WO2025031974A1

WO2025031974A1 - A process for the hydrodeoxygenation and hydrocracking of sustainable feedstocks

Info

Publication number: WO2025031974A1
Application number: PCT/EP2024/071982
Authority: WO
Inventors: Ivana JEVTOVIKJ; Stephan A Schunk; Alexander Czaja; Feelly RUETHER; Alois Kindler; Piyush Ingale; Reni GRAUKE
Original assignee: BASF SE
Current assignee: BASF SE
Priority date: 2023-08-04
Filing date: 2024-08-02
Publication date: 2025-02-13
Anticipated expiration: 2026-02-04

Abstract

The present invention relates to a process for the hydrodeoxygenation and hydrocracking of a feed comprising, preferably consisting of, (1) providing a feed MF comprising one or more oxygen containing compounds comprising, independently of one another, one or more alkyl chains, wherein the alkyl chains have, independently of one another, a length n with 4 ≤ n ≤ 30; (2) providing a heterogeneous catalyst comprising a zeolitic material loaded with one or more metals; (3) subjecting the feed MF provided according to (1) to hydrodeoxygenation and hydrocracking conditions in a reaction space S, said conditions comprising contacting the mixture MF with the catalyst provided according to (2) in a reducing gas atmosphere, obtaining in said reaction space S a reaction mixture comprising one or more alkanes having a chain length m with m < n.

Description

A process for the hydrodeoxygenation and hydrocracking of sustainable feedstocks

TECHNICAL FIELD

The present invention relates to a hydrodeoxygenation and hydrocracking process for a sustainable feedstock comprising one or more of an oil or a fat of vegetable or animal origin, and a pyrolysis oil for the production of a mixture of liquefied petroleum gas (LPG) and/or naphtha grades.

INTRODUCTION

Hydrocracking is used to break long-chain hydrocarbons into shorter hydrocarbons. Catalytic hydrocracking is typically carried out over bifunctional catalysts in a hydrogen atmosphere at pressures between 40-200 bar, temperatures between 300-600 °C. If the process takes place at medium pressure between 40 to 80 bar, it is referred to as mild hydrocracking (MHC). The bifunctional catalysts used contain a de-/hydrogenation and an acid functionality, e.g. nickel, molybdenum or noble metals on alumina, zeolites or other aluminosilicates.

The mechanism of hydrocracking by bifunctional catalysts can proceed through a) acid catalyzed formation of carbonium- and carbenium intermediates from alkanes or alternatively through b) dehydrogenation of the n-alkanes at the active metal site, followed by conversion of the formed alkene at the acid sites of the zeolite to a carbenium ion intermediate. The carbenium ion intermediate can either undergo an isomerization reaction to branched alkenes or - scission to smaller hydrocarbons followed by a final hydrogenation of the branched or cracked unsaturated hydrocarbons.

WO 2019/229072 A1 relates to a two-step process for the conversion of a feedstock comprising at least 50 wt.-% related to the total weight of the feedstock of triglycerides, fatty acid esters and/or fatty acids having at least 10 carbon atoms into diesel fuel, jet fuel, naphtha and liquefied petroleum gas.

EP 2770040 A2 relates to processes for the production of bio-hydrocarbons and the use of totally hydrogenated animal and/or vegetable oils as feedstock for a cracker.

US 2013/0116491 A1 relates to a process for hydro treatment of a feed from renewable sources such as vegetable oils for the production of paraffinic hydrocarbons comprising a pre-treatment step by crystallisation and/or precipitation and pre-hydrogenation of the feed.

WO 2009/011160 A1 relates to process for producing a hydrocarbon oil, wherein in the presence of hydrogen, a raw oil containing an oxygenous organic compound and a water-insoluble chlorinous compound is brought into contact with a hydrogenation catalyst composed of a support containing a porous inorganic oxide and, supported thereon, at least one metal selected from among those of Group VIA and Group VIII of the periodic table so as to form a hydrocarbon oil and water through hydrogenation deoxygenation of the oxygenous organic compound and convert the water-insoluble chlorinous compound to a water-soluble chlorinous compound, thereby obtaining a reaction product containing the hydrocarbon oil, water and the water-soluble chlorinous compound.

JP 5273724 B2 relates to a catalyst for hydrocracking comprising a porous solid oxide modified by a metal belonging to group 10 of the periodic table or a compound containing the same and a metal belonging to group 6 or 7 of the periodic table or a compound containing the same, and is used in hydrocracking triglyceride and manufacturing 15-18C hydrocarbons.

WO 2023/099658 A1 relates to a process for production of a hydrocarbon fraction from an oxygenate feedstock, comprising the steps of providing a process feed comprising an amount of an ammonia precursor, hydrogen and an amount of oxygenates at a temperature above 200°C, directing said process feed to contact a material catalytically active in hydrodeoxygenation (HDO) under hydrotreating conditions to provide a hydrodeoxygenated intermediate product, wherein said ammonia precursor provides an amount of ammonia corresponding to a partial pressure of NH3 in the presence of said material catalytically active in hydrodeoxygenation being at least 0.1 mbar.

Despite the advances made in the hydrocracking of suitable feedstocks, there remains the need for energy- and cost-efficient hydrocracking processes, in particular with regard to feedstocks stemming from sustainable sources.

DETAILED DESCRIPTION

Thus, it was an object of the present invention to provide an improved process for the hydrocracking of sustainable feedstocks. Said object is achieved by the one-step process of the present invention, consisting of a selective zeolite-catalysed hydrocracking of sustainable feedstocks towards LPG and/or naphtha grade cracking products. In particular, It has surprisingly been found that a highly efficient one-step process for the hydrocracking of sustainable feedstocks, in particular with regard to the product selectivity towards LPG and/or naphtha grade cracking products, may be provided by the inventive process.

In the following, the term hydrodeoxygenation preferably refers to a chemical conversion reaction involving the removal of oxygen atoms from the oxygen containing compound and the addition of hydrogen to the cleaved portion. In the following, the term hydrocracking preferably refers to a process of breaking hydrocarbons with carbon chains of a certain length (alkyl chain length of n) into hydrocarbons with shorter carbon chains (alkyl chain length of m, with m < n).

Therefore, the present invention relates to a process for the hydrodeoxygenation and hydrocracking of a feed comprising, preferably consisting of,

(1 ) providing a feed MF comprising one or more oxygen containing compounds comprising, independently of one another, one or more alkyl chains, wherein the alkyl chains have, independently of one another, a length n with 4 < n < 30;

(2) providing a heterogeneous catalyst comprising a zeolitic material loaded with one or more metals;

(3) subjecting the feed MF provided according to (1 ) to hydrodeoxygenation and hydrocracking conditions in a reaction space S, said conditions comprising contacting the mixture MF with the catalyst provided according to (2) in a reducing gas atmosphere, obtaining in said reaction space S a reaction mixture comprising one or more alkanes having a chain length m with m < n.

It is preferred that the process further comprises

(4) removing a product mixture MP from the reaction space S, wherein the mixture MP comprises the one or more alkanes having a chain length m with m < n.

It is preferred that 1 < m < 18, preferably 2 < m < 16, more preferably 2 < m < 14, more preferably 3 < m < 10.

It is preferred that 4 < n < 28, preferably 5 < n < 24, more preferably 6 < n < 22, more preferably 8 < n < 20.

It is preferred that the one or more oxygen containing compounds comprised in the feed MF in (1 ) have one or more functional groups selected from the group consisting of a carboxylic acid group, a ketone group, an aldehyde group, an ester group, an ether group, an acetal group, a lactone group, or a hydroxyl group.

It is preferred that the feed MF provided according to (1 ) has a content in oxygen stemming from the one or more oxygen containing compounds in the range of from 0.1 to 50 wt.-%, based on the total weight of the one or more oxygen containing compounds, preferably from 0.1 to 40 wt.- %, more preferably from 0.1 to 30 wt.-%, more preferably from 0.2 to 20 wt.-%, more preferably from 0.5 to 10 wt.-%.

It is preferred that the feed MF provided according to (1) has a content of the one or more oxygen containing compounds in the range of from 1 to 100 wt.-%, based on the total weight of the feed MF, preferably from 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%. It is preferred that the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that the one or more oxygen containing compounds comprise, preferably consists of, waste materials, preferably of waste materials of biomaterials and/or plastics, more preferably waste materials selected from the group consisting of vegetable oils, animal fats, pyrolysis oils and derivatives thereof.

Sustainable cracking feedstocks

It is possible that a feedstock obtained from the recycling of mixed chemical waste is used as feed stock for the inventive hydrocracking process. The chemical recycling of mixed plastic waste leads to a recycled oil, generally referred to as pyrolysis oil. Major components of such mixed plastic waste may include, but are not limited to, polyethylenes, polypropylenes, polyethylene terephthalates, polystyrenes, copolymers of one or more of the foregoing, block polymers of one or more of the foregoing, graft copolymers of one or more of the foregoing, and mixtures of two or more of the foregoing. Prior to using a pyrolysis oil as feedstock for a cracker process, it may be necessary to subject it to a suitable purification including, but not being restricted to, catalytic methods and/or adsorption methods.

It is also possible that bionaphtha is used as feedstock for the cracking process. Bionaphtha may be preferably produced from vegetable oils, preferably from waste food vegetable oil and/or non-food vegetable oil. Typically, it is obtained by transesterification of the vegetable oil by reaction of the oil with an alcohol, such as usually methanol, in the presence of a suitable catalyst. The reaction results in the formation of fatty acid methyl esters (FAMEs), which are the main component of bionaphtha. Vegetable oils which may be used include, but are not limited to, soybean oil, canola oil, sunflower oil, rapeseed oil, corn oil, palm oil, peanut oil, cottonseed oil, jatropha oil, algal oil.

It is preferred that the one or more oxygen containing compounds in the feed MF in (1) are selected from the group consisting of triglycerides of vegetable or animal origin, derivates of triglycerides of vegetable or animal origin, and mixtures thereof.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that the vegetable oil is selected from the group consisting of palm oil, soybean oil, rapeseed oil, sunflower oil, linseed oil, rice bran oil, maize oil, olive oil, castor oil, sesame oil, pine oil, peanut oil, mustard oil, palm kernel oil, hempseed oil, coconut oil, babassu oil, cottonseed oil, jatropha oil, used cooking oils, oils derived from algae, corn oil, safflower oil, sunflower oil, almond oil, beech nut oil, brazil nut oil, cashew oil, hazelnut oil, macadamia oil, mongongo nut oil, pecan oil, pistachio oil, walnut oil, pumpkin seed oil, amaranth oil, argan oil, ben oil, date seed oil, dika oil, false flax oil, grape seed oil, hemp oil, kapok seed oil, kenaf seed oil, marula oil, meadowfoam seed oil, okra seed oil, perilla seed oil, persimmon seed oil, pequi oil, pili nut oil, poppyseed oil, pracaxi oil, quinoa oil, colza oil, radish oil, safflower oil, tigernut oil, tung oil and mixtures of two or more thereof.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that the animal fat is selected from the group consisting of tallow, lard, grease, fish oil, butterfat, milk fat, and mixtures of two or more thereof.

It is preferred that the feed MF in (1) comprises 50 wt.-% or more of fatty acid esters and/or free fatty acids, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more of fatty acid esters and/or free fatty acids.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that animal fats and vegetable oils are at least partially hydrogenated, preferably hydrogenated.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that the feed MF in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

In the case where the feed MF in (1) comprises, preferably consists of, pyrolysis oil of biogenic nature, it is preferred that the pyrolysis oil of biogenic nature is selected from the group consisting of wood, straw, scrap wood, and mixtures of two or more thereof.

In the case where the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof, it is preferred that the feed MF in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms.

In the case where the feed MF in (1) comprises, preferably consists of, pyrolysis oil, it is preferred that the feed MF in (1) comprises 50 wt.-% or more of pyrolysis oil, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more, more preferably 95 wt.-% or more of pyrolysis oil.

It is preferred that the zeolitic material in (2) has an AFR, AFS, AFY, BEA, BEC, BOG, BOZ, BPH, CON, CSV, DFO, EMT, EON, EWF, FAU, FER, GME, IFW, IMF, ISV, ITE, ITG, ITH, ITR, IWR, IWS, IWV, IWW, JSR, KFI, LTA, LTF, LTL, MEI, MEL, MER, MFI, MFS, MOR, MOZ, MSE, MWF, MWW, NES, OBW, OFF, OKO, OSO, PAU, PGR, POS, PWN, RHO, RTH, SAO, SAV, SBS, SBT, SEW, SFG, SFO, SFS, SOR, SOV, SSF, STI, STT, SZR, TER, TUN, UOV, USI, UTL, UWY or YFI structure type, mixtures of two or more thereof, or a mixed structure type of two or more thereof, preferably an AFS, AFY, BEA, BEG, BOG, BOZ, BPH, CON, DFO, EMT, FAU, GME, IFW, IMF, ISV, ITG, ITH, ITR, IWR, IWS, IWW, JSR, KFI, LTA, LTF, LTL, MEI, MEL, MER, MFI, MOR, MOZ, MSE, MWF, OBW, OFF, OSO, PAU, POS, PWN, RHO, SAO, SAV, SBS, SBT, SOR, SOV, SZR, TUN, UOV, UWY, or YFI structure type, or a mixed structure type of two or more thereof, more preferably an AFS, AFY, BEA, BOG, BOZ, BPH, CON, FAU, IFW, IMF, ISV, ITG, IWR, IWS, IWW, JSR, MEI, MEL, MFI, MOR, MSE, OBW, OFF, POS, SAO, SOR, SOV, TUN, UWY, or YFI structure type, or a mixed structure type of two or more thereof, more preferably a BEA, FAU, MFI or MOR structure type, or a mixed structure type of two or more thereof, more preferably an FAU or MFI structure type.

Alternatively, it is preferred that the zeolitic material in (2) is a mixture of two or more structure types, wherein the structure types are selected from the list consisting of AFS, AFY, BEA, BOG, BOZ, BPH, CON, FAU, IFW, IMF, ISV, ITG, IWR, IWS, IWW, JSR, MEI, MEL, MFI, MOR, MSE, OBW, OFF, POS, SAO, SOR, SOV, TUN, UWY, or YFI, preferably selected from the list consisting of BEA, FAU, MFI or MOR, more preferably wherein the zeolitic material in (2) is a mixture of FAU and MFI structure types.

In the case where the zeolitic material in (2) is a mixture of two or more structure types, it is preferred that the weight ratio of the first zeolitic material to the second zeolitic material is in the range of from 1 :10 to 10:1 , preferably in the range of from 1 :5 to 5:1 , more preferably in the range of from 1 :3 to 3: 1.

It is preferred that the zeolitic material in (2) has a BEA type framework structure, and wherein the zeolite is selected from the group consisting of zeolite beta, zeolite beta dealuminated, Tschernichite, [B-Si-O]-BEA, [Ga-Si-O]-BEA, and [Ti-Si-O]-BEA, Al-rich zeolite beta, pure silica beta and CIT-6, preferably zeolite beta.

In the case where the zeolitic material in (2) has a BEA type framework structure, it is preferred that the SiO2:AhO3 molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 35, more preferably from 20 to 30.

It is preferred that the zeolitic material in (2) has an MOR type framework structure, and wherein the zeolite is selected from the group consisting of Na-D, Ca-Q, Mordenite, Mordenite dealuminated, Mordenite silicious, LZ-211 , [Ga-Si-O]-MOR, Maricopaite and RMA-1 , preferably mordenite. In the case where the zeolitic material in (2) has an MOR type framework structure, it is preferred that the SiO2:AhO3 molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 30, more preferably from 15 to 25.

It is preferred that the zeolitic material in (2) has a FAU type framework structure, and wherein the zeolite is selected from the group consisting of (2) Faujasite, [Ga-Ge-O]-FAU, [Al-Ge-O]- FAU, zeolite X, zeolite Y, Na-X, ZSM-3, CSZ-1 , CSZ-3, zeolite Y dealuminated, SAPO-37, US- Y, LZ-210, ECR-30, ZSM-20, Na-Y, [Ga-AI-Si-O]-FAU, [Ga-Si-O]-FAU and Li-LSX, preferably US-Y.

In the case where the zeolitic material in (2) has a FAU type framework structure, it is preferred that the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

It is preferred that the zeolitic material in (2) has an MFI type framework structure, and wherein the zeolite is selected from the group consisting of ZSM-5, Silicalite, Bor-C, Boralite-C, LZ-105, AMS-1 B, FZ-1 , TZ-01 , USC-4, NU-5, ZMQ-TB, TS1 , USI-108, AZ-1 , TSZ, ZKQ-1 B, Encilite, NU- 4, TSZ-III, ZBH, [Fe-Si-O]-MFI, H-ZSM-5, [Ga-Si-O]-MFI, [As-Si-O]-MFI, Mutinaite, MnS-1 , FeS- 1 and ZSM-5 dealuminated, preferably ZSM-5.

In the case where the zeolitic material in (2) has an MFI type framework structure, it is preferred that the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

It is preferred that the one or more alkanes comprised in the reaction mixture obtained in (3) comprise one or more unbranched and/or branched alkanes, preferably one or more unbranched alkanes.

In the case where the one or more alkanes comprised in the reaction mixture obtained in (3) comprise one or more unbranched and/or branched alkanes, it is preferred that the molar ratio of unbranched to branched alkanes is in the range of from 1 :1 to 1 :4, preferably from 1 :1 .5 to 1 :3.5, more preferably from 1 :2 to 1 :3.

Yet further, it is preferred that the one or more alkanes comprised in the reaction mixture obtained in (3) comprise unbranched and mono-branched alkanes, wherein the molar ratio of unbranched to mono-branched alkanes is in the range of from 1 :1 to 1 :5, preferably from 1 :2 to 1 :4.5, more preferably from 1 :3 to 1 :4.

Alternatively, in the case where the one or more alkanes comprised in the reaction mixture obtained in (3) comprise one or more unbranched and/or branched alkanes, it is preferred that the molar ratio of unbranched to branched alkanes is in the range of from 1 :1 to 4:1 , preferably from 1.5:1 to 3.5:1 , more preferably from 2:1 to 3:1.

Yet further, it is preferred that the molar ratio of unbranched to mono-branched alkenes is in the range of from 1 :1 to 5:1 , preferably from 1 .5:1 to 4:1 , more preferably from 2:1 to 3:1 .

It is preferred that the heterogeneous catalyst in (2) is substantially free of rhenium, preferably wherein the heterogeneous catalyst in (2) contains less than 0.1 wt.-% of rhenium, more preferably less than 0.01 wt.-%, more preferably less than 0.001 wt.-%, wherein more preferably the heterogeneous catalyst in (2) is free of rhenium.

It is preferred that the one or more metals loaded on the zeolitic material in (2) are selected from the group consisting of Li, Na, K, Cs, Mg, Ca, Sr, Ba, La, Ce, Y, V, Mo, W, Nb, Sn, P, Sb, S, Se, Fe, Ni, Co, Pt, Pd, Rh and mixtures thereof, preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof.

Alternatively, it is preferred that the one or more metals loaded on the zeolitic material in (2) are group 9 to 11 metals, preferably group 10 metals, more preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof, more preferably Ni, Pt, and mixtures thereof, more preferably Ni or Pt.

It is preferred that the heterogeneous catalyst in (2) contains Pt, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Pt, wherein more preferably the zeolitic material has a Pt content in the range of from 0.001 to 5 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.01 to 2 wt.-%, more preferably from 0.1 to 1 .5 wt.-%, more preferably from 0.5 to 1 .3 wt.-%, more preferably from 0.8 to 1 .2 wt.-%, more preferably from 0.9 to 1 .1 wt.-%.

It is preferred that the heterogeneous catalyst in (2) contains Ni, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Ni, wherein more preferably the zeolitic material has a Ni content in the range of from 0.01 to 10 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.1 to 9 wt.-%, more preferably from 1 to 8 wt.-%, more preferably from 2 to 7 wt.-%, more preferably from 3 to 6 wt.-%, more preferably from 4 to 5.5 wt.-%.

It is preferred that the zeolitic material in (2) comprises YO2 and X2O3 in its framework structure, wherein Y stands for a tetravalent element and X stands for a trivalent element.

In the case where the zeolitic material in (2) comprises YO2 and X2O3 in its framework structure, it is preferred that X is selected from the group consisting of Al, B, Ga and combinations thereof, wherein X is preferably AL Yet further, in the case where the zeolitic material in (2) comprises YO2 and X2O3 in its framework structure, it is preferred that Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is preferably Si.

It is preferred that the surface area of the zeolitic material in (2) ranges of from 350 to 900 m²/g, preferably from 360 to 800 m²/g, more preferably from 370 to 700 m²/g, more preferably from 380 to 600 m²/g, more preferably from 390 to 550 m²/g, more preferably from 400 to 500 m²/g, wherein the surface area is determined using the zeolitic material in its H-form.

It is preferred that the heterogeneous catalyst in (2) further comprises a binder, wherein the binder preferably comprises, more preferably consists of, one or more selected from the group consisting of titania, zirconia, alumina, silica, silica-alumina, titania-silica, titania-alumina, zirco- nia-silica, zirconia-alumina, and titania-zirconia, more preferably from the group consisting of silica-alumina, titania-silica, titania-alumina, zirconia-silica, zirconia-alumina, and titania-zirconia, wherein more preferably the binder comprises, more preferably consists of, silica, alumina or mixtures thereof.

It is preferred that the heterogeneous catalyst in (2) is provided as a shaped body, preferably as an extrudate.

Alternatively, it is preferred that the heterogeneous catalyst in (2) is provided as a shaped body, preferably a 3D printed structure.

In the case where the heterogeneous catalyst in (2) is provided as a shaped body, it is preferred that the heterogeneous catalyst has a cross-sectional profile, wherein the cross-sectional profile is circular, hexagonal, rectangular, quadratic, triangular, oval, a star-shaped polygon having 3, 4, 5, 6, 7, or 8 tips, a trilobe or a quadrilobe, preferably a trilobe or a quadrilobe.

In the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that from 95 to 100 wt.-% of the heterogeneous catalyst provided in (2) consists of the zeolite and the optional binder, preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, based on the total weight of the catalyst.

Yet further, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the binder content of the heterogeneous catalyst in (2) ranges of from 10 to 90 wt.-%, preferably from 14 to 80 wt.-%, more preferably from 16 to 70 wt.-%, more preferably from 18 to 60 wt.-%, more preferably from 20 to 50 wt.-%.

Yet further, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the preparation of the heterogeneous catalyst according to (2) comprises, (2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture M_a;

(2.b) extruding the mixture M_a obtained according to (2a); (2.c) optionally drying the extrudate obtained according to (2.b);

(2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

(2.e) optionally reducing the extrudate obtained according to (2.b), (2.c) or (2.d);

(2.f) optionally passivating the extrudate obtained according to (2.b), (2.c), (2.d) or (2.e).

Alternatively, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the preparation of the heterogeneous catalyst according to (2) comprises, (2. a’) mixing a binder and a zeolitic material, obtaining a mixture M_a;

(2.b’) extruding the mixture M_a obtained according to (2. a’);

(2.c’) optionally drying the extrudate obtained according to (2.b’);

(2.d’) impregnating the extrudate obtained according to (2.b’), preferably according to (2.c’), with one or more metals, by exposing the extrudate obtained according to (2.b’), preferably according to (2.c’), to an impregnation solution, which comprises an aqueous solvent and a water-soluble compound containing the one or more metals;

(2.e’) optionally drying the impregnated extrudate obtained according to (2.d’);

(2.f’) optionally calcining the impregnated extrudate obtained according to (2.d’), preferably obtained according to (2.e’);

(2.g’) optionally reducing the impregnated extrudate obtained according to (2.d’), preferably according to (2.e’), more preferably according to (2.f’);

(2.h’) optionally passivating the extrudate obtained according to (2.d’), (2.e’), (2.f’) or (2.g’).

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that the binder is a colloid or a colloidal dispersion.

In the case where (2) comprises step (2. a) to (2.f), it is preferred that prior to (2. a) the binder is subject to a peptization step.

In the case where the binder is a colloid or a colloidal dispersion, it is preferred that the solid content of the colloidal dispersion is in the range of from 1 to 40 wt.-%, based on 100 wt.-% of the colloidal dispersion, preferably in the range of from 5 to 30 wt.-%, more preferably in the range of from 10 to 20 wt.-%.

It is preferred that the zeolitic material content of the heterogeneous catalyst in (2) ranges of from 20 to 90 wt.-%, preferably from 30 to 86 wt.-%, more preferably from 40 to 84 wt.-%, more preferably from 50 to 82 wt.-%, more preferably from 60 to 80 wt.-%.

It is preferred that the process includes a step of regenerating the heterogeneous catalyst in (2) after contacting with the feed MF in (3) wherein the catalyst is preferably regenerated by steaming at a temperature in the range of from 300 to 800 °C, preferably from 350 to 700 °C, more preferably from 400 to 600 °C, more preferably from 450 to 500 °C.

It is preferred that the reaction space S in (3) is a fixed bed reactor or a fluidized bed reactor, preferably in a fixed bed reactor. It is preferred that in (3) the reducing gas atmosphere comprises, preferably consists of, hydrogen.

In case where the reducing gas atmosphere comprises, preferably consists of, hydrogen, it is preferred that the volume flow of the hydrogen stream is preferably in the range of from 10 to 80 L/h, preferably from 20 to 60 L/h, more preferably from 25 to 50 L/h, more preferably from 30 to 40 L/h, more preferably from 34 to 38 L/h.

It is preferred that during subjecting according to (3) the pressure in the reaction space S is in the range of from 10 to 200 bar, preferably from 15 to 150 bar, more preferably from 20 to 100 bar, more preferably from 25 to 75 bar, more preferably from 30 to 50 bar.

It is preferred that in (3) the temperature in the reaction space S is in the range of from 150 to 350 °C, preferably from 200 to 310 °C, more preferably from 210 to 300 °C, more preferably from 220 to 290 °C, more preferably from 220 to 260°C.

It is preferred that the weight hourly space velocity at which the feed MF according to (1) is contacted with the heterogeneous catalyst according to (2) in (3) is in the range of from 0.1 to 5 IT¹ , preferably from 1 to 3 IT¹ , more preferably from 1 .8 to 2.8 IT¹ , more preferably from 1 .9 to 2.7 h- ¹, more preferably from 2 to 2.6 IT¹.

It is preferred that the feed MF in (1) is a feed stream and contacting in (3) is conducted as a continuous process.

Alternatively, it is preferred that the process is conducted as a batch process.

It is preferred that the feed MF provided in (1 ) and contacted with the heterogeneous catalyst (3) is in the liquid phase and/or the gas phase, preferably in the gas phase.

It is preferred that the methane content of the reaction mixture obtained in (3) is 1 wt.-% or less, based on the total reaction mixture, preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less.

It is preferred that the reaction mixture obtained according to (3) comprises one or more branched and/or unbranched alkanes, preferably wherein the one or more branched and/or unbranched alkanes are selected from the group consisting of methane, ethane, propane, butane, pentane, hexane, heptane, octane and nonane, more preferably from the group consisting of ethane, propane, butane, pentane, hexane and heptane, more preferably from the group consisting of ethane, propane, butane and pentane, more preferably from the group consisting of propane and butane. Alternatively, it is preferred that the reaction mixture obtained according to (3) comprises one or more branched and/or unbranched alkanes, preferably wherein the one or more branched and/or unbranched alkanes are selected from the group consisting of methane, ethane, propane, butane, pentane, hexane, heptane, octane and nonane, more preferably from the group consisting of ethane, propane, butane, pentane, hexane, heptane, more preferably from the group consisting of propane, butane, pentane and hexane, more preferably from the group consisting of butane, pentane and hexane.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is conducted at a temperature in the range of from 50 to 300 °C, preferably from 100 to 200 °C, more preferably from 120 to 180 °C, more preferably from 130 to 170 °C, more preferably from 140 to 160 °C.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.c) or (2.e’) preferably comprises an inert gas, preferably nitrogen and/or argon, more preferably comprises nitrogen.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is conducted for a period ranging from 6 to 48 h, preferably from 12 to 36 h, more preferably from 20 to 28 h.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is conducted at a temperature in the range of from 100 to 500 °C, preferably from 200 to 400 °C, more preferably from 240 to 360 °C, more preferably from 260 to 340 °C, more preferably from 280 to 320 °C.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.e) or (2.g’) preferably comprises a reducing gas, more preferably comprises hydrogen.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is conducted for a period ranging from 6 to 36 h, preferably from 8 to 24 h, more preferably from 10 to 14 h.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other passivating in (2.f) or (2.h’) is conducted at a temperature in the range of from 50 to 200 °C, preferably from 60 to 150 °C, more preferably from 70 to 100 °C.

In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other passivating in (2.f) or (2.h’) us conducted for a period ranging from 1 to 36 h, preferably from 3 to 28 h, more preferably from 6 to 20 h. It is preferred that during subjecting in (3) 75 % or more of the feed MF is cracked, preferably 80 % or more, more preferably 85 % or more, more preferably 90 % or more, more preferably 95 % or more, more preferably 97 % or more, more preferably 99 % or more of the feed MF is cracked.

It is preferred that the reaction space S is a trickle-bed reactor or an ebullated bed reactor, preferably a plug-flow trickle-bed reactor.

In the case where the reaction space S is a trickle-bed reactor, it is preferred that the trickle-bed reactor comprises a structured catalyst bed which comprises stacked layers of the catalyst according to (2).

In the case where the trickle-bed reactor comprises a structured catalyst bed, it is preferred that the number of stacked layers is in the range of from 2 to 30, preferably from 3 to 20, more preferably from 4 to 10.

In the case where the reaction space S is a trickle-bed reactor, it is preferred that the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers. With the meaning of the present invention, the term “positive binder gradient" refers to a binder content change from a lower binder content of a first layer to a higher binder content of a second layer, wherein the second layer is located at a higher position in the stacked layers of the catalyst than the first layer.

In the case where the trickle-bed reactor is operated over a positive binder gradient from lower to upper layer, it is preferred that the binder gradient is uniform across a portion of the tricklebed reactor, wherein each upper layer has a slightly higher binder content than the adjacent lower layer.

Alternatively, in the case where the trickle-bed reactor is operated over a positive binder gradient from lower to upper layer, it is preferred that the binder gradient is non-uniform, wherein the binder content of an upper layer is higher than the binder content of a lower layer.

In the case where the process comprises step (4), it is preferred that the process further comprises

(5) separating the one or more alkanes having a chain length m with m < n from the product mixture Mp.

In the case where the process comprises step (5), it is preferred that the one or more alkanes according to (5) is conducted by distillation, preferably fractional distillation.

It is preferred that the feed MF according to (1) has not been subject to a hydrodeoxygenation treatment, wherein preferably the feed MF according to (1 ) has not been subject to a deoxygenation treatment. It is preferred that the feed MF according to (1) is a merged feed of two or more sub-feeds, wherein at least one of the two or more sub-feeds comprises one or more oxygen containing compounds comprising, independently of one another, one or more alkyl chains, wherein the alkyl chains have, independently of one another, a length n with 4 < n < 30.

In case where the feed MF according to (1 ) is a merged feed of two or more sub-feeds, it is preferred that at least one of the two or more sub-feeds is substantially free of oxygen containing compounds, preferably wherein, independently from one another, at least one of the sub-feeds contains 1 wt.-% or less of oxygen containing compounds, more preferably 0.1 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.001 wt.-% or less, based on the total weight of the respective sub-feed.

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 represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.

1 . A process for the hydrodeoxygenation and hydrocracking of a feed comprising, preferably consisting of,

2. The process according to embodiment 1 , further comprising

(4) removing a product mixture MP from the reaction space S, wherein the mixture MP comprises the one or more alkanes having a chain length m with m < n. 3. The process according to embodiment 1 or 2, wherein 1 < m < 18, preferably 2 < m < 16, more preferably 2 < m < 14, more preferably 3 < m < 10.

4. The process according to any of embodiments 1 to 3, wherein 4 < n < 28, preferably 5 < n < 24, more preferably 6 < n < 22, more preferably 8 < n < 20.

5. The process according to any of embodiments 1 to 4, wherein the one or more oxygen containing compounds comprised in the feed MF in (1) have one or more functional groups selected from the group consisting of a carboxylic acid group, a ketone group, an aldehyde group, an ester group, an ether group, an acetal group, a lactone group, or a hydroxyl group.

6. The process according to any of embodiments 1 to 5, wherein the feed MF provided according to (1) has a content in oxygen stemming from the one or more oxygen containing compounds in the range of from 0.1 to 50 wt.-%, based on the total weight of the one or more oxygen containing compounds, preferably from 0.1 to 40 wt.-%, more preferably from 0.1 to 30 wt.-%, more preferably from 0.2 to 20 wt.-%, more preferably from 0.5 to 10 wt.-%.

7. The process according to any of embodiments 1 to 6, wherein the feed MF provided according to (1) has a content of the one or more oxygen containing compounds in the range of from 1 to 100 wt.-%, based on the total weight of the feed MF, preferably from 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%.

8. The process according to any of embodiments 1 to 7, wherein the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof.

9. The process according to embodiment 8, wherein the one or more oxygen containing compounds comprise, preferably consists of, waste materials, preferably of waste materials of biomaterials and/or plastics, more preferably waste materials selected from the group consisting of vegetable oils, animal fats, pyrolysis oils and derivatives thereof.

10. The process according to any of embodiments 1 to 9, wherein the one or more oxygen containing compounds in the feed MF in (1) are selected from the group consisting of triglycerides of vegetable or animal origin, derivates of triglycerides of vegetable or animal origin, and mixtures thereof.

11 . The process according to any of embodiments 8 to 10, wherein the vegetable oil is selected from the group consisting of palm oil, soybean oil, rapeseed oil, sunflower oil, linseed oil, rice bran oil, maize oil, olive oil, castor oil, sesame oil, pine oil, peanut oil, mustard oil, palm kernel oil, hempseed oil, coconut oil, babassu oil, cottonseed oil, jatropha oil, used cooking oils, oils derived from algae, corn oil, safflower oil, sunflower oil, almond oil, beech nut oil, brazil nut oil, cashew oil, hazelnut oil, macadamia oil, mongongo nut oil, pecan oil, pistachio oil, walnut oil, pumpkin seed oil, amaranth oil, argan oil, ben oil, date seed oil, dika oil, false flax oil, grape seed oil, hemp oil, kapok seed oil, kenaf seed oil, marula oil, meadowfoam seed oil, okra seed oil, perilla seed oil, persimmon seed oil, pequi oil, pili nut oil, poppyseed oil, pracaxi oil, quinoa oil, colza oil, radish oil, safflower oil, tigernut oil, tung oil and mixtures of two or more thereof.

12. The process according to any of embodiments 8 to 11 , wherein the animal fat is selected from the group consisting of tallow, lard, grease, fish oil, butterfat, milk fat, and mixtures of two or more thereof.

13. The process according to embodiments 1 to 12, wherein the feed MF in (1) comprises 50 wt.-% or more of fatty acid esters and/or free fatty acids, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more of fatty acid esters and/or free fatty acids.

14. The process according to embodiments 8 to 13, wherein the animal fats and vegetable oils are at least partially hydrogenated, preferably hydrogenated.

15. The process according to any of embodiments 1 to 8, wherein the feed MF in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

16. The process according to embodiment 15, wherein the pyrolysis oil of biogenic nature is selected from the group consisting of wood, straw, scrap wood, and mixtures of two or more thereof.

17. The process according to any of embodiments 1 to 8, wherein the feed MF in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms.

18. The process according to any of embodiments 15 to 17, wherein the feed MF in (1 ) comprises 50 wt.-% or more of pyrolysis oil, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more, more preferably 95 wt.-% or more of pyrolysis oil.

19. The process according to any of embodiments 1 to 18, wherein the zeolitic material in (2) has an AFR, AFS, AFY, BEA, BEC, BOG, BOZ, BPH, CON, CSV, DFO, EMT, EON, EWF, FAU, FER, GME, IFW, IMF, ISV, ITE, ITG, ITH, ITR, IWR, IWS, IWV, IWW, JSR, KFI, LTA, LTF, LTL, MEI, MEL, MER, MFI, MFS, MOR, MOZ, MSE, MWF, MWW, NES, OBW, OFF, OKO, OSO, PAU, PGR, POS, PWN, RHO, RTH, SAO, SAV, SBS, SBT, SEW, SFG, SFO, SFS, SOR, SOV, SSF, STI, STT, SZR, TER, TUN, UOV, USI, UTL, UWY or YFI structure type, mixtures of two or more thereof, or a mixed structure type of two or more thereof, preferably an AFS, AFY, BEA, BEG, BOG, BOZ, BPH, CON, DFO, EMT, FAU, GME, IFW, IMF, ISV, ITG, ITH, ITR, IWR, IWS, IWW, JSR, KFI, LTA, LTF, LTL, MEI, MEL, MER, MFI, MOR, MOZ, MSE, MWF, OBW, OFF, OSO, PAU, POS, PWN, RHO, SAO, SAV, SBS, SBT, SOR, SOV, SZR, TUN, UOV, UWY, or YFI structure type, or a mixed structure type of two or more thereof, more preferably an AFS, AFY, BEA, BOG, BOZ, BPH, CON, FAU, IFW, IMF, ISV, ITG, IWR, IWS, IWW, JSR, MEI, MEL, MFI, MOR, MSE, OBW, OFF, POS, SAO, SOR, SOV, TUN, UWY, or YFI structure type, or a mixed structure type of two or more thereof, more preferably a BEA, FAU, MFI or MOR structure type, or a mixed structure type of two or more thereof, more preferably an FAU or MFI structure type.

20. The process according to any of embodiments 1 to 18, wherein the zeolitic material in (2) is a mixture of two or more structure types, wherein the structure types are selected from the list consisting of AFS, AFY, BEA, BOG, BOZ, BPH, CON, FAU, IFW, IMF, ISV, ITG, IWR, IWS, IWW, JSR, MEI, MEL, MFI, MOR, MSE, OBW, OFF, POS, SAO, SOR, SOV, TUN, UWY, or YFI, preferably selected from the list consisting of BEA, FAU, MFI or MOR, more preferably wherein the zeolitic material in (2) is a mixture of FAU and MFI structure types.

21 . The process of embodiment 20, wherein the zeolitic material in (2) is a mixture of two or more structure types, it is preferred that the weight ratio of the first zeolitic material to the second zeolitic material is in the range of from 1 :10 to 10:1 , preferably in the range of from 1 :5 to 5: 1 , more preferably in the range of from 1 :3 to 3: 1.

22. The process according to any of embodiments 1 to 21 , wherein the zeolitic material in (2) has a BEA type framework structure, and wherein the zeolite is selected from the group consisting of zeolite beta, zeolite beta dealuminated, Tschernichite, [B-Si-O]- BEA, [Ga-Si-O]-BEA, and [Ti-Si-O]-BEA, Al-rich zeolite beta, pure silica beta and CIT- 6, preferably zeolite beta.

23. The process according to embodiment 22, wherein the SiO2:AhO3 molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 35, more preferably from 20 to 30.

24. The process according to any of embodiments 1 to 23, wherein the zeolitic material in (2) has an MOR type framework structure, and wherein the zeolite is selected from the group consisting of Na-D, Ca-Q, Mordenite, Mordenite dealuminated, Mordenite sili- cious, LZ-211 , [Ga-Si-O]-MOR, Maricopaite and RMA-1 , preferably mordenite. 25. The process according to embodiment 24, wherein the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 30, more preferably from 15 to 25.

26. The process according to any of embodiments 1 to 25, wherein the zeolitic material in (2) has a FAU type framework structure, and wherein the zeolite is selected from the group consisting of (2) Faujasite, [Ga-Ge-O]-FAU, [AI-Ge-O]-FAU, zeolite X, zeolite Y, Na-X, ZSM-3, CSZ-1 , CSZ-3, zeolite Y dealuminated, SAPO-37, US-Y, LZ-210, ECR- 30, ZSM-20, Na-Y, [Ga-AI-Si-O]-FAU, [Ga-Si-O]-FAU and Li-LSX, preferably US-Y.

27. The process according to embodiment 26, wherein the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

28. The process according to any of embodiments 1 to 27, wherein the zeolitic material in (2) has an MFI type framework structure, and wherein the zeolite is selected from the group consisting of ZSM-5, Silicalite, Bor-C, Boralite-C, LZ-105, AMS-1 B, FZ-1 , TZ-01 , USC-4, NU-5, ZMQ-TB, TS1 , USI-108, AZ-1 , TSZ, ZKQ-1 B, Encilite, NU-4, TSZ-III, ZBH, [Fe-Si-O]-MFI, H-ZSM-5, [Ga-Si-O]-MFI, [As-Si-O]-MFI, Mutinaite, MnS-1, FeS-1 and ZSM-5 dealuminated, preferably ZSM-5.

29. The process according to embodiment 28, wherein the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

30. The process according to any of embodiments 1 to 29, wherein the one or more alkanes comprised in the reaction mixture obtained in (3) comprise one or more unbranched and/or branched alkanes, preferably one or more unbranched alkanes.

31 . The process according to embodiment 30, wherein the one or more alkanes comprised in the reaction mixture obtained in (3) comprise unbranched and branched alkanes, wherein the molar ratio of unbranched to branched alkanes is in the range of from 1 :1 to 1 :4, preferably from 1 :1.5 to 1 :3.5, more preferably from 1 :2 to 1 :3.

32. The process according to embodiment 30 or 31 , wherein the one or more alkanes comprised in the reaction mixture obtained in (3) comprise unbranched and monobranched alkanes, wherein the molar ratio of unbranched to monobranched alkanes is in the range of from 1 :1 to 1 :5, preferably from 1 :2 to 1 :4.5, more preferably from 1 :3 to 1 :4.

33. The process according to embodiment 30, wherein the molar ratio of unbranched to branched alkanes is in the range of from 1 :1 to 4:1 , preferably from 1.5:1 to 3.5:1 , more preferably from 2:1 to 3:1. 34. The process according to embodiment 30 or 33, wherein the molar ratio of unbranched to mono-branched alkenes is in the range of from 1 :1 to 5:1 , preferably from 1.5:1 to 4: 1 , more preferably from 2:1 to 3: 1 .

35. The process according to any of embodiments 1 to 34, wherein the heterogeneous catalyst in (2) is substantially free of rhenium, preferably wherein the heterogeneous catalyst in (2) contains less than 0.1 wt.-% of rhenium, more preferably less than 0.01 wt.-%, more preferably less than 0.001 wt.-%, wherein more preferably the heterogeneous catalyst in (2) is free of rhenium.

36. The process according to any of embodiments 1 to 35, wherein the one or more metals loaded on the zeolitic material in (2) are selected from the group consisting of Li, Na, K, Cs, Mg, Ca, Sr, Ba, La, Ce, Y, V, Mo, W, Nb, Sn, P, Sb, S, Se, Fe, Ni, Co, Pt, Pd, Rh and mixtures thereof, preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof.

37. The process according to any of embodiments 1 to 35, wherein the one or more metals loaded on the zeolitic material in (2) are group 9 to 11 metals, preferably group 10 metals, more preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof, more preferably Ni, Pt, and mixtures thereof, more preferably Ni or Pt.

38. The process according to any of embodiments 1 to 37, wherein the heterogeneous catalyst in (2) contains Pt, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Pt, wherein more preferably the zeolitic material has a Pt content in the range of from 0.001 to 5 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.01 to 2 wt.-%, more preferably from 0.1 to 1 .5 wt.-%, more preferably from 0.5 to 1 .3 wt.-%, more preferably from 0.8 to 1 .2 wt.-%, more preferably from 0.9 to 1 .1 wt.-%.

39. The process according to any of embodiments 1 to 38, wherein the heterogeneous catalyst in (2) contains Ni, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Ni, wherein more preferably the zeolitic material has a Ni content in the range of from 0.01 to 10 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.1 to 9 wt.-%, more preferably from 1 to 8 wt.-%, more preferably from 2 to 7 wt.-%, more preferably from 3 to 6 wt.-%, more preferably from 4 to 5.5 wt.-%.

40. The process according to any of embodiments 1 to 39, wherein the zeolitic material in (2) comprises YO2 and X2O3 in its framework structure, wherein Y stands for a tetravalent element and X stands for a trivalent element. 41 . The process according to embodiment 40, wherein X is selected from the group consisting of Al, B, Ga and combinations thereof, wherein X is preferably Al.

42. The process according to embodiment 40 or 41 , wherein Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is preferably Si.

43. The process according to any of embodiments 1 to 42, wherein the surface area of the zeolitic material in (2) ranges of from 350 to 900 m²/g, preferably from 360 to 800 m²/g, more preferably from 370 to 700 m²/g, more preferably from 380 to 600 m²/g, more preferably from 390 to 550 m²/g, more preferably from 400 to 500 m²/g, wherein the surface area is determined using the zeolitic material in its H-form.

44. The process according to any of embodiments 1 to 43, wherein the heterogeneous catalyst in (2) further comprises a binder, wherein the binder preferably comprises, more preferably consists of, one or more selected from the group consisting of titania, zirconia, alumina, silica, silica-alumina, titania-silica, titania-alumina, zirconia-silica, zirconia-alumina, and titania-zirconia, more preferably from the group consisting of silica- alumina, titania-silica, titania-alumina, zirconia-silica, zirconia-alumina, and titania-zirconia, wherein more preferably the binder comprises, more preferably consists of, silica, alumina or mixtures thereof.

45. The process according to any of embodiments 1 to 44, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably as an extrudate.

46. The process according to any of embodiments 1 to 44, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably a 3D printed structure.

47. The process according to embodiment 45 or 46, wherein the heterogeneous catalyst has a cross-sectional profile, wherein the cross-sectional profile is circular, hexagonal, rectangular, quadratic, triangular, oval, a star-shaped polygon having 3, 4, 5, 6, 7, or 8 tips, a trilobe or a quadrilobe, preferably a trilobe or a quadrilobe.

48. The process according to any of embodiments 44 to 47, wherein from 95 to 100 wt.-% of the heterogeneous catalyst provided in (2) consists of the zeolite and the optional binder, preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, based on the total weight of the catalyst.

49. The process according to any of embodiments 44 to 48, wherein the binder content of the heterogeneous catalyst in (2) ranges of from 10 to 90 wt.-%, preferably from 14 to 80 wt.-%, more preferably from 16 to 70 wt.-%, more preferably from 18 to 60 wt.-%, more preferably from 20 to 50 wt.-%. 50. The process according to any of embodiments 44 to 49, wherein the preparation of the heterogeneous catalyst according to (2) comprises,

(2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture M_a;

(2.b) extruding the mixture M_a obtained according to (2a);

(2.c) optionally drying the extrudate obtained according to (2.b);

(2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

51 . The process according to any of embodiments 44 to 49, wherein the preparation of the heterogeneous catalyst according to (2) comprises,

(2. a’) mixing a binder and a zeolitic material, obtaining a mixture M_a;

(2.b’) extruding the mixture M_a obtained according to (2. a’);

(2.c’) optionally drying the extrudate obtained according to (2.b’);

52. The process according to embodiment 50 or 51 , wherein the binder is a colloid or a colloidal dispersion.

53. The process according to embodiment 50 or 52, wherein prior to (2. a) the binder is subject to a peptization step.

54. The process according to embodiment 52, wherein the solid content of the colloidal dispersion is in the range of from 1 to 40 wt.-%, based on 100 wt.-% of the colloidal dispersion, preferably in the range of from 5 to 30 wt.-%, more preferably in the range of from 10 to 20 wt.-%.

55. The process according to any of embodiments 1 to 54, wherein the zeolitic material content of the heterogeneous catalyst in (2) ranges of from 20 to 90 wt.-%, preferably from 30 to 86 wt.-%, more preferably from 40 to 84 wt.-%, more preferably from 50 to 82 wt.-%, more preferably from 60 to 80 wt.-%. 56. The process according to any of embodiments 1 to 55, wherein the process includes a step of regenerating the heterogeneous catalyst in (2) after contacting with the feed MF in (3) wherein the catalyst is preferably regenerated by steaming at a temperature in the range of from 300 to 800 °C, preferably from 350 to 700 °C, more preferably from 400 to 600 °C, more preferably from 450 to 500 °C.

57. The process according to any of embodiments 1 to 56, wherein the reaction space S in (3) is a fixed bed reactor or a fluidized bed reactor, preferably in a fixed bed reactor.

58. The process according to any of embodiments 1 to 57, wherein in (3) the reducing gas atmosphere comprises, preferably consists of, hydrogen.

59. The process according to embodiment 58, wherein in (3) the reducing gas atmosphere comprises, preferably consists of, a hydrogen stream, wherein the volume flow of the hydrogen stream is preferably in the range of from 10 to 80 L/h, preferably from 20 to 60 L/h, more preferably from 25 to 50 L/h, more preferably from 30 to 40 L/h, more preferably from 34 to 38 L/h.

60. The process according to any of embodiments 1 to 59, wherein during subjecting according to (3) the pressure in the reaction space S is in the range of from 10 to 200 bar, preferably from 15 to 150 bar, more preferably from 20 to 100 bar, more preferably from 25 to 75 bar, more preferably from 30 to 50 bar.

61 . The process according to any of embodiments 1 to 60, wherein in (3) the temperature in the reaction space S is in the range of from 150 to 350 °C, preferably from 200 to 310 °C, more preferably from 210 to 300 °C, more preferably from 220 to 290 °C, more preferably from 220 to 260°C.

62. The process according to any of embodiments 1 to 61 , wherein the weight hourly space velocity at which the feed MF according to (1) is contacted with the heterogeneous catalyst according to (2) in (3) is in the range of from 0.1 to 5 IT¹, preferably from 1 to 3 IT¹, more preferably from 1 .8 to 2.8 IT¹, more preferably from 1 .9 to 2.7 IT¹, more preferably from 2 to 2.6 IT¹.

63. The process according to any of embodiments 1 to 62, wherein the feed MF in (1 ) is a feed stream and contacting in (3) is conducted as a continuous process.

64. The process according to any of embodiments 1 to 62, wherein the process is conducted as a batch process. 65. The process according to any of embodiments 1 to 64, wherein the feed MF provided in (1) and contacted with the heterogeneous catalyst (3) is in the liquid phase and/or the gas phase, preferably in the gas phase.

66. The process according to any of embodiments 1 to 65, wherein the methane content of the reaction mixture obtained in (3) is 1 wt.-% or less, based on the total reaction mixture, preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less.

67. The process according to any of embodiments 1 to 66, wherein the reaction mixture obtained according to (3) comprises one or more branched and/or unbranched alkanes, preferably wherein the one or more branched and/or unbranched alkanes are selected from the group consisting of methane, ethane, propane, butane, pentane, hexane, heptane, octane and nonane, more preferably from the group consisting of ethane, propane, butane, pentane, hexane and heptane, more preferably from the group consisting of ethane, propane, butane and pentane, more preferably from the group consisting of propane and butane.

68. The process according to any of embodiments 1 to 66, wherein the reaction mixture obtained according to (3) comprises one or more branched and/or unbranched alkanes, preferably wherein the one or more branched and/or unbranched alkanes are selected from the group consisting of methane, ethane, propane, butane, pentane, hexane, heptane, octane and nonane, more preferably from the group consisting of ethane, propane, butane, pentane, hexane, heptane, more preferably from the group consisting of propane, butane, pentane and hexane, more preferably from the group consisting of butane, pentane and hexane.

69. The process according to any of embodiments 50 to 68, wherein independently from each other drying in (2.c) or (2.e’) is conducted at a temperature in the range of from 50 to 300 °C, preferably from 100 to 200 °C, more preferably from 120 to 180 °C, more preferably from 130 to 170 °C, more preferably from 140 to 160 °C.

70. The process according to any of embodiments 50 to 69, wherein independently from each other drying in (2.c) or (2.e’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.c) or (2.e’) preferably comprises an inert gas, preferably nitrogen and/or argon, more preferably comprises nitrogen.

71 . The process according to any of embodiments 50 to 70, wherein independently from each other drying in (2.c) or (2.e’) is conducted for a period ranging from 6 to 48 h, preferably from 12 to 36 h, more preferably from 20 to 28 h.

72. The process according to any of embodiments 50 to 71 , wherein independently from each other reducing in (2.e) or (2.g’) is conducted at a temperature in the range of from 100 to 500 °C, preferably from 200 to 400 °C, more preferably from 240 to 360 °C, more preferably from 260 to 340 °C, more preferably from 280 to 320 °C.

73. The process according to any of embodiments 50 to 72, wherein independently from each other reducing in (2.e) or (2.g’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.e) or (2.g’) preferably comprises a reducing gas, more preferably comprises hydrogen.

74. The process according to any of embodiments 50 to 73, wherein independently from each other reducing in (2.e) or (2.g’) is conducted for a period ranging from 6 to 36 h, preferably from 8 to 24 h, more preferably from 10 to 14 h.

75. The process according to any of embodiments 50 to 74, wherein independently from each other passivating in (2.f) or (2.h’) is conducted at a temperature in the range of from 50 to 200 °C, preferably from 60 to 150 °C, more preferably from 70 to 100 °C.

76. The process according to any of embodiments 50 to 75, wherein independently from each other passivating in (2.f) or (2.h’) us conducted for a period ranging from 1 to 36 h, preferably from 3 to 28 h, more preferably from 6 to 20 h.

77. The process according to any of embodiments 1 to 76, wherein during subjecting in (3) 75 % or more of the feed MF is cracked, preferably 80 % or more, more preferably 85 % or more, more preferably 90 % or more, more preferably 95 % or more, more preferably 97 % or more, more preferably 99 % or more of the feed MF is cracked.

78. The process according to any of embodiments 1 to 77, wherein the reaction space S is a trickle-bed reactor or an ebullated bed reactor, preferably a plug-flow trickle-bed reactor.

79. The process according to embodiment 78, wherein trickle-bed reactor comprises a structured catalyst bed which comprises stacked layers of the catalyst according to (2).

80. The process according to embodiment 79, wherein the number of stacked layers is in the range of from 2 to 30, preferably from 3 to 20, more preferably from 4 to 10.

81 . The process according to any of embodiments 78 to 80, wherein the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers.

82. The process according to embodiment 81 , wherein the binder gradient is uniform across a portion of the trickle-bed reactor, wherein each upper layer has a slightly higher binder content than the adjacent lower layer. 83. The process according to embodiment 81 , wherein the binder gradient is non-uniform, wherein the binder content of an upper layer is higher than the binder content of a lower layer.

84. The process according to any of embodiments 2 to 83, further comprising

85. The process according to embodiment 84, wherein separating the one or more alkanes according to (5) is conducted by distillation, preferably fractional distillation.

86. The process according to any of embodiments 1 to 85, wherein the feed MF according to (1 ) has not been subject to a hydrodeoxygenation treatment, wherein preferably the feed MF according to (1) has not been subject to a deoxygenation treatment.

87. The process according to any of embodiments 1 to 86, wherein the feed MF according to (1 ) is a merged feed of two or more sub-feeds, wherein at least one of the two or more sub-feeds comprises one or more oxygen containing compounds comprising, independently of one another, one or more alkyl chains, wherein the alkyl chains have, independently of one another, a length n with 4 < n < 30.

88. The process according to embodiment 87, wherein at least one of the two or more sub-feeds is substantially free of oxygen containing compounds, preferably wherein, independently from one another, at least one of the sub-feeds contains 1 wt.-% or less of oxygen containing compounds, more preferably 0.1 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.001 wt.-% or less, based on the total weight of the respective sub-feed.

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

EXAMPLES

Reference Example 1 : Preparation of the zeolite catalyst

Binder preparation:

DI water was provided in a breaker. Under stirring Dispersal P2 was added to gain a mixture with an AI2O3 content of 14.54 wt.-%. SiC>2 (LUDOX AS-40) was used as binder.

Conversion of zeolite into H-form:

Table 1 : Overview of the zeolites as commercially obtained from Zeolyst.

Zeolites obtained in ammonium form were calcined in a muffle furnace at 550 °C (heating rate 5 K/min, dwell time 6 h, air flow 6 L/min) on a porcelain dish with a zeolite bed height of 20 mm or less.

Mixing zeolite and binder:

DI water was provided in a breaker. Under stirring the X wt.-% (X= 20, 40, 60 or 80, see table 2) of zeolite in H-form was added , wherein X refers to the amount of zeolite relative to the total sample weight. The amount of DI water was adjusted until a good stirrable suspension was obtained. The suspension was stirred for 2 -3 h at ambient temperature. Y wt.-% (80, 60, 40 or 20, table 2) of binder dispersion was added, wherein Y refers to the amount of binder relative to the total sample weight and the mixture stirred for 1h.

Freeze drying:

The mixture was transferred into liquid nitrogen to shock freeze it. The now solid mixture was transferred into a precooled freeze dryer (-30 °C) and freeze dried for 7-10 days at -10 °C at 2.56 mbar. The resulting solid was dried at 20 °C and 2.56 mbarfor 2 days. The dried sample was transferred into a porcelain dish and calcined at 300 °C in a muffle furnace (heating rate 5 K/min, dwell time 4 h, air flow 6 L/min).

Shaping:

For pelletizing a tableting device was used with a diameter of 40 mm, press force of ~201 and a resulting tablet height of 4-5 mm.

The tablets were crushed with a resin pestle on analytical sieves (200mm) and sieved through a sieving tower consisting of 5000 pm < 2500 pm < 1400 pm < 1000 pm < 500 pm < bottom. The sample is crushed through all sieves . Fine particles (<500 pm) are sieved out manually for 2-3 min and are separated from the sample.

Impregnation:

The zeolite-binder compounds water uptake is determined prior to the impregnation. The respective amount of Ni(NOs)2 which is required to obtain a zeolite with Z wt.-% of Pt (Z= 0.1 , 0.3, 0.5 or 1 , see table 2) loading or the respective amount of Ni which is required to obtain a zeolite with 5 wt.-% of Ni loading, is diluted with DI water to final volume of 90% of the compounds water uptake. The solution is added dropwise onto the carrier under vigorous mixing. The sample was aged for 30 min at ambient conditions in a fume hood before drying the sample in a drying oven at 80 °C for 16 h in air. Calcination:

The dried sample was calcined in a 2-step calcination process under air in a muffle furnace:

1) Decomposition of nitrates: 220 °C (heating rate 1 K/min, dwell time 3h, air flow 6 L/min)

2) Final Calcination: 350°C (heating rate 1 K/min, dwell time 3h, air flow 6 L/min)

Table 2: Overview of prepared zeolite samples and their properties.

Reference Example 2: Gas Chromatography

Samples of the liquid product mixture from catalytic experiments were analysed by gas chromatography (HP-5890, Hewlett Packard) equipped with a flame ionization detector and a capillary colum (Restek Rtx®-5, diphenyl-/dimethylpolysiloxane, 30 m length, 0.25 mm inner diameter, 25 pm film thickness). After sample injection, the temperature of the column was kept at 40 °C for 3 min and subsequently heated to 190 °C with a rate of 8 K/min and held for 10 min.

Alternatively, gas chromatographic analysis was conducted on a GC2030 by Shimadzu equipped with a flame ionization detector and a capillary column (RT®-Q-BOND, Divinylben- zene, 30 m length, 0.53 mm inner diameter, 20 pm film thickness). After sample injection, the column was kept at 40 °C for 5 min and subsequently increased to 200 °C with a rate of 6 K/min and held for 5 min. For quantitative analysis an external calibration for methane was performed.

The components of the gaseous and liquid product mixture were identified by their retention time and subdivided into unbranched (n-C_n), mono- (iso-C_n) and multibranched (isoiso-C_n) alkanes. The total composition of the gaseous and liquid product mixture was calculated by peak areas, external calibration of n-dodecane and methane relative response factors of the corresponding alkanes and the mass balance of reactants and products. Reference Example 3: Stoichiometric calculations for the hydrocracking of n-dodecane

The conversion X_n-Ci2 of n-dodecane, the yield Y and selectivity S of the conversion products of the hydrocracking reaction were calculated using the mass flow of n-dodecane (min) and liquid product (m_out). Here, cracking products are all hydrocarbons that underwent at least one cracking reaction.

The equations used to calculate the conversion Xn-C12 of n-dodecane (1 ), the product yields Yen (2) and selectivity S_cn for the conversion products, with C_n resembling all possible chain lengths between n=1 to n=9 as well as iso-Ci2 and isoiso-Ci2 resembling the mono- and multibranched isomerization products of n-dodecane with a carbon number of twelve.

Methane was used as a standard for the quantitative calibration of the gaseous products. For this purpose, a gas mixture of 5.03 VoL-% CH3 in H2 was applied and the relative response factors (RRF) were considered for all gaseous products except methane. The RRF were used according to Dietz and, if not available, calculated according to Dettmer-Wilde et aL. The following equations were used to calculate the molar flow rates n_cn in the gaseous products for each gaseous hydrocracking product C_n with the integrated peak are of the chromatogram C_an of the product C_n, A_Ch4 of methan and the molar mass Men of the respective component results. The molar flow rates nc_n,corr. For gaseous products corrected by the mass fraction of gaseous and liquid products were calculated with equation (7). The mass flow mij_q.j_n and the liquid products miiq-’Out

Without methane as internal standard the molar flow rates nc_n for gaseous products were calculated according to equation (8).

The molar flow rates for the liquid products were calculated using an external calibration of n- dodecane according to the subsequent equations. Here, C_n is the volume fraction of the hydrocracking product C_n in the liquid phase and pen is the density of the respective component.

Reference Example 3: Determination of the surface area

Nitrogen sorption analysis was performed at 77 K using a Tristar II (Micrometrics Instruments Corporation), and the samples were degassed prior to measurements. The surface area was determined using the Brunauer-Emmett-Teller (BET) method.

Reference Example 4: Determination of the Si/AI ratio

SARs were estimated by X-ray fluorescence spectroscopy (XRF) performed in a M4 TORNADO from Brucker with rhodium X-ray source and silicon drift detector. The elementary composition of Si and Al were determined by ESPIRIT software.

Example 4: Catalytic testing

The catalytic experiments were carried out in a continuous-flow apparatus with a tubular fold high throughput reactor run in plug-flow mode as trickle-bed reactor at hte GmbH (Germany). The reactors (stainless steel 1.4571 , 4.5 mm internal diameter, 290 mm length) were filled with 1 ml catalyst (sieve fraction 250-315 pm) with a pre-/post-bed of corundum (a-ALOs).

The reaction feed used was liquid n-dodecane and/or 5 wt.% triglycerides in n-dodecane. The hydrodeoxygenation and hydrocracking reaction was carried out at LHSV 2 h-1 , and pH2 of 40 bar and reaction temperature was varied between 220-300 °C. Samples of liquid product mixtures were taken at certain intervals sample of the gaseous product mixture was taken after 360 minimum time on-stream. All liquid and gaseous samples were analysed by gas chromatography. For all experiments, the mass flow rate of reactant and liquid product mixture were detected for mass balancing. Samples of the liquid product mixtures from catalytic experiments were analyzed by gas chromatography (HP-5890, Hewlett Packard) equipped with a flame ionization detector and a capillary column (Restek Rtx®-5, diphenyl-/dimethylpolysiloxane, 30 m length, 0.25 mm inner diameter, 25 pm film thickness). Gaseous samples were analyzed by gas chromatography (DaniEducational) equipped with a flame ionization detector and a capillary column (Restek Rt®-Alumina PLOT, 30 m length, 0.53 mm inner diameter, 5 pm film thickness). Table 3: Overview of conversions and selectivities of tested zeolite samples.

All investigated catalysts are active in the catalytic hydrodeoxygenation and hydrocracking of the corresponding feed. Cracking products of Examples 1 to 3 mainly consist of C3-C9 cracking products, while only traces of C1 and C2 if any, are formed. It has surprisingly been found that the inventive examples lead to a high conversion of the mixed feed for both compounds, which is comparable to the conversion of a pure n-dodecane feed. Further, it has surprisingly been found that a highly efficient one step process for the hydrodeoxygenation and hydrocracking of a feed comprising one or more oxygen containing compounds, in particular with regard to the product selectivity towards LPG and/or naphtha grade cracking products, may be provided by the inventive process. CITED LITERATURE:

- WO 2019/229072 A1

- EP 2770040 A2

- US 2013/0116491 A1

- WO 2009/011160 A1 - J P 5273724 B2

- WO 2023/099658 A1

Claims

2. The process according to claim 1 , further comprising

3. The process according to claim 1 or 2, wherein the one or more oxygen containing compounds comprised in the feed MF in (1) have one or more functional groups selected from the group consisting of a carboxylic acid group, a ketone group, an aldehyde group, an ester group, an ether group, an acetal group, a lactone group, or a hydroxyl group.

4. The process according to any of claims 1 to 3, wherein the feed MF provided according to (1 ) has a content in oxygen stemming from the one or more oxygen containing compounds in the range of from 0.1 to 50 wt.-%, based on the total weight of the one or more oxygen containing compounds.

5. The process according to any of claims 1 to 4, wherein the one or more oxygen containing compounds comprised in the feed MF in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils including mixtures of two or more thereof.

6. The process according to claim 1 to 5, wherein the feed MF in (1) comprises 50 wt.-% or more of fatty acid esters and/or free fatty acids.

7. The process according to any of claims 1 to 6, wherein the one or more metals loaded on the zeolitic material in (2) are selected from the group consisting of Li, Na, K, Cs, Mg, Ca, Sr, Ba, La, Ce, Y, V, Mo, W, Nb, Sn, P, Sb, S, Se, Fe, Ni, Co, Pt, Pd, Rh and mixtures thereof.

8. The process according to any of claims 1 to 7, wherein the zeolitic material in (2) is a mixture of two or more structure types, wherein the structure types are selected from the list consisting of AFS, AFY, BEA, BOG, BOZ, BPH, CON, FAU, IFW, IMF, ISV, ITG, IWR, IWS, IWW, JSR, MEI, MEL, MFI, MOR, MSE, OBW, OFF, POS, SAO, SOR, SOV, TUN, UWY, or YFI.

9. The process according to any of claims 1 to 8, wherein in (3) the reducing gas atmosphere comprises hydrogen.

10. The process according to any of claims 1 to 9, wherein during subjecting according to (3) the pressure in the reaction space S is in the range of from 10 to 200 bar.

11 . The process according to any of claims 1 to 10, wherein in (3) the temperature in the reaction space S is in the range of from 150 to 350 °C.

12. The process according to any of claims 1 to 11 , wherein the feed MF in (1 ) is a feed stream and contacting in (3) is conducted as a continuous process.

13. The process according to any of claims 2 to 12, further comprising

14. The process according to any of claims 1 to 13, wherein the feed MF according to (1) has not been subject to a hydrodeoxygenation treatment.

15. The process according to any of claims 1 to 14, wherein the feed MF according to (1 ) is a merged feed of two or more sub-feeds, wherein at least one of the two or more sub-feeds comprises one or more oxygen containing compounds comprising, independently of one another, one or more alkyl chains, wherein the alkyl chains have, independently of one another, a length n with 4 < n < 30.