An integrated process for the production of LPG and bionaptha from oxygen-containing compounds

Abstract

The present invention relates to an integrated process for the production of C1 to C12 alkanes, comprising (1) providing a feed F1 comprising one or more oxygen containing compounds comprising one or more C6 to C30 alkyl chains; (2) providing a catalyst C1 comprising one or more metals; (3) contacting the feed F1 provided in (1) with the catalyst C1 in an H2-containing atmosphere, obtaining a stream S1 comprising one or more compounds selected from the group consisting of C1 to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes; (4) separating at least part of the one or more compounds selected from the group consisting of C1 to C4 alkanes, and at least part of the one or more compounds selected from the group consisting of C5 to C12 alkanes, from the stream S1 obtained in (3), obtaining a stream S2 comprising the one or more compounds selected from the group consisting of C1 to C4 alkanes and a stream S3 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes; (5.1) pyrolyzing at least part of the stream S2, obtaining a stream S4 comprising H2; (5.2) providing the stream S4 to (3) as a source of H2 for the H2-containing atmosphere in (3).

Description

[0001] An integrated process for the production of LPG and bionaptha from oxygen-containing compounds

[0002] TECHNICAL FIELD

[0003] The present invention relates to an integrated process for the production of Ci to C4 alkanes, comprising a feed comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains.

[0004] INTRODUCTION

[0005] 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.

[0006] 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.

[0007] 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.

[0008] US 11 326 110 B2 concerns a process for hydrotreating a feedstock comprising renewable sources.

[0009] US 2016 / 289576 A1 relates to an integrated process for producing hydrocarbons from renewable sources, which includes a hydroprocessing step.

[0010] CN 113 913 210 A concerns a method for hydroprocessing biological feedstocks.

[0011] Despite the advances made in the hydrocracking of suitable feedstocks, there remains the need for energy- and cost-efficient hydrocracking processes displaying a reduced CO2 footprint. DETAILED DESCRIPTION

[0012] Thus, it was an object of the present invention to provide an improved process for hydrocracking. Said object is achieved by the 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 process for hydrocracking, in particular with regard to the product selectivity towards LPG and / or naphtha grade cracking products, may be provided by the inventive process. In addition thereto, it has unexpectedly been found that pyrolyzing the lightest alkane fraction obtained from a hydrocracking step allows for the production of hydrogen which may be recycled to the hydrocracking step without producing any carbon dioxide. Rather, pyrolysis of said fraction not only allows for a highly effective sequestration of the carbon product, but even allows for obtaining carbon in the form of a value product (e.g. as high purity carbon in various forms such as carbon black, carbon powder, or granular carbon). Further, it has been found that the obtained LPG cracking products can be subjected to steam reforming toward H2 which can be equally reintroduced into the hydrocracking process.

[0013] Therefore, the present invention relates to an integrated process for the production of Ci to C12 alkanes, comprising

[0014] (1 ) providing a feed F1 comprising, preferably consisting of, one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;

[0015] (2) providing a catalyst C1 , preferably a heterogeneous catalyst C1 , comprising one or more metals, preferably one or more transition metals;

[0016] (3) contacting the feed F1 provided in (1) with the catalyst C1 in an ^-containing atmosphere, obtaining a stream S1 comprising one or more compounds selected from the group consisting of Ci to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes;

[0017] (4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 alkanes, and at least part of the one or more compounds selected from the group consisting of C5 to C12 alkanes, from the stream S1 obtained in (3), obtaining a stream S2 comprising, preferably consisting of, the one or more compounds selected from the group consisting of Ci to C4 alkanes and a stream S3 comprising, preferably consisting of, the one or more compounds selected from the group consisting of C5 to C12 alkanes;

[0018] (5.1) pyrolyzing at least part of the stream S2, obtaining a stream S4 comprising H2;

[0019] (5.2) providing the stream S4 to (3) as a source of H2 for the ^-containing atmosphere in (3).

[0020] Within the meaning of the present invention, hydrocarbon pyrolysis may be carried out according to methods known to the person skilled in the art. Such methods are for example disclosed in Muradov et aL, International Journal Hydrogen Energy 2008, 33, 6804-6839; Abbas et aL, International Journal Hydrogen Energy 2010, 35, 1160-1190; Dagle et al. in An Overview of Natu- ral Gas Conversion Technologies for Co-Production of Hydrogen and Value-Added Solid Carbon Products, Report by Argonne National Laboratory and Pacific Northwest National Laboratory (ANL-17 / 11 , PNNL-26726, November 2017); WO 2015 / 116797 and WO 2015 / 116800 (plasma pyrolysis); WO 2020 / 161192 and WO 2021 / 183959 (metal melting / metal salt melting); US 2982622, WO 2019 / 145279, WO 2020 / 200522, and WO 2023 / 057242 (moving bed processes); WO 2011 / 029144 and WO 2016 / 154666 (fluidized bed catalytic processes);

[0021] WO 2020 / 118417 and US 2022 / 0185664 (partial / pulsed combustion); US 2982622, WO 2019 / 145279, and WO 2020 / 200522 (resistive heating or Joule heating). The moving bed processes are particularly advantageous due to their high efficiency, heat integration, flexibility, and favorable product carbon footprint. These processes differ in the form of the energy used (thermal, electrical, etc.), the process conditions (temperature, pressure, etc.), the catalysts, and / or auxiliary materials used.

[0022] It is preferred that the feed F1 provided according to (1) comprises, more preferably consists of, one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C28 alkyl chains, preferably one or more Ce to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains.

[0023] It is preferred that the one or more oxygen containing compounds comprised in the feed F1 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.

[0024] It is preferred that the feed F1 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, more 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.-%.

[0025] It is preferred that the feed F1 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 F 1 , more preferably from 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%.

[0026] It is preferred that the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof.

[0027] In the case that the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof, it is preferred that the one or more oxygen containing compounds comprise, more 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. Further, it is preferred that the one or more oxygen containing compounds in the feed F1 in (1) are selected from the group consisting of triglycerides of vegetable or animal origin, derivatives of triglycerides of vegetable or animal origin, and mixtures thereof.

[0028] Yet further, 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, seaweed oil, 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.

[0029] Yet further, 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.

[0030] It is preferred that the feed F1 in (1) comprises of 50 wt.-% or more of fatty acid esters and / or free fatty acids, more 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.

[0031] In the case that the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof, it is preferred that the animal fats and vegetable oils are at least partially hydrogenated, more preferably hydrogenated.

[0032] In the case that the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof, it is preferred that the feed F1 in (1 ) comprises, more preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

[0033] In the case that the feed F1 in (1) comprises pyrolysis oil, 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.

[0034] In the case that the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof, it is preferred that the feed F1 in (1 ) comprises, more preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms. In the case that the feed F1 in (1 ) comprises pyrolysis oil, it is preferred that the feed F1 in (1 ) comprises of 50 wt.-% or more of pyrolysis oil, more 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.

[0035] It is preferred that step (1 ) comprises

[0036] (1.1 ) optionally adding water to a feed F0 comprising biomass, obtaining a feed F0’;

[0037] (1.2) pyrolyzing a feed F0 comprising biomass, or a feed F0’ obtained according to (1.1), obtaining a stream SO comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;

[0038] (1 .3) separating the solid faction from the stream SO obtained according to (1 .2), obtaining a stream SO’ comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;

[0039] (1 .4) separating the aqueous faction from the stream SO’ obtained according to (1 .3), obtaining one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains.

[0040] In the case that the process comprises steps (1 .1) to (1 .4), it is preferred that the biomass is selected from the group consisting of plant biomass, animal biomass, municipal waste biomass and mixtures of two or more thereof, more preferably wherein the plant biomass is selected from the group consisting of agricultural products, forestry products, agricultural waste, forestry waste, and mixtures of two or more thereof, more preferably wherein the plant biomass is selected from the group consisting of wood, pellets, sawdust, aspen wood, wood chips, grasses, grain residues, vegetables, fruits, sugar, starches, algae, seaweed, silage, sewage, waste grain, fodder leftovers, and mixtures of two or more thereof, more preferably wherein the municipal waste biomass is selected from the group consisting of house waste, industrial waste, and mixtures thereof, more preferably wherein the municipal waste biomass is selected from the group consisting of sludge, grease, paper, pulp, textiles, rubber, plastics, tires, crude oil processing waste, and mixtures of two or more thereof, more preferably wherein the animal biomass is manure. Further, it is preferred that the temperature during pyrolysis in (1.2) is in the range of from 200 to 700 °C, more preferably in the range of from 300 to 600 °C, more preferably in the range of from 400 to 550 °C. Yet further, it is preferred that the pressure during pyrolysis in (1 .2) is in the range of from 0.1 to 200 bar, more preferably in the range of from 1 to 150 bar, more preferably in the range of from 10 to 100 bar.

[0041] It is preferred that the feed F1 in (1) is a feed stream and contacting in (3) is conducted as a continuous process.

[0042] It is preferred that the feed F1 according to (1) has not been subject to a hydrodeoxygenation treatment, wherein more preferably the feed F1 according to (1) has not been subject to a deoxygenation treatment. It is preferred that the one or more metals comprised in catalyst C1 are selected from the group consisting of Ni, Co, Pt, Pd, Rh, Mo, and W, more preferably from the group consisting of Ni, Co, Pt, Pd, and Rh, wherein more preferably catalyst C1 comprises one or more of Ni and Pt.

[0043] It is preferred that the catalyst C1 in (2) comprises a zeolitic material, wherein more preferably the zeolitic material is loaded with the one or more metals.

[0044] In case that the catalyst C1 in (2) comprises a zeolitic material, it is preferred that the zeolitic material 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, PCR, 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, or a mixed structure type of two or more thereof, more preferably an AFS, AFY, BEA, BEC, 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.

[0045] Further, it is preferred that the zeolitic material in (2) has a BEA type framework structure, and wherein the zeolitic material 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, more preferably zeolite beta. In case that 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, more preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 35, more preferably from 20 to 30.

[0046] Alternatively, it is preferred that the zeolitic material in (2) has an MOR type framework structure, and wherein the zeolitic material 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 , more preferably mordenite. In case that 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, more preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 30, more preferably from 15 to 25.

[0047] As a third alternative, it is preferred that the zeolitic material in (2) has a FAU type framework structure, and wherein the zeolitic material 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, more preferably US-Y. In case that 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, more preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

[0048] As a fourth alternative, it is preferred that the zeolitic material in (2) has an MFI type framework structure, and wherein the zeolitic material is selected from the group consisting of ZSM-5, Sili- calite, 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, more preferably ZSM-5. In case that the zeolitic material in (2) has an MFI 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, more preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

[0049] It is preferred that the one or more compounds comprised in the stream S1 obtained in (3) comprise one or more unbranched and / or branched alkanes, more preferably one or more unbranched alkanes.

[0050] In case that the one or more compounds comprised in the stream S1 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, more preferably from 1 :1 .5 to 1 :3.5, more preferably from 1 :2 to 1 :3. Further, it is preferred that the one or more compounds comprised in the stream S1 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, more preferably from 1 :2 to 1 :4.5, more preferably from 1 :3 to 1 :4.

[0051] Alternatively, in case that the one or more compounds comprised in the stream S1 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 , more preferably from 1 .5:1 to 3.5:1 , more preferably from 2:1 to 3:1 . Further, it is preferred that the molar ratio of unbranched to monobranched alkenes is in the range of from 1 :1 to 5:1 , more preferably from 1.5:1 to 4: 1 , more preferably from 2:1 to 3: 1 .

[0052] In case that the catalyst C1 in (2) comprises a zeolitic material, 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, more preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof.

[0053] Further, it is preferred that the one or more metals loaded on the zeolitic material in (2) are group 9 to 11 metals, more preferably group 10 metals, more preferably selected from the group consisting of Fe, N i, Co, Pt, Pd, Rh, and mixtures thereof, more preferably Ni, Pt, and mixtures thereof, more preferably Ni or Pt.

[0054] Yet further, it is preferred that the catalyst C1 in (2) contains Pt, wherein more preferably the ze- olitic 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, more 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.-%.

[0055] Yet further, it is preferred that the catalyst C1 in (2) contains Ni, wherein more 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, more 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.-%.

[0056] Yet further, 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.

[0057] In case that 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 more preferably Al. Further, it is preferred that Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is more preferably Si.

[0058] In case that the catalyst C1 in (2) comprises a zeolitic material, it is preferred that the surface area of the zeolitic material in (2) ranges of from 350 to 900 m2 / g, more 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.

[0059] It is preferred that the heterogeneous catalyst in (2) further comprises a binder, wherein the binder more 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.

[0060] It is preferred that the heterogeneous catalyst in (2) is provided as a shaped body, more 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.

[0061] In case that 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, more preferably a trilobe or a quadrilobe. Further, it is preferred that from 95 to 100 wt.-% of the heterogeneous catalyst provided in (2) consists of the zeolitic material and the optional binder, more 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.

[0062] Yet further, it is preferred that the binder content of the heterogeneous catalyst in (2) ranges of from 10 to 90 wt.-%, more 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.-%.

[0063] Yet further, it is preferred that the preparation of the heterogeneous catalyst according to (2) comprises,

[0064] (2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture Ma;

[0065] (2.b) extruding the mixture Maobtained according to (2a);

[0066] (2.c) optionally drying the extrudate obtained according to (2.b);

[0067] (2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

[0068] (2.3) optionally reducing the extrudate obtained according to (2.b), (2.c) or (2.d);

[0069] (2.f) optionally passivating the extrudate obtained according to (2.b), (2.c), (2.d) or (2.e).

[0070] Yet further, it is preferred that the preparation of the heterogeneous catalyst C1 according to (2) comprises,

[0071] (2. a’) mixing a binder and a zeolitic material, obtaining a mixture Ma;

[0072] (2.b’) extruding the mixture Maobtained according to (2. a’);

[0073] (2.c’) optionally drying the extrudate obtained according to (2.b’);

[0074] (2.d’) impregnating the extrudate obtained according to (2.b’), more 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;

[0075] (2.e’) optionally drying the impregnated extrudate obtained according to (2.d’);

[0076] (2.f’) optionally calcining the impregnated extrudate obtained according to (2.d’), more preferably obtained according to (2.e’);

[0077] (2.g’) optionally reducing the impregnated extrudate obtained according to (2.d’), more preferably according to (2.e’), more preferably according to (2.f’);

[0078] (2.h’) optionally passivating the extrudate obtained according to (2.d’), (2.e’), (2.f’) or (2.g’). In case that the integrated process 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, more 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. Further, 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’) more preferably comprises an inert gas, preferably nitrogen and / or argon, more preferably comprises nitrogen.

[0079] Yet further, 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, more preferably from 12 to 36 h, more preferably from 20 to 28 h.

[0080] Yet further, 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, more 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.

[0081] Yet further, 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’) more preferably comprises a reducing gas, more preferably comprises hydrogen.

[0082] Yet further, 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, more preferably from 8 to 24 h, more preferably from 10 to 14 h.

[0083] Yet further, 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, more preferably from 60 to 150 °C, more preferably from 70 to 100 °C.

[0084] Yet further, 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, more preferably from 3 to 28 h, more preferably from 6 to 20 h.

[0085] Yet further, it is preferred that the binder is a colloid or a colloidal dispersion.

[0086] Yet further, it is preferred that prior to (2. a) the binder is subject to a peptization step.

[0087] In case that prior to (2. a) the binder is subject to a peptization step, 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, more preferably in the range of from 5 to 30 wt.-%, more preferably in the range of from 10 to 20 wt.-%. In case that the catalyst C1 in (2) comprises a zeolitic material, it is preferred that the zeolitic material content of the heterogeneous catalyst in (2) ranges of from 20 to 90 wt.-%, more 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.-%.

[0088] It is preferred that the process includes a step of regenerating the heterogeneous catalyst in (2) after contacting with the feed F1 in (3) wherein the catalyst is more preferably regenerated by steaming at a temperature in the range of from 300 to 800 °C, more preferably from 350 to 700 °C, more preferably from 400 to 600 °C, more preferably from 450 to 500 °C.

[0089] It is preferred that contacting in (3) is conducted at a temperature in the range of from 150 to 800 °C, more preferably from 170 to 600 °C, more preferably from 190 to 500 °C, and more preferably from 200 to 400 °C.

[0090] It is preferred that contacting in (3) is conducted at a pressure in the range of from 20 to 200 bara, more preferably from 25 to 150 bara, more preferably from 30 to 100 bara, more preferably from 35 to 80 bara, and more preferably from 40 to 60 bara.

[0091] It is preferred that contacting in (3) is conducted at a weight hourly space velocity in the range of from 0.1 to 5 IT1, more 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.

[0092] It is preferred that contacting in (3) is conducted in a fixed bed reactor or a fluidized bed reactor, more preferably in a fixed bed reactor.

[0093] It is preferred that the H2-containing atmosphere in (3) consists of hydrogen.

[0094] In case that the H2-containing atmosphere in (3) consists of hydrogen, it is preferred that in (3) the H2-containing 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.

[0095] It is preferred that during contacting according to (3) the pressure is in the range of from 10 to 200 bar, more 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.

[0096] It is preferred that during contacting according to (3) the temperature is in the range of from 150 to 350 °C, more 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 F1 according to (1) is contacted with the catalyst C1 according to (2) in (3) is in the range of from 0.1 to 5 IT1, more 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.

[0097] It is preferred that the feed F1 provided in (1 ) and contacted with the catalyst C1 according to (3) is in the liquid phase and / or the gas phase, more preferably in the gas phase.

[0098] It is preferred that the methane content of the stream S1 obtained in (3) is 1 wt.-% or less, more preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less.

[0099] It is preferred that the stream S1 obtained in (3) comprises one or more branched and / or unbranched alkanes, more 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.

[0100] Alternatively, it is preferred that the stream S1 obtained in (3) comprises one or more branched and / or unbranched alkanes, more 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.

[0101] It is preferred that during contacting in (3) 75 % or more of the feed F1 is cracked, more 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 F1 is cracked.

[0102] It is preferred that contacting in (3) is conducted in a trickle-bed reactor or an ebullated bed reactor, more preferably a plug-flow trickle-bed reactor.

[0103] In case that contacting in (3) is conducted in a trickle-bed reactor or an ebulatted 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). Further, it is preferred that the number of stacked layers is in the range of from 2 to 30, more preferably from 3 to 20, more preferably from 4 to 10. Yet further, it is preferred that the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers. In case that the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers, it is preferred that 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.

[0104] Alternatively, 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.

[0105] It is preferred that step (4) comprises, more preferably consists of,

[0106] (4.1) feeding the stream S1 obtained in (3) into a vapor-liquid separator, obtaining a liquid fraction LF1 comprising one or more compounds selected from the group consisting of Ci to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes, and a gaseous fraction GF1 comprising H2 and CO2;

[0107] (4.2) separating H2 from the gaseous fraction GF1 obtained in (4.1 ), obtaining a gaseous fraction GF2 comprising H2 and a gaseous fraction GF3 comprising CO2;

[0108] (4.3) providing the gaseous fraction GF2 to (3) as a source of H2 for the H2-containing atmosphere in (3);

[0109] (4.4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 alkanes from the liquid fraction LF1 obtained in (4.1 ), obtaining a stream S2 comprising, more preferably consisting of, the one or more compounds selected from the group consisting of Ci to C4 alkanes and a stream S3 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes.

[0110] In case that the integrated process comprises steps (4.1 ) to (4.4), it is preferred that (4.4) further comprises separating one or more compounds selected from the group consisting of C13 to C30 alkanes and / or one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains from the liquid fraction LF1 obtained in (4.1), obtaining a stream S3 comprising, more preferably consisting of, the one or more compounds selected from the group consisting of C5 to C12 alkanes.

[0111] Further, it is preferred that step (4) further comprises

[0112] (4.5) providing the separated one or more compounds selected from the group consisting of C13 to C30 alkanes and / or one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains obtained in (4.4) to (1 ) as a source of one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains for preparing the feed F1 in (1 ).

[0113] It is preferred that separation in (4) is achieved by distillation, more preferably by fractionated distillation.

[0114] It is preferred that the temperature during pyrolysis in (5.1 ) is in the range of from 500 to 900 °C, more preferably in the range of from 600 to 850 °C, more preferably in the range of from 700 to 800 °C. It is preferred that the pressure during pyrolysis in (5.1 ) is in the range of from 0.1 to 200 bar, more preferably in the range of from 1 to 150 bar, more preferably in the range of from 10 to 100 bar.

[0115] It is preferred that (5.1) further comprises obtaining a solid carbon product.

[0116] It is preferred that pyrolysis in (5.1 ) is conducted with a catalyst.

[0117] In case that pyrolysis in (5.1 ) is conducted with a catalyst, it is preferred that the catalyzed pyrolysis is conducted as a fixed bed or a moving bed process, more preferably as a moving bed process, more preferably as a fluidized bed process. Further, it is preferred that the solid carbon product generated from catalyzed pyrolysis is granular carbon.

[0118] Alternatively, it is preferred that pyrolysis in (5.1 ) is conducted thermally, preferably without a catalyst.

[0119] In case that pyrolysis in (5.1) is conducted thermally and preferably without a catalyst, it is preferred that the heat input for thermal pyrolysis in (5.1) is via one or more selected from the list consisting of plasma, microwave, heated carrier gas, resistive heating, induction, liquid metal processes, autothermal heating, metal melting, metal salt melting, partial combustion, and pulsed combustion, wherein more preferably the heat input for pyrolysis in (5.1 ) is via resistive heating. Further, it is preferred that the heat input for thermal pyrolysis in (5.1 ) is via plasma and the solid carbon product generated from thermal pyrolysis is carbon black. Alternatively, it is further preferred that the heat input for thermal pyrolysis in (5.1 ) is via liquid metal processes and the solid carbon product generated from thermal pyrolysis is carbon powder.

[0120] Further, in case that pyrolysis in (5.1) is conducted thermally and preferably without a catalyst, it is preferred that the energy input for thermal pyrolysis in (5.1 ) is electrical energy.

[0121] In case that (5.1 ) further comprises obtaining a solid carbon product, it is preferred that the process further comprises

[0122] (5.3) collecting the solid carbon product, preferably by a cyclone or by filtration, more preferably by a cyclone;

[0123] (5.4) post-treatment of the solid carbon product.

[0124] Further, it is preferred that the post-treatment in (5.4) includes agglomeration of the solid carbon product, preferably granulation of the solid carbon product.

[0125] Yet further, it is preferred that the post-treatment in (5.4) includes purification of the solid carbon product, preferably by washing and / or evaporation. In case that (5.1 ) further comprises obtaining a solid carbon product, it is further preferred that after (5.1 ) and prior to (5.2), stream S4 is subject to a purification treatment, preferably by pressure swing adsorption.

[0126] It is preferred that the integrated process further comprises

[0127] (5.1 ’) adding CO2 to part of the stream S2, obtaining a stream S5;

[0128] (5.2’) providing a catalyst C2 comprising one or more of metals selected from the group consisting of Ni, Cr, Mo, Fe, Co, Cu, Pt, Pd, Rh, Ru, Os, Zr, Al, Si, Ti, Mg and Ir;

[0129] (5.3’) contacting the stream S5 obtained according to (5.1 ’) with the catalyst C2, obtaining a stream S6 comprising H2 and CO.

[0130] In case that the integrated process comprises steps (5.1 ’) to (5.3’), it is preferred that at least part of the CO2 added according to (5.1 ’) comprises the gaseous fraction GF3 separated according to (4.2).

[0131] Further, it is preferred that at least part of the CO2 added according to (5.1 ’) comprises CO2 from an industrial process, more preferably wherein the industrial process is one or more of a combustion process of biomass, a coal gasification, a steam reforming, and a reverse water gas shift process.

[0132] Yet further, it is preferred that contacting in (5.3’) is conducted at a temperature in the range of from 500 to 1000 °C, more preferably in the range of from 600 to 950 °C, more preferably in the range of from 650 to 850 °C.

[0133] Yet further, it is preferred that contacting in (5.3’) is conducted at a pressure in the range of from 1 to 40 bar, more preferably in the range of from 2 to 30 bar, more preferably in the range of from 5 to 25 bar.

[0134] Yet further, it is preferred that the molar ratio of CO to H2 in the stream S6 obtained according to (5.3’) is in the range of from 1 :1 to 1 :20, more preferably in the range of from 1 :2 to 1 :10, more preferably in the range of from 1 :3 to 1 :5.

[0135] It is preferred that the integrated process further comprises

[0136] (6) adding H2O to the stream S3 obtained in (4) or (4.4), obtaining a stream S7;

[0137] (7) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S7, obtaining a stream S8 comprising H2, methane, ethane, olefins and aromatic hydrocarbons;

[0138] (8) separating at least part of the H2, methane and ethane from the stream S8, obtaining a stream S9 comprising, more preferably consisting of, the separated H2, methane and ethane. In case that the integrated process comprises steps (6) to (8), it is preferred that the stream S7 contains in the range of from 10 to 95 vol.-% of H2O, more preferably from 20 to 80 vol.-% of H2O, more preferably from 30 to 60 vol.-% of H2O.

[0139] Further, it is preferred that steam cracking in (7) is conducted at a temperature in the range of from 500 to 950 °C, more preferably from 600 to 920 °C, more preferably from 650 to 900 °C, more preferably from 700 to 880 °C, and more preferably from 750 to 850 °C.

[0140] Yet further, it is preferred that steam cracking in (7) is conducted at a pressure in the range of from 1 to 5 bara, more preferably from 1 .3 to 3.5 bara, more preferably from 1 .5 to 3 bara, and more preferably from 1 .7 to 2.5 bara.

[0141] Yet further, it is preferred that separation in (8) is achieved by distillation, more preferably by fractionated distillation.

[0142] Yet further, it is preferred that after (7) and prior to the separation in (8), the stream S8 is cooled to a temperature in the range of from -60 to -29 °C, more preferably from -55 to -31 °C, more preferably from -50 to -33 °C, and more preferably from -45 to -35 °C.

[0143] Yet further, it is preferred that step (8) further comprises

[0144] (8.1) optionally separating at least part of the H2 from stream S9, obtaining a stream S12 containing H2;

[0145] (8.2) providing the stream S9 comprising methane and ethane to (5.1).

[0146] Alternatively, it is preferred that step (8) further comprises

[0147] (8.1 ’) separating H2 from stream S9, obtaining a stream S13 containing H2 and a stream S14 comprising methane and ethane;

[0148] (8.2’) providing the stream S14 to (5.1 ’).

[0149] In case that the integrated process comprises steps (6) to (8), it is preferred that at least part of the stream S2 obtained according to (4) or (4.4) is provided as fuel for the steam cracking according to (7). In case that at least part of the stream S2 obtained according to (4) or (4.4) is provided as fuel for the steam cracking according to (7), it is preferred that at least part of the CO2 added according to (5.1 ’) comprises the CO2 obtained during the combustion of S2 as fuel for the steam cracking according to (7).

[0150] It is preferred that step (5.2) comprises

[0151] (5.2a) mixing the stream S4 with a stream S10 comprising H2 and / or stream S12 obtained according to (8.1 ) and / or stream S13 obtained according to (8.1 ’), obtaining a stream S11 ;

[0152] (5.2b) providing the stream S11 to (3) as a source of H2 for the H2-containing atmosphere in (3). In case that the integrated process comprises steps (5.2a) to (5.2b), it is preferred that the stream S10 is provided from one or more of biogas reforming, water electrolysis, NH3 cracking, and methanol cracking.

[0153] 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 integrated 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.

[0154] 1 . An integrated process for the production of Ci to C12 alkanes, comprising

[0155] (1 ) providing a feed F1 comprising, preferably consisting of, one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;

[0156] (2) providing a catalyst C1 , preferably a heterogeneous catalyst C1 , comprising one or more metals, preferably one or more transition metals;

[0157] (3) contacting the feed F1 provided in (1 ) with the catalyst C1 in an H2-containing atmosphere, obtaining a stream S1 comprising one or more compounds selected from the group consisting of Ci to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes;

[0158] (4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 alkanes, and at least part of the one or more compounds selected from the group consisting of C5 to C12 alkanes, from the stream S1 obtained in (3), obtaining a stream S2 comprising, preferably consisting of, the one or more compounds selected from the group consisting of Ci to C4 alkanes and a stream S3 comprising, preferably consisting of, the one or more compounds selected from the group consisting of C5 to C12 alkanes;

[0159] (5.1 ) pyrolyzing at least part of the stream S2, obtaining a stream S4 comprising H2;

[0160] (5.2) providing the stream S4 to (3) as a source of H2 for the H2-containing atmosphere in (3).

[0161] 2. The integrated process according to embodiment 1 , wherein the feed F1 provided according to (1 ) comprises, preferably consists of, one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C28 alkyl chains, preferably one or more Ce to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains. 3. The integrated process according to embodiment 1 or 2, wherein the one or more oxygen containing compounds comprised in the feed F1 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.

[0162] 4. The integrated process according to any one of embodiments 1 to 3, wherein the feed F1 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.-%.

[0163] 5. The integrated process according to any one of embodiments 1 to 4, wherein the feed F1 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 F1 , preferably from 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%.

[0164] 6. The integrated process according to any one of embodiments 1 to 5, wherein the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof.

[0165] 7. The integrated process according to embodiment 6, 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.

[0166] 8. The integrated process according to embodiment 6 or 7, wherein the one or more oxygen containing compounds in the feed F1 in (1) are selected from the group consisting of triglycerides of vegetable or animal origin, derivatives of triglycerides of vegetable or animal origin, and mixtures thereof.

[0167] 9. The integrated process according to any one of embodiments 6 to 8, 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, seaweed oil, 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.

[0168] 10. The integrated process according to any one of embodiments 6 to 9, 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.

[0169] 11 . The integrated process according to any one of embodiments 1 to 10, wherein the feed F1 in (1) comprises of 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.

[0170] 12. The integrated process according to embodiments 7 to 12, wherein the animal fats and vegetable oils are at least partially hydrogenated, preferably hydrogenated.

[0171] 13. The integrated process according to embodiment 6, wherein the feed F1 in (1 ) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

[0172] 14. The integrated process according to embodiment 13, 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.

[0173] 15. The integrated process according to any one of embodiments 6 to 14, wherein the feed F1 in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms.

[0174] 16. The integrated process according to any one of embodiments 13 to 15, wherein the feed F1 in (1) comprises of 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.

[0175] 17. The integrated process according to any one of embodiments 1 to 16, wherein (1) comprises

[0176] (1.1 ) optionally adding water to a feed F0 comprising biomass, obtaining a feed F0’;

[0177] (1 .2) pyrolyzing a feed F0 comprising biomass, or a feed F0’ obtained according to (1.1), obtaining a stream SO comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;

[0178] (1 .3) separating the solid faction from the stream SO obtained according to (1 .2), obtaining a stream SO’ comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains; (1 .4) separating the aqueous faction from the stream SO’ obtained according to (1 .3), obtaining one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains.

[0179] 18. The integrated process according to embodiment 17, wherein the biomass is selected from the group consisting of plant biomass, animal biomass, municipal waste biomass and mixtures of two or more thereof, preferably wherein the plant biomass is selected from the group consisting of agricultural products, forestry products, agricultural waste, forestry waste, and mixtures of two or more thereof, more preferably wherein the plant biomass is selected from the group consisting of wood, pellets, sawdust, aspen wood, wood chips, grasses, grain residues, vegetables, fruits, sugar, starches, algae, seaweed, silage, sewage, waste grain, fodder leftovers, and mixtures of two or more thereof, preferably wherein the municipal waste biomass is selected from the group consisting of house waste, industrial waste, and mixtures thereof, more preferably wherein the municipal waste biomass is selected from the group consisting of sludge, grease, paper, pulp, textiles, rubber, plastics, tires, crude oil processing waste, and mixtures of two or more thereof, preferably wherein the animal biomass is manure.

[0180] 19. The integrated process according to embodiment 17 or 18, wherein the temperature during pyrolysis in (1.2) is in the range of from 200 to 700 °C, preferably in the range of from 300 to 600 °C, more preferably in the range of from 400 to 550 °C.

[0181] 20. The integrated process according to any one of embodiments 17 to 19, wherein the pressure during pyrolysis in (1 .2) is in the range of from 0.1 to 200 bar, preferably in the range of from 1 to 150 bar, more preferably in the range of from 10 to 100 bar.

[0182] 21 . The integrated process according to any one of embodiments 1 to 20, wherein the feed F1 in (1) is a feed stream and contacting in (3) is conducted as a continuous process.

[0183] 22. The integrated process according to any one of embodiments 1 to 21 , wherein the feed F1 according to (1) has not been subject to a hydrodeoxygenation treatment, wherein preferably the feed F1 according to (1 ) has not been subject to a deoxygenation treatment.

[0184] 23. The integrated process according to any one of embodiments 1 to 22, wherein the one or more metals comprised in catalyst C1 are selected from the group consisting of Ni, Co, Pt, Pd, Rh, Mo, and W, preferably from the group consisting of Ni, Co, Pt, Pd, and Rh, wherein more preferably catalyst C1 comprises one or more of Ni and Pt. 24. The integrated process according to any one of embodiments 1 to 23, wherein the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the zeolitic material is loaded with the one or more metals.

[0185] 25. The integrated process according to embodiment 24, wherein the zeolitic material 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, PCR, 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, or a mixed structure type of two or more thereof, preferably an AFS, AFY, BEA, BEC, 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.

[0186] 26. The integrated process according to embodiment 24 or 25, wherein the zeolitic material in (2) has a BEA type framework structure, and wherein the zeolitic material 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.

[0187] 27. The integrated process according to embodiment 26, 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.

[0188] 28. The integrated process according to embodiment 24 or 25, wherein the zeolitic material in (2) has an MOR type framework structure, and wherein the zeolitic material 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.

[0189] 29. The integrated process according to embodiment 28, 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 30, more preferably from 15 to 25.

[0190] 30. The integrated process according to embodiment 24 or 25, wherein the zeolitic material in (2) has an FAU type framework structure, and wherein the zeolitic material 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.

[0191] 31 . The integrated process according to embodiment 30, 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.

[0192] 32. The integrated process according to embodiment 24 or 25, wherein the zeolitic material in (2) has an MFI type framework structure, and wherein the zeolitic material 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.

[0193] 33. The integrated process according to embodiment 32, 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.

[0194] 34. The integrated process according to any one of embodiments 1 to 33, wherein the one or more compounds comprised in the stream S1 obtained in (3) comprise one or more unbranched and / or branched alkanes, preferably one or more unbranched alkanes.

[0195] 35. The integrated process according to embodiment 34, wherein the one or more compounds comprised in the stream S1 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.

[0196] 36. The integrated process according to embodiment 34 or 35, wherein the one or more compounds comprised in the stream S1 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.

[0197] 37. The integrated process according to embodiment 34, 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.

[0198] 38. The integrated process according to any one of embodiments 34 to 37, wherein the molar ratio of unbranched to monobranched 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. 39. The integrated process according to any one of embodiments 24 to 38, 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.

[0199] 40. The integrated process according to any one of embodiments 24 to 38, 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.

[0200] 41 . The integrated process according to any one of embodiments 24 to 40, wherein the catalyst C1 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.-%.

[0201] 42. The integrated process according to any one of embodiments 24 to 41 wherein the catalyst C1 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.-%.

[0202] 43. The integrated process according to any one of embodiments 24 to 42, 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.

[0203] 44. The integrated process according to embodiment 43, wherein X is selected from the group consisting of Al, B, Ga and combinations thereof, wherein X is preferably AL

[0204] 45. The integrated process according to embodiment 43 or 44, wherein Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is preferably Si.

[0205] 46. The integrated process according to any one of embodiments 24 to 45, 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.

[0206] 47. The integrated process according to any one of embodiments 1 to 46, 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.

[0207] 48. The integrated process according to any one of embodiments 1 to 47, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably as an extrudate.

[0208] 49. The integrated process according to any one of embodiments 1 to 47, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably a 3D printed structure.

[0209] 50. The integrated process according to embodiment 48 or 49, 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.

[0210] 51 . The integrated process according to any one of embodiments 47 to 50, wherein from 95 to 100 wt.-% of the heterogeneous catalyst provided in (2) consists of the zeolitic material 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.

[0211] 52. The integrated process according to any one of embodiments 47 to 51 , 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.-%.

[0212] 53. The integrated process according to any one of embodiments 47 to 52, wherein the preparation of the heterogeneous catalyst according to (2) comprises,

[0213] (2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture Ma;

[0214] (2.b) extruding the mixture Maobtained according to (2a);

[0215] (2.c) optionally drying the extrudate obtained according to (2.b);

[0216] (2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

[0217] (2.3) optionally reducing the extrudate obtained according to (2.b), (2.c) or (2.d);

[0218] (2.f) optionally passivating the extrudate obtained according to (2.b), (2.c), (2.d) or (2.e). 54. The integrated process according to any one of embodiments 47 to 52, wherein the preparation of the heterogeneous catalyst C1 according to (2) comprises,

[0219] (2. a’) mixing a binder and a zeolitic material, obtaining a mixture Ma;

[0220] (2.b’) extruding the mixture Maobtained according to (2. a’);

[0221] (2.c’) optionally drying the extrudate obtained according to (2.b’);

[0222] (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;

[0223] (2.e’) optionally drying the impregnated extrudate obtained according to (2.d’);

[0224] (2.f’) optionally calcining the impregnated extrudate obtained according to (2.d’), preferably obtained according to (2.e’);

[0225] (2.g’) optionally reducing the impregnated extrudate obtained according to (2.d’), preferably according to (2.e’), more preferably according to (2.f’);

[0226] (2.h’) optionally passivating the extrudate obtained according to (2.d’), (2.e’), (2.f’) or (2.g’).

[0227] 55. The integrated process according to any one of embodiments 53 or 54, 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.

[0228] 56. The integrated process according to any one of embodiments 53 to 55, 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.

[0229] 57. The integrated process according to any one of embodiments 53 to 56, 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.

[0230] 58. The integrated process according to any one of embodiments 53 to 57, 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.

[0231] 59. The integrated process according to any one of embodiments 53 to 58, 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. 60. The integrated process according to any one of embodiments 53 to 59, 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.

[0232] 61 . The integrated process according to any one of embodiments 53 to 60, 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.

[0233] 62. The integrated process according to any one of embodiments 53 to 61 , 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.

[0234] 63. The integrated process according to any one of embodiments 53 to 62, wherein the binder is a colloid or a colloidal dispersion.

[0235] 64. The integrated process according to any one of embodiments 53 to 63, wherein prior to (2. a) the binder is subject to a peptization step.

[0236] 65. The integrated process according to embodiment 64, 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.-%.

[0237] 66. The integrated process according to any one of embodiments 24 to 65, wherein the zeo- litic 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.-%.

[0238] 67. The integrated process according to any one of embodiments 1 to 66, wherein the process includes a step of regenerating the heterogeneous catalyst in (2) after contacting with the feed F1 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.

[0239] 68. The integrated process according to any one of embodiments 1 to 67, wherein contacting in (3) is conducted at a temperature in the range of from 150 to 800 °C, preferably from 170 to 600 °C, more preferably from 190 to 500 °C, and more preferably from 200 to 400 °C.

[0240] 69. The integrated process according to any one of embodiments 1 to 68, wherein contacting in (3) is conducted at a pressure in the range of from 20 to 200 bara, preferably from 25 to 150 bara, more preferably from 30 to 100 bara, more preferably from 35 to 80 bara, and more preferably from 40 to 60 bara.

[0241] 70. The integrated process according to any one of embodiments 1 to 69, wherein contacting in (3) is conducted at a weight hourly space velocity 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.

[0242] 71 . The integrated process according to any one of embodiments 1 to 70, wherein contacting in (3) is conducted in a fixed bed reactor or a fluidized bed reactor, preferably in a fixed bed reactor.

[0243] 72. The integrated process according to any one of embodiments 1 to 71 , wherein the H2- containing atmosphere in (3) consists of hydrogen.

[0244] 73. The integrated process according to embodiment 72, wherein in (3) the H2-containing 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.

[0245] 74. The integrated process according to any one of embodiments 1 to 73, wherein during contacting according to (3) the pressure 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.

[0246] 75. The integrated process according to any one of embodiments 1 to 74, wherein during contacting according to (3) the temperature 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.

[0247] 76. The integrated process according to any one of embodiments 1 to 75, wherein the weight hourly space velocity at which the feed F1 according to (1 ) is contacted with the catalyst C1 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.

[0248] 77. The integrated process according to any one of embodiments 1 to 76, wherein the feed F1 provided in (1 ) and contacted with the catalyst C1 according to (3) is in the liquid phase and / or the gas phase, preferably in the gas phase. 78. The integrated process according to any one of embodiments 1 to 77, wherein the methane content of the stream S1 obtained in (3) is 1 wt.-% or less, preferably 0.5 wt.-% or less, more preferably 0.1 wt.-% or less.

[0249] 79. The integrated process according to any one of embodiments 1 to 78, wherein the stream S1 obtained in (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.

[0250] 80. The integrated process according to any one of embodiments 1 to 78, wherein the stream S1 obtained in (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.

[0251] 81 . The integrated process according to any one of embodiments 1 to 80, wherein during contacting in (3) 75 % or more of the feed F1 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 F1 is cracked.

[0252] 82. The integrated process according to any one of embodiments 1 to 81 , wherein contacting in (3) is conducted in a trickle-bed reactor or an ebullated bed reactor, preferably a plugflow trickle-bed reactor.

[0253] 83. The integrated process according to embodiment 82, wherein trickle-bed reactor comprises a structured catalyst bed which comprises stacked layers of the catalyst according to (2).

[0254] 84. The integrated process according to embodiment 83, 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.

[0255] 85. The integrated process according to any one of embodiments 82 to 84, wherein the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers. The integrated process according to embodiment 85, 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. The integrated process according to embodiment 85, 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. The integrated process according to any one of embodiments 1 to 87, wherein (4) comprises, preferably consists of,

[0256] (4.1 ) feeding the stream S1 obtained in (3) into a vapor-liquid separator, obtaining a liquid fraction LF1 comprising one or more compounds selected from the group consisting of Ci to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes, and a gaseous fraction GF1 comprising H2 and CO2;

[0257] (4.2) separating H2 from the gaseous fraction GF1 obtained in (4.1 ), obtaining a gaseous fraction GF2 comprising H2 and a gaseous fraction GF3 comprising CO2;

[0258] (4.3) providing the gaseous fraction GF2 to (3) as a source of H2 for the H2-containing atmosphere in (3);

[0259] (4.4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 alkanes from the liquid fraction LF1 obtained in (4.1 ), obtaining a stream S2 comprising, preferably consisting of, the one or more compounds selected from the group consisting of Ci to C4 alkanes and a stream S3 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes. The integrated process according to embodiment 88, wherein (4.4) further comprises separating one or more compounds selected from the group consisting of C13 to C30 alkanes and / or one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains from the liquid fraction LF1 obtained in (4.1), obtaining a stream S3 comprising, preferably consisting of, the one or more compounds selected from the group consisting of C5 to C12 alkanes. The integrated process according to any one of embodiment 88 or 89, wherein (4) further comprises

[0260] (4.5) providing the separated one or more compounds selected from the group consisting of C13 to C30 alkanes and / or one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains obtained in (4.4) to (1 ) as a source of one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more Ce to C30 alkyl chains for preparing the feed F1 in (1 ). The integrated process according to any one of embodiments 1 to 90, wherein separation in (4) is achieved by distillation, preferably by fractionated distillation. 92. The integrated process according to any one of embodiments 1 to 91 , wherein the temperature during pyrolysis in (5.1) is in the range of from 500 to 900 °C, preferably in the range of from 600 to 850 °C, more preferably in the range of from 700 to 800 °C.

[0261] 93. The integrated process according to any one of embodiments 1 to 92, wherein the pressure during pyrolysis in (5.1) is in the range of from 0.1 to 200 bar, preferably in the range of from 1 to 150 bar, more preferably in the range of from 10 to 100 bar.

[0262] 94. The integrated process according to any one of embodiments 1 to 93, wherein (5.1) further comprises obtaining a solid carbon product.

[0263] 95. The integrated process according to any one of embodiments 1 to 94, wherein pyrolysis in (5.1) is conducted with a catalyst.

[0264] 96. The integrated process according to embodiment 95, wherein the catalyzed pyrolysis is conducted as a fixed bed or a moving bed process, preferably as a moving bed process, more preferably as a fluidized bed process.

[0265] 97. The integrated process according to embodiment 95 or 96, wherein the solid carbon product generated from catalyzed pyrolysis is granular carbon.

[0266] 98. The integrated process according to any one of embodiments 1 to 94, wherein pyrolysis in (5.1) is conducted thermally, preferably without a catalyst.

[0267] 99. The integrated process according to embodiment 98, wherein the heat input for thermal pyrolysis in (5.1) is via one or more selected from the list consisting of plasma, microwave, heated carrier gas, resistive heating, induction, liquid metal processes, autothermal heating, metal melting, metal salt melting, partial combustion, and pulsed combustion, wherein preferably the heat input for pyrolysis in (5.1) is via resistive heating.

[0268] 100. The integrated process according to embodiment 99, wherein the heat input for thermal pyrolysis in (5.1) is via plasma and the solid carbon product generated from thermal pyrolysis is carbon black.

[0269] 101 . The integrated process according to embodiment 99, wherein the heat input for thermal pyrolysis in (5.1) is via liquid metal processes and the solid carbon product generated from thermal pyrolysis is carbon powder.

[0270] 102. The integrated process according to any one of embodiments 98 to 101 , wherein the energy input for thermal pyrolysis in (5.1) is electrical energy.

[0271] 103. The integrated process according to any one of embodiments 94 to 102, wherein the process further comprises (5.3) collecting the solid carbon product, preferably by a cyclone or by filtration, more preferably by a cyclone;

[0272] (5.4) post-treatment of the solid carbon product.

[0273] 104. The integrated process according to embodiment 103, wherein the post-treatment in (5.4) includes agglomeration of the solid carbon product, preferably granulation of the solid carbon product.

[0274] 105. The integrated process according to embodiment 103 or 104, wherein the post-treatment in (5.4) includes purification of the solid carbon product, preferably by washing and / or evaporation.

[0275] 106. The integrated process according to any one of embodiments 94 to 105, wherein after (5.1) and prior to (5.2), stream S4 is subject to a purification treatment, preferably by pressure swing adsorption.

[0276] 107. The integrated process according to any one of embodiments 1 to 106, wherein the integrated process further comprises

[0277] (5.T) adding CO2 to part of the stream S2, obtaining a stream S5;

[0278] (5.2’) providing a catalyst C2 comprising one or more of metals selected from the group consisting of Ni, Cr, Mo, Fe, Co, Cu, Pt, Pd, Rh, Ru, Os, Zr, Al, Si, Ti, Mg and Ir;

[0279] (5.3’) contacting the stream S5 obtained according to (5.T) with the catalyst C2, obtaining a stream S6 comprising H2 and CO.

[0280] 108. The integrated process according to embodiment 107, wherein at least part of the CO2 added according to (5.T) comprises the gaseous fraction GF3 separated according to (4.2).

[0281] 109. The integrated process according to embodiment 107 or 108, wherein at least part of the CO2 added according to (5.T) comprises CO2 from an industrial process, preferably wherein the industrial process is one or more of a combustion process of biomass, a coal gasification, a steam reforming, and a reverse water gas shift process.

[0282] 110. The integrated process according to any one of embodiments 107 to 109, wherein contacting in (5.3’) is conducted at a temperature in the range of from 500 to 1000 °C, preferably in the range of from 600 to 950 °C, more preferably in the range of from 650 to 850 °C.

[0283] 111. The integrated process according to any one of embodiments 107 to 110, wherein contacting in (5.3’) is conducted at a pressure in the range of from 1 to 40 bar, preferably in the range of from 2 to 30 bar, more preferably in the range of from 5 to 25 bar. 112. The integrated process according to any one of embodiments 107 to 111 , wherein the molar ratio of CO to H2 in the stream S6 obtained according to (5.3’) is in the range of from 1 :1 to 1 :20, preferably in the range of from 1 :2 to 1 :10, more preferably in the range of from 1 :3 to 1 :5.

[0284] 113. The integrated process according to any one of embodiments 1 to 112, wherein the process further comprises

[0285] (6) adding H2O to the stream S3 obtained in (4) or (4.4), obtaining a stream S7;

[0286] (7) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S7, obtaining a stream S8 comprising H2, methane, ethane, olefins and aromatic hydrocarbons;

[0287] (8) separating at least part of the H2, methane and ethane from the stream S8, obtaining a stream S9 comprising, preferably consisting of, the separated H2, methane and ethane.

[0288] 114. The integrated process according to embodiment 113, wherein the stream S7 contains in the range of from 10 to 95 vol.-% of H2O, preferably from 20 to 80 vol.-% of H2O, more preferably from 30 to 60 vol.-% of H2O.

[0289] 115. The integrated process according to embodiment 113 or 114, wherein steam cracking in (7) is conducted at a temperature in the range of from 500 to 950 °C, preferably from 600 to 920 °C, more preferably from 650 to 900 °C, more preferably from 700 to 880 °C, and more preferably from 750 to 850 °C.

[0290] 116. The integrated process according to any one of embodiments 113 to 115, wherein steam cracking in (7) is conducted at a pressure in the range of from 1 to 5 bara, preferably from 1 .3 to 3.5 bara, more preferably from 1.5 to 3 bara, and more preferably from 1 .7 to 2.5 bara.

[0291] 117. The integrated process according to any one of embodiments 113 to 116, wherein separation in (8) is achieved by distillation, preferably by fractionated distillation.

[0292] 118. The integrated process according to any one of embodiments 113 to 117, wherein after (7) and prior to the separation in (8), the stream S8 is cooled to a temperature in the range of from -60 to -29 °C, preferably from -55 to -31 °C, more preferably from -50 to -33 °C, and more preferably from -45 to -35 °C.

[0293] 119. The integrated process according to any one of embodiments 113 to 118, wherein (8) further comprises

[0294] (8.1) optionally separating at least part of the H2 from stream S9, obtaining a stream S12 containing H2;

[0295] (8.2) providing the stream S9 comprising methane and ethane to (5.1). 120. The integrated process according to any one of embodiments 113 to 119, wherein

[0296] (8) further comprises

[0297] (8.T) separating H2 from stream S9, obtaining a stream S13 containing H2 and a stream S14 comprising methane and ethane;

[0298] (8.2’) providing the stream S14 to (5.T).

[0299] 121 . The integrated process according to any one of embodiments 113 to 120, wherein at least part of the stream S2 obtained according to (4) or (4.4) is provided as fuel for the steam cracking according to (7).

[0300] 122. The integrated process according to embodiment 121 , wherein at least part of the CO2 added according to (5.T) comprises the CO2 obtained during the combustion of S2 as fuel for the steam cracking according to (7).

[0301] 123. The integrated process according to any one of embodiments 1 to 122, wherein

[0302] (5.2) comprises

[0303] (5.2a) mixing the stream S4 with a stream S10 comprising H2 and / or stream S12 obtained according to (8.1) and / or stream S13 obtained according to (8.T), obtaining a stream S11 ;

[0304] (5.2b) providing the stream S11 to (3) as a source of H2 for the H2-containing atmosphere in (3).

[0305] 124. The integrated process according to embodiment 123, wherein the stream S10 is provided from one or more of biogas reforming, water electrolysis, NH3 cracking, and methanol cracking.

[0306] The present invention is further illustrated by the following reference examples, examples and comparative examples.

[0307] EXAMPLES

[0308] Reference Example 1 : Preparation of the zeolite catalyst

[0309] Binder preparation:

[0310] 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.

[0311] Conversion of zeolite into H-form:

[0312] Table 1 : Overview of the zeolites as commercially obtained from Zeolyst.

[0313] 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.

[0314] Mixing zeolite and binder:

[0315] 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 1 h.

[0316] Freeze drying:

[0317] 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 mbar for 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).

[0318] Shaping:

[0319] 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.

[0320] 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.

[0321] Impregnation:

[0322] 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.

[0323] Calcination:

[0324] The dried sample was calcined in a 2-step calcination process under air in a muffle furnace:

[0325] 1) Decomposition of nitrates: 220 °C (heating rate 1 K / min, dwell time 3h, air flow 6 L / min)

[0326] 2) Final Calcination: 350°C (heating rate 1 K / min, dwell time 3h, air flow 6 L / min)

[0327] Table 2: Overview of prepared zeolite samples and their properties.

[0328] Reference Example 2: Gas Chromatography

[0329] Samples of the liquid product mixture from catalytic experiments were analysed by gas chroma- tography (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.

[0330] 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-Cn), mono- (iso-Cn) and multibranched (isoiso-Cn) 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.

[0331] Reference Example 3: Stoichiometric calculations for the hydrocracking of n-dodecane

[0332] The conversion Xn-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 (mout). Here, cracking products are all hydrocarbons that underwent at least one cracking reaction.

[0333] The equations used to calculate the conversion Xn-C12 of n-dodecane (1 ), the product yields Yen (2) and selectivity Scnfor the conversion products, with Cnresembling 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.

[0334] >mn-C12out An-C2—1. n-c12in

[0335] 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 ncnin the gaseous products for each gaseous hydrocracking product Cnwith the integrated peak are of the chromatogram Canof the product Cn, ACh4 of methan and the molar mass Men of the respective component results. The molar flow rates ncn,corr. For gaseous products corrected by the mass fraction of gaseous and liquid products were calculated with equation (7). The mass flow mijq.jnand the liquid products miiq-’Out

[0336] VcH / i^in ■ CH, 0.6 I min-1■ 5.03 Vol. —% . nCH„ = - ^77 - ~ = - - rn - = 1.347 - 103mo I min1CHiVm22.41 mol-1 me = nr- Mc

[0337] Without methane as internal standard the molar flow rates ncnfor gaseous products were calculated according to equation (8).

[0338] The molar flow rates for the liquid products were calculated using an external calibration of n- dodecane according to the subsequent equations. Here, Cnis the volume fraction of the hydrocracking product Cnin the liquid phase and pen is the density of the respective component.

[0339] Reference Example 4: Determination of the surface area

[0340] 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.

[0341] Reference Example 5: Determination of the Si / AI ratio

[0342] 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.

[0343] Example 16: Catalytic testing

[0344] The catalytic experiments were carried out in a continuous-flow apparatus with a tubular r 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 model hydrogenated vegetable oil (HVO). HVO feed was prepared by mixing 11 wt.% pentadecane, 36 wt.% hexadecane, 12 wt.% heptadecane and 40 wt.% octadecane. The 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 chromatog- raphy. 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).

[0345] Table 3: Overview of conversions and selectivities of tested zeolite samples.

[0346]

[0347] All investigated catalyst are active in the catalytic hydrocracking of the corresponding feed. Cracking products consists mainly of C3-C8 cracking products, while only traces of C1 and C2 if any, are formed. 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.

[0348] Description of the figures

[0349] Figure 1 is a schematic representation of a production unit used for the process according to an embodiment of the invention, wherein the feed (1) is fed into a first reactor (2) and wherein the stream S1 obtained in (2) is first fed into a vapor-liquid separator (3), and then into a distillation unit (4). The stream S2 obtained in (4) is fed into a pyrolysis reactor (5) and wherein the stream S4 is obtained, which is reintroduced as H2-source in (2).

[0350] Figure 2 is a schematic representation of a production unit used for the process according to an embodiment of the invention, wherein the feed (1) is fed into a first reactor (2) and wherein the stream S1 obtained in (2) is first fed into a vapor-liquid separator

[0351] (3), and then into a distillation unit (4). At least a part of the stream S2 obtained in

[0352] (4) is fed into a pyrolysis reactor (5), wherein the stream S4 is obtained, which is reintroduced as H2-source in (2). CO2 is added to at least a part of stream S2 obtained in (4) to obtain stream S5, which is fed into a third reactor (6), wherein the stream S6 is obtained. Figure 3 is a schematic representation of a production unit used for the process according to an embodiment of the invention, wherein the feed (1) is fed into a first reactor (2) and wherein the stream S1 obtained in (2) is first fed into a vapor-liquid separator

[0353] (3), and then into a distillation unit (4). At least a part of the stream S2 obtained in

[0354] (4) is fed into a pyrolysis reactor (5), wherein the stream S4 is obtained, which is reintroduced as H2-source in (2). CO2 is added to at least a part of stream S2 obtained in (4) to obtain stream S5, which is fed into a third reactor (6), wherein the stream S6 is obtained. Water is added to stream S3 obtained in (4) to obtain stream S7, which is fed into a steam cracker (7) to obtain stream S8. At least a part of the H2, methane and ethane are separated from the stream S8 in the distillation unit (8), obtaining a stream S9 which is further reacted in (5). H2 is removed from a part of the stream S9 obtaining a stream S14 which is further reacted in (6).

[0355] Reference numbers in the figures

[0356] (1 ) Feed

[0357] (2) First reactor comprising C1

[0358] (3) Vapor-liquid separator

[0359] (4) Distillation unit

[0360] (5) Pyrolysis reactor

[0361] (6) Third reactor comprising C2

[0362] (7) Steam cracker

[0363] (8) Distillation unit

[0364] Cited Literature

[0365] - WO 2019 / 229072 A1

[0366] - US 11 326 110 B2

[0367] - US 2016 / 289576 A1

[0368] - CN 113 913 210 A

Claims

Claims1 . An integrated process for the production of Ci to C12 alkanes, comprising(1 ) providing a feed F1 comprising one or more oxygen containing compounds comprising one or more Ce to C30 alkyl chains;(2) providing a catalyst C1 comprising one or more metals;(3) contacting the feed F1 provided in (1 ) with the catalyst C1 in an H2-containing atmosphere, obtaining a stream S1 comprising one or more compounds selected from the group consisting of Ci to C4 alkanes, and one or more compounds selected from the group consisting of C5 to C12 alkanes;(4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 alkanes, and at least part of the one or more compounds selected from the group consisting of C5 to C12 alkanes, from the stream S1 obtained in (3), obtaining a stream S2 comprising the one or more compounds selected from the group consisting of Ci to C4 alkanes and a stream S3 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes;(5.1 ) pyrolyzing at least part of the stream S2, obtaining a stream S4 comprising H2;(5.2) providing the stream S4 to (3) as a source of H2 for the H2-containing atmosphere in (3).

2. The integrated process according to claim 1 , wherein the one or more oxygen containing compounds comprised in the feed F1 in (1) are selected from the group consisting of vegetable oils, animal fats, and pyrolysis oils, and derivatives thereof including mixtures of two or more thereof.

3. The integrated process according to claim 1 or 2, wherein the one or more metals comprised in catalyst C1 are selected from the group consisting of Ni, Co, Pt, Pd, Rh, Mo, and W.

4. The integrated process according to any one of claims 1 to 3, wherein the catalyst C1 in (2) comprises a zeolitic material.

5. The integrated process according to any one of claims 1 to 4, wherein contacting in (3) is conducted at a temperature in the range of from 150 to 800 °C.

6. The integrated process according to any one of claims 1 to 5, wherein contacting in (3) is conducted at a pressure in the range of from 20 to 200 bara.

7. The integrated process according to any one of claims 1 to 6, wherein the temperature during pyrolysis in (5.1 ) is in the range of from 500 to 900 °C.

8. The integrated process according to any one of claims 1 to 7, wherein the pressure during pyrolysis in (5.1 ) is in the range of from 0.1 to 200 bar.

9. The integrated process according to any one of claims 1 to 8, wherein the integrated process further comprises(5.T) adding CO2 to part of the stream S2, obtaining a stream S5;(5.2’) providing a catalyst C2 comprising one or more of metals selected from the group consisting of Ni, Cr, Mo, Fe, Co, Cu, Pt, Pd, Rh, Ru, Os, Zr, Al, Si, Ti, Mg and Ir;(5.3’) contacting the stream S5 obtained according to (5.T) with the catalyst C2, obtaining a stream S6 comprising H2 and CO.

10. The integrated process according to claim 9, wherein at least part of the CO2 added according to (5.T) comprises CO2 from an industrial process.11 . The integrated process according to any one of claims 1 to 10, wherein the process further comprises(6) adding H2O to the stream S3 obtained in (4) or (4.4), obtaining a stream S7;(7) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S7, obtaining a stream S8 comprising H2, methane, ethane, olefins and aromatic hydrocarbons;(8) separating at least part of the H2, methane and ethane from the stream S8, obtaining a stream S9 comprising the separated H2, methane and ethane.

12. The integrated process according to claim 11 , wherein steam cracking in (7) is conducted at a temperature in the range of from 500 to 950 °C.

13. The integrated process according to any one of claims 11 or 12, wherein (8) further comprises(8.1) optionally separating at least part of the H2 from stream S9, obtaining a stream S12 containing H2;(8.2) providing the stream S9 comprising methane and ethane to (5.1).

14. The integrated process according to any one of claims 1 to 13, wherein (5.2) comprises (5.2a) mixing the stream S4 with a stream S10 comprising H2 and / or stream S12 obtained according to (8.1 ), obtaining a stream S11 ;(5.2b) providing the stream S11 to (3) as a source of H2 for the H2-containing atmosphere in (3).

15. The integrated process according to claim 14, wherein the stream S10 is provided from one or more of biogas reforming, water electrolysis, NH3 cracking, and methanol cracking.

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