolitic material;

(1.2) supporting one or more platinum group metals on the zeolitic material according to (i-1);

(1.3) optionally washing the zeolitic material obtained in (i.2) with water, preferably with de-ionized water;

(1.4) optionally drying the zeolitic material obtained in (i.2) or (i.3) in a gas atmosphere;

(1.5) optionally shaping the zeolitic material obtained in (i.2), (i.3), or (i.4);

(1.6) optionally calcining the zeolitic material obtained in (i.2), (i.3), (i.4), or (i.5) in a gas atmosphere;

(1.7) optionally subjecting the one or more platinum group metals supported on the zeolitic material obtained in (i.2), (i.3), (i.4), (i.5), or (i.6) to a reduction procedure in a gas atmosphere comprising H2; to obtain the catalyst.

22. The process of any one of embodiments 1 to 20, wherein providing the catalyst according to (i) comprises

(i.T) providing a zeolitic material;

(i.2’) shaping the zeolitic material provided in (i.T);

(i.3’) supporting one or more platinum group metals on the zeolitic material obtained in (i.2’);

(i.4’) optionally washing the zeolitic material obtained in (i.3’) with water, preferably with de-ionized water; (i.5’) optionally drying the zeolitic material obtained in (i.3’) or (i.4’) in a gas atmosphere; (i.6’) optionally calcining the zeolitic material obtained in (i.3’), (i.4’), or (i.5’) in a gas atmosphere;

(i.7’) optionally subjecting the one or more platinum group metals supported on the zeolitic material obtained in (i.3’), (i.4’), (i.5’), or (i.6’) to a reduction procedure in a gas atmosphere comprising H2; to obtain the catalyst. The process of embodiment 21 or 22, wherein shaping according to (i.5) or (i.2’) comprises pelletizing, tableting, or extruding. The process of any one of embodiments 21 to 23, wherein providing the zeolitic material according to (i.1) or (i.T) comprises preparing the zeolitic material by an organotemplate mediated synthesis or by an organotemplate-free synthesis, preferably by an organotem- plate-free synthesis. The process of any one of embodiments 21 to 24, wherein supporting the one or more platinum group metals on the zeolitic material according to (i.2) or (i.3’) comprises subjecting the zeolitic material to one or more ion-exchange procedures using an aqueous solution of the one or more platinum group metals. The process of embodiment 25, wherein the one or more platinum metals comprise, preferably consist of, Pt, and wherein the aqueous solution of the one or more platinum group metals comprises one or more of an ammine stabilized hydroxo Pt(ll) complex, hexachlo- roplatinic acid, potassium hexachloroplatinate, platinum(ll) nitrate, and ammonium hexachloroplatinate, more preferably one or more of tetraammineplatinum chloride, preferably tetraammineplatinum chloride hydrate, platinum(ll) nitrate, and tetraammineplatinum nitrate, preferably tetraammineplatinum nitrate hydrate, wherein the aqueous solution of the one or more platinum group metals more preferably comprises tetraammineplatinum chloride, more preferably tetraammineplatinum chloride hydrate. The process of any one of embodiments 21 to 26, wherein drying the zeolitic material in a gas atmosphere according to (i.4) or (i.5’) is performed at a temperature of the gas atmosphere in the range of from 30 to 200 °C, preferably in the range of from 35 to 160 °C, more preferably in the range of from 40 to 120 °C, more preferably in the range of from 40 to 80 °C, preferably in the range of from 50 to 70 °C, more preferably in the range of from 55 to 65 °C. The process of any one of embodiments 21 to 27, wherein the gas atmosphere in (i.4) or (i.5’) comprises one or more of N2 and O2, wherein the gas atmosphere preferably comprises, more preferably consists of, air. 29. The process of any one of embodiments 21 to 28, wherein drying the zeolitic material in a gas atmosphere according to (i.4) or (i.5’) is performed for a duration in the range of from 1 to 28 h, preferably in the range of from 2 to 24 h, more preferably in the range of from 5 to 20 h, preferably in the range of from 8 to 16 h, more preferably in the range of from 10 to 14 h.

30. The process of any one of embodiments 21 to 29, wherein calcining the zeolitic material in a gas atmosphere comprising O2 according to (i.6) or (i.6’) is performed at a temperature of the gas atmosphere in the range of from 300 to 500 °C, preferably in the range of from 350 to 450 °C, more preferably in the range of from 375 to 425 °C.

31 . The process of any one of embodiments 21 to 30, wherein the gas atmosphere comprising O2 in (i.6) or (i.6’) further comprises one or more of N2 and Ar, wherein the gas atmosphere comprising O2 in (i.6) or (i.6’) preferably comprises air, wherein preferably from 95 to 100 volume-%, preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the gas atmosphere comprising O2 consists of O2, or wherein preferably from 1 to 25 volume-%, preferably from 1 .5 to 22 volume-%, more preferably from 2.0 to 5.0 volume-%, of the gas atmosphere comprising O2 in (i.6) or (i.6’) consists of O2.

32. The process of any one of embodiments 21 to 31 , wherein calcining the zeolitic material in a gas atmosphere according to (i.6) or (i.6’) is performed for a duration in the range of from 2 to 6 h, preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h.

33. The process of any one of embodiments 21 to 32, wherein subjecting the one or more platinum group metals supported on the zeolitic material to a reduction procedure in a gas atmosphere comprising H2 according to (i.7) or (i.7’) is performed at a temperature of the gas atmosphere in the range of from 300 to 500 °C, preferably in the range of from 350 to 450 °C, more preferably in the range of from 375 to 425 °C.

34. The process of any one of embodiments 21 to 33, wherein the gas atmosphere comprising H2 in (i.7) or (i.7’) further comprises one or more of nitrogen and argon, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the gas atmosphere comprising H2 in (i.7) or (i.7’) consists of H2, or wherein preferably from 1 to 50 volume-%, more preferably from 3 to 30 volume-%, more preferably from 4 to 25 volume-%, of the gas atmosphere comprising H2 in (i.7) or (i.7’) consists of H2.

35. The process of any one of embodiments 21 to 34, wherein subjecting the one or more platinum group metals supported on the zeolitic material to a reduction procedure in a gas atmosphere comprising H2 according to (i.7) or (i.7’) is performed for a duration in the range of from 2 to 6 h, preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h. 36. The process of any one of embodiments 1 to 35, wherein the catalyst is provided in (i) in a fixed-bed or in a fluidized bed, preferably in a fixed bed.

37. The process of any one of embodiments 1 to 36, wherein the catalyst consists of the zeo- litic material and the one or more platinum group metals.

38. The process of any one of embodiments 1 to 37, wherein the one or more alkanes comprise, preferably consist of, (C4-C2o)alkanes, preferably (C4-Cis)alkanes, more preferably (C4-Ci2)alkanes, more preferably (C4-Cw)alkanes, more preferably (C4-Cs)alkanes, more preferably (C4-Ce)alkanes, more preferably (C4-Cs)alkanes, wherein the one or more alkanes are preferably linear, wherein the one or more alkanes more preferably comprise, preferably consist of, one or more of n-hexane, n-pentane and n-butane.

39. The process of any one of embodiments 1 to 38, wherein the one or more alkanes comprise, preferably consist of, n-butane, and wherein the product stream comprises isobutane.

40. The process of any one of embodiments 1 to 39, wherein the one or more alkanes comprise, preferably consist of, n-pentane, and wherein the product stream comprises isopentane.

41 . The process of any one of embodiments 1 to 40, wherein the contacting according to (ii) is effected at a temperature in the range of from 240 to 395 °C, preferably in the range of from 260 to 385 °C, more preferably in the range of from 270 to 375 °C, more preferably in the range of from 280 to 365 °C, more preferably in the range of from 290 to 355 °C, more preferably in the range of from 300 to 350 °C, more preferably in the range of from 305 to 345 °C.

42. The process of any one of embodiments 1 to 41 , wherein the contacting according to (ii) is effected at a total pressure in the range of from 0.5 to 1.5 bar(abs), preferably in the range of from 0.8 to 1 .2 bar(abs), more preferably in the range of from 0.9 to 1 .1 bar(abs), wherein the total pressure is more preferably 1 bar(abs), wherein the total pressure is calculated as sum of the partial pressure of H2 and the partial pressure of the one or more alkanes, or wherein the contacting according to (ii) is effected at a total pressure in the range of from 1 to 60 bar(abs), preferably in the range of from 5 to 55 bar(abs), more preferably in the range of from 10 to 50 bar(abs), wherein the total pressure is calculated as sum of the partial pressure of H2 and the partial pressure of the one or more alkanes.

43. The process of any one of embodiments 1 to 42, wherein the contacting according to (ii) is effected at a partial pressure of the one or more alkanes in the range of from 0.07 to 0.32 bar(abs), preferably in the range of from 0.12 to 0.27 bar(abs), more preferably in the range of from 0.14 to 0.25 bar(abs). 44. The process of any one of embodiments 1 to 43, wherein the contacting according to (ii) is effected at a partial pressure of the one or more alkanes in the range of from 0.68 to 0.93 bar(abs), preferably in the range of from 0.73 to 0.88 bar(abs), more preferably in the range of from 0.75 to 0.86 bar(abs).

45. The process of any one of embodiments 1 to 44, wherein the feed stream comprising H2 and one or more alkanes according to (ii) has a weight hourly space velocity in the range of from 0.1 to 30 IT ¹ , preferably in the range of from 1 to 20 IT ¹ , more preferably in the range of from 3 to 15 IT ¹ , more preferably in the range of from 3.5 to 14 IT ¹ , or wherein the feed stream comprising H2 and one or more alkanes according to (ii) has a weight hourly space velocity in the range of from 0.1 to 10 IT ¹ , preferably in the range of from 0.25 to 6 IT ¹ , more preferably in the range of from 0.5 to 4 IT ¹ .

46. The process of any one of embodiments 1 to 45, wherein the feed stream comprising H2 and one or more alkanes according to (ii) has a molar ratio of H2, calculated as molar amount of H2, to the one or more alkanes, calculated as sum of the molar amounts of the one or more alkanes, 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 4:1 to 6:1 , more preferably in the range of from 4.6:1 to 5.8:1 , more preferably in the range of from 4.8:1 to 5.67:1 , or wherein the feed stream comprising H2 and one or more alkanes according to (ii) has a molar ratio of H2, calculated as molar amount of H2, to the one or more alkanes, calculated as sum of the molar amounts of the one or more alkanes, in the range of from 1 : 10 to 20: 1 , preferably in the range of from 1 :5 to 10: 1 , more preferably in the range of from 1 :2 to 4: 1 .

47. The process of any one of embodiments 1 to 46, wherein from 95 to 100 volume-%, preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the feed stream comprising H2 and one or more alkanes according to (ii) consists of H2 and the one or more alkanes.

48. The process of any one of embodiments 1 to 47, further comprising

(iii) treating the catalyst obtained in (ii), (i.2), (i .3), (i.4), (i.5), (i.6), (i.7), (i.3’), (i.4’), (i .5’), (i.6’), or (i.7’) with a gas atmosphere comprising O2;

(iv) treating the catalyst obtained in (iii) with a gas atmosphere comprising H2; for regenerating the catalyst.

49. The process of embodiment 48, wherein treating the catalyst according to (iii) with a gas atmosphere comprising O2 is performed at a temperature of the gas atmosphere comprising O2 in the range of from 450 to 650 °C, preferably in the range of from 500 to 600 °C, more preferably in the range of from 525 to 575 °C.

50. The process of embodiment 48 or 49, wherein treating the catalyst according to (iii) with a gas atmosphere comprising O2 is performed for a duration in the range of from 1 to 20 h, preferably in the range of from 1.5 to 16 h, more preferably in the range of from 2 to 6 h, preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h. The process of any one of embodiments 48 to 50, wherein treating the catalyst according to (iii) with a gas atmosphere comprising O2 comprises heating of the gas atmosphere comprising O2 with a heating rate in the range of from 0.5 to 1 .5 °C/minute, preferably in the range of from 0.9 to 1.1 °C/minute. The process of any one of embodiments 48 to 51 , wherein the gas atmosphere comprising O2 according to (iii) further comprises one or more of N2 and Ar, wherein the gas atmosphere comprising O2 in (iii) preferably comprises air, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-% of the gas atmosphere comprising O2 according to (iii) consists of O2, or wherein preferably 1 to 25 volume-%, preferably from 1.5 to 22 volume-%, more preferably from 2.0 to 5.0 volume-%, of the gas atmosphere comprising O2 according to (iii) consists of O2. The process of any one of embodiments 48 to 52, wherein treating the catalyst according to (iv) with a gas atmosphere comprising H2 is performed at a temperature of the gas atmosphere comprising H2 in the range of from 300 to 700 °C, preferably in the range of from 400 to 600 °C, more preferably in the range of from 450 to 550 °C, more preferably in the range of from 475 to 525 °C. The process of any one of embodiments 48 to 53, wherein treating the catalyst according to (iv) with a gas atmosphere comprising H2 is performed for a duration in the range of from 1 to 10 h, preferably in the range of from 2 to 6 h, more preferably in the range of from 3 to 5 h, more preferably in the range of from 3.5 to 4.5 h. The process of any one of embodiments 48 to 54, wherein treating the catalyst according to (iv) with a gas atmosphere comprising H2 comprises heating of the gas atmosphere comprising H2 with a heating rate in the range of from 0.5 to 1 .5 °C/minute, preferably in the range of from 0.9 to 1.1 °C/minute. The process of any one of embodiments 48 to 55, wherein the gas atmosphere comprising H2 according to (iv) further comprises one or more of N2 and Ar, wherein preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-% of the gas atmosphere comprising H2 according to (iv) consists of H2, or wherein preferably 1 to 50 volume-%, more preferably from 3 to 30 volume- %, more preferably from 4 to 25 volume-%, of the gas atmosphere comprising H2 according to (iv) consists of H2. The present invention is further illustrated by the following Reference Examples, Examples and Comparative examples.

EXAMPLES

Reference Example 1 : Determination of the Lewis acid site density and of the Bronsted acid site density

The type of acid sites and acid site densities were determined by pyridine adsorption infrared spectroscopy (Py-FTIR), measured on a Thermo Scientific Nicolet 6700 FT-IR spectrometer equipped with a DTGS detector. The sample was pressed into a self-supporting wafer and activated under vacuum at 400 °C for 1 h. A reference spectrum was collected at 150 °C. 25 mbar of pyridine was passed over the sample wafer at 50 °C until saturation, after which weakly coordinated pyridine was removed at this temperature by evacuation. The IR spectra were collected at 150 °C and the quantification of adsorbed pyridine was done using integrated band areas of the difference spectrum and Emeis’ integrated molar extinction coefficients for the corresponding characteristic bands (Bronsted acid sites at 1545 cm ^-1 and Lewis acid sites at 1450 cm ^-1 ) (see C. A. Emeis: “Determination of integrated molar extinction coefficients for infrared absorption bands of pyridine adsorbed on solid acid catalysts” in Journal of Catalysis 1993, vol. 141 , p. 347-354 and M. Velthoen et al. “Probing acid sites in solid catalysts with pyridine UV-Vis spectroscopy” in Physical Chemistry Chemical Physics 2018, vol. 20, p. 21647-21659 as regards the determination of acidity properties of a material via spectroscopy and the interpretation of the resulting data).

Reference Example 2: Powder X-ray diffraction

Powder X-ray diffractograms were recorded on a Malvern Panalytical Empyrean diffractometer in transmission/Debye-Scherrer geometry (1.3° < 2theta < 45°, 0.013° step size) with a PIXcel3D detector.

Reference Example 3: Metal dispersion and particle size determinations

For metal dispersion and particle size determinations, CO chemisorption experiments were performed on a Quantachrome ChemBET PULSAR. The sample was first reduced in hydrogen at 200 °C, then the sample was pulsed with CO (Air Liquide N37) and flushed with He alternately. Analysis was done under the assumption of a stoichiometry of 0.5 CO molecule per surface Pt atom.

Reference Example 4: Determination of chemical compositions

Chemical compositions of the samples were measured by inductively coupled plasma-optical emission spectroscopy (ICP-OES) using a Varian 720-ES. Reference Example 5: Preparation of Pt-containing catalysts

To prepare a Pt-containing catalyst with ion-exchange, the target amount of tetraammineplati- num(ll) chloride hydrate (Sigma-Aldrich, 98%) was first dissolved in Milli Q ultrapure water, and then added dropwise to a stirred suspension of zeolitic material (25 mL(water)/g(zeolitic material)). After the mixture was left stirring overnight at room temperature, the samples were washed with Milli Q ultrapure water and subsequently dried at 60 °C overnight. Samples were pelletized to sizes of 250-500 micrometer before calcination in oxygen at 400 °C for 4 h at a heating rate of 1 °C/min, followed by a repetition of the program in a reductive atmosphere of hydrogen. An overview of the prepared catalysts is given in table 1 below.

Table 1 :

Overview of zeolitic materials used as catalysts.

Acid site properties of the catalysts according to Reference Examples 10a and 11a are shown in table 2 below.

Table 2

Acid site properties of the catalysts according to Reference Examples 10a and 11a as determined according to Reference Example 1.

Example 1 : n-butane skeletal hydroisomerization

N-butane hydroisomerization was performed in a fixed bed reactor at atmospheric pressure with a stainless steel tube (inner diameter 4.4 mm). In the catalytic test, a pelletised catalyst (250- 500 micrometer) was pre-treated in hydrogen (Air Liquide, alphal) at 300 °C for 1 h prior to the reaction. In the case of the zeolitic material according to Reference Example 15 50 mg were used as catalyst, in the case of the zeolitic material according to Reference Example 10a 200 mg were used as catalyst, and in the case of the zeolitic material according to Reference Example 11a 50 mg were used as catalyst. A binary mixture of hydrogen and n-butane (Air Liquide, N25) was fed into the reactor. The H2:n-butane ratio was kept at 5.67 and the weight hourly space velocity (WHSV) of n-butane was 3.5 h ^-1 . The gaseous products were analyzed using an on-line gas chromatograph (Shimadzu GC-2010 Plus) equipped with a flame ionization detector (FID) and a GsBP PLOT-Q capillary column (30 m * 0.53 mm * 30 micrometer).

The results are shown in figures 1-2 and table 3 below, wherein table 3 shows the data for the diagram shown in figure 2.

Table 3

Results for the catalytic testing according to Example 1 for the catalyst according to Reference Example 11a.

As can be gathered from table 3 above, the zeolitic materials according to Reference Examples 10a and 11a achieved a high conversion of n-butane as a catalyst, in particular at temperatures equal or greater than 340 °C. Also, said catalysts achieved a high selectivity towards isobutane.

In contrast thereto, the zeolitic material having CON framework structure and a Si: Al molar ratio of 50 did not show any catalytic activity, in particular no conversion of n-butane was observed.

Example 2: n-pentane skeletal hydroisomerization

N-pentane hydroisomerization was performed in a fixed bed reactor at atmospheric pressure with a stainless steel tube (inner diameter 4.4 mm). In the catalytic test, 0.06 g of a pelletized catalyst (250-500 micrometer) was pre-treated in hydrogen (Air Liquide, N40) at 300 °C for 1 h prior to the reaction, then cooled to the reaction temperature. Afterwards, n-pentane (Fisher Chemical, > 99 %) was introduced into the reactor by bubbling hydrogen into a saturator containing n-pentane, maintained at 0 °C throughout the reaction. An additional hydrogen flow was added to achieve a 4.8 molar ratio of H2:n-pentane, before this binary mixture is passed over the catalyst. The WHSV of n-pentane was 14 h ^-1 . The gaseous products were analyzed using an on-line gas chromatograph (Shimadzu GC-2010 Plus) equipped with a flame ionization detector (FID) and a GsBP PLOT-Q capillary column (30 m * 0.53 mm * 30 micrometer).

The results are shown in figures 3-6. As can be seen from said figures, the zeolitic materials according to Reference Examples 10a, 10b, 11a, and 12 achieved a high conversion of n- pentane as a catalyst, especially at a temperature of 300 °C. Further, said zeolitic materials achieved a high selectivity towards isopentane.

In contrast thereto, the zeolitic material having BEA framework structure and a Si:AI molar ratio of 60 showed a comparatively lower catalytic activity, in particular a comparatively lower conversion of n-pentane was observed.

Brief description of figures

Figure 1 : shows the catalytic performance of the catalyst according to Reference Example 10a of the present invention in the n-butane skeletal hydroisomerization according to Example 1. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isobutane yield in %. Figure 2: shows the catalytic performance of the catalyst according to Reference Example 11a of the present invention in n-butane skeletal hydroisomerization according to Example 1. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isobutane yield in %.

Figure 3: shows the catalytic performance of the catalyst according to Reference Example 12 of the present invention in n-pentane skeletal hydroisomerization according to Example 2. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isopentane yield in %.

Figure 4: shows the catalytic performance of the catalyst according to Reference Example 10b of the present invention in n-pentane skeletal hydroisomerization according to Example 2. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isopentane yield in %.

Figure 5: shows the catalytic performance of the catalyst according to Reference Example 10a of the present invention in n-pentane skeletal hydroisomerization according to Example 2. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isopentane yield in %.

Figure 6: shows the catalytic performance of the catalyst according to Reference Example 11a of the present invention in n-pentane skeletal hydroisomerization according to Example 2. The temperature [°C] is shown on the abscissa, and the selectivity [%] as well as the conversion [%] on the ordinate. Diamonds indicate the conversion, and crosses indicate the isopentane yield in %.

Cited literature

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G. Ye et al. “Effects of zeolite particle size and internal grain boundaries on Pt/Beta catalyzed isomerization of n-pentane” in Journal of Catalysis 2018, vol. 360, p. 152-159

P. Tamizhdurai et al. “Effect of acidity and porosity changes of dealuminated mordenite on n-pentane n-hexane and light naphtha isomerization” in Microporous and Mesoporous Materials 2019, vol. 287, p. 192-202

H. Zhao et al. “Influence of sulfating method on La-Ni-S2O8 ^2- /ZrO2-Al2O3 solid superacid catalyst for n-pentane isomerization” in Progress in Reaction Kinetics and Mechanism 2020, vol. 45, p. 1-11 - W. Lee et al. “Isomerization of n-pentane over platinum promoted tungstated zirconia supported on mesoporous SBA-15 prepared by supercritical impregnation” in J. Chin. Chem. Soc. 2021 , vol. 68, p. 409-420

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