An integrated process for the production of lpg, olefins, and aromatic hydrocarbons

Abstract

The present invention relates to an integrated process for the production of C1 to C4 alkanes, olefins, and aromatic hydrocarbons, comprising (1) preparing a feed F1 comprising one or more compounds selected from the group consisting of C6 to C30 alkanes and 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 from the stream S1 obtained in (3), obtaining a stream S2 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes; (5) adding H2O to the stream S2, obtaining a stream S3; (6) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S3 by heating the stream S3, obtaining a stream S4 comprising H2, methane, ethane, olefins, and aromatic hydrocarbons; (7) separating at least part of the H2, methane, and ethane from the stream S4, obtaining a stream S5 comprising the separated H2, methane, and ethane; (8) providing a catalyst C2 comprising one or more metals selected from the group consisting of Ni, Pt, Pd, Rh, Ru, Os, and Ir; (9) adding H2O to the stream S5, obtaining a stream S6; (10) contacting the stream S6 with the catalyst C2, obtaining a stream S7 comprising H2 and CO2; (11) separating at least part of the CO2 from the stream S7, obtaining a stream S8 comprising H2; (12) providing the stream S8 to (3) as a source of H2 for the H2-containing atmosphere in (3).

Description

[0001] An integrated process for the production of LPG, olefins, and aromatic hydrocarbons

[0002] TECHNICAL FIELD

[0003] The present invention relates to an integrated process for the production of Ci to C4 alkanes, olefins, and aromatic hydrocarbons, comprising a feed comprising one or more compounds selected from the group consisting of C@ to C30 alkanes and oxygen containing compounds comprising one or more C@ 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 0- 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 8692040 B2 relates to a process for treatment of a feedstock that is obtained from a renewable source that comprises a hydrotreatment in two stages in which said first stage of treatment that comprises a mild prehydrogenation operates at a temperature of between 50 and 300° C., at a partial hydrogen pressure of between 0.1 and 10 MPa, and at an hourly volumetric flow rate on the catalyst of between 0.1 h-1and 10 h-1,in which said prehydrogenation catalyst comprises at least one noble metal of group VIII that is selected from among palladium and platinum or comprises at least one non-noble metal of group VIII and / or at least one metal of group VIB, whereby the non-noble metal of group VIII is selected from among nickel and cobalt and the metal of group VIB is selected from among molybdenum and tungsten, whereby said prehydrogenation catalyst is a metal-phase catalyst, and in which said second treatment stage operates at a temperature of between 200 and 450° C., at a pressure of between 1 MPa and 10 MPa, at an hourly volumetric flow rate on the catalyst of between 0.1 tr1and 10 tr1, and at a total quantity of hydrogen that is mixed with the feedstock, such that the hydrogen to feedstock ratio is between 50 and 1 ,000 Nm3of hydrogen per m3of feedstock, in which said catalyst of the second treatment stage comprises at least one non-noble metal of group VIII and / or VIB, whereby the non-noble metal of group VIII is selected from among nickel and cobalt, and whereby the metal of group VIB is selected from among molybdenum and tungsten and is a sulfide-phase catalyst.

[0009] CN 112678771 A1 relates to an integration system comprising an SMR unit for methane steam reforming to generate a first synthesis gas and outputting high temperature steam; a methanol steam reforming unit used for reforming methanol steam to generate second synthesis gas; a PSA unit used for purifying the first synthesis gas and the second synthesis gas and outputting Fh; a first pipeline used for conveying the first synthesis gas to the PSA unit; a second pipeline used for conveying the high-temperature steam to the methanol steam reforming unit; and a third pipeline used for returning part of the high-temperature water vapor to the SMR unit.

[0010] US 2011 / 263916 A1 relates to a system to convert polyols into hydrocarbons comprising: a feed stream comprising a oxygenate feedstock, a catalytic upgrader comprising a zeolite catalyst, a separator to generate a light gas stream, an aqueous stream and an organic stream, a reformer to convert the light gas stream into a hydrogen stream, a hydrotreater to convert part of the organic stream and hydrogen stream into a saturated hydrocarbon stream, and a recycle system where a portion of the hydrotreater product containing saturated hydrocarbons is recycled to the catalytic upgrader as a hydrogen donor molecule.

[0011] US 2021 / 198584 A1 relates to a process for the production of bio-chemicals, from natural occurring oils containing acyl-containing compounds having 10 to 24 carbons including fatty acid esters and free fatty acids, and other components including impurities.

[0012] Despite the advances made in the hydrocracking of suitable feedstocks, there remains the need for energy- and cost-efficient hydrocracking processes.

[0013] DETAILED DESCRIPTION

[0014] 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.

[0015] Therefore, the present invention relates to an integrated process for the production of Ci to C4 alkanes, olefins, and aromatic hydrocarbons, comprising, preferably consisting of, (1 ) preparing a feed F1 comprising, preferably consisting of, one or more compounds selected from the group consisting of C@ to C30 alkanes and oxygen containing compounds comprising one or more C@ to C30 alkyl chains;

[0016] (2) providing a catalyst C1 , preferably a heterogeneous catalyst C1 , comprising one or more metals, preferably one or more transition metals;

[0017] (3) contacting the feed F1 provided in (1 ) with the catalyst C1 in an Fh-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;

[0018] (4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 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 C5 to C12 alkanes;

[0019] (5) adding H2O to the stream S2, obtaining a stream S3;

[0020] (6) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S3 by heating the stream S3, obtaining a stream S4 comprising H2, methane, ethane, olefins, and aromatic hydrocarbons;

[0021] (7) separating at least part of the H2, methane, and ethane from the stream S4, obtaining a stream S5 comprising, preferably consisting of, the separated H2, methane, and ethane;

[0022] (8) providing a catalyst C2 comprising one or more metals selected from the group consisting of Ni, Pt, Pd, Rh, Ru, Os, and Ir;

[0023] (9) adding H2O to the stream S5, obtaining a stream S6;

[0024] (10) contacting the stream S6 with the catalyst C2, obtaining a stream S7 comprising H2 and CO2;

[0025] (11) separating at least part of the CO2 from the stream S7, obtaining a stream S8 comprising, preferably consisting of, Fh;

[0026] (12) providing the stream S8 to (3) as a source of H2 for the Fh-containing atmosphere in (3).

[0027] It is preferred that (4) comprises, preferably consists of,

[0028] (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 Fh;

[0029] (4.2) providing the gaseous fraction GF1 to (3) as a source of H2 for the Fh-containing atmosphere in (3);

[0030] (4.3) 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 C5 to C12 alkanes.

[0031] In the case where (4) comprises steps (4.1 ) to (4.3), it is preferred that in (4.3) CO2 is separated in addition to the one or more compounds selected from the group consisting of Ci to C4 alkanes from the liquid fraction LF1 obtained in (4.1). In the case where (4) comprises steps (4.1 ) to (4.3), it is preferred that (4.3) 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 C@ to C30 alkyl chains 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 C5 to C12 alkanes.

[0032] In the case where (4) comprises steps (4.1) to (4.3), it is preferred that (4) further comprises (4.4) 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 C@ to C30 alkyl chains obtained in (4.3) to (1) as a source of one or more compounds selected from the group consisting of C13 to C30 alkanes and / or of one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains for preparing the feed F1 in (1).

[0033] 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, 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.

[0034] It is preferred that the catalyst C2 further comprises one or more promoter metals, wherein the one or more promoter metals are preferably selected from the group consisting of W, Fe, V, Na, Li, K, Ca, Sr, Ba, Mg, Al, B, and Ga, including combinations of two or more thereof, more preferably from the group consisting of W, Fe, and V, including combinations of two or more thereof, wherein more preferably the one or more promoter metals are Fe and / or V.

[0035] It is preferred that the catalyst C2 comprises one or more support materials, wherein the one or more metals and / or the one or more promoter metals, preferably the one or more metals and the one or more promoter metals are supported on the one or more support materials, wherein the one or more support materials are preferably selected from the group consisting of zirconia, alumina, silica, titanium oxide, silica-alumina, silicon carbide, magnesium aluminum spinel, and mixtures of two or more thereof, more preferably wherein the one or more support materials are selected from the group consisting of zirconia, alumina, silica, silica-alumina, silicon carbide, magnesium aluminum spinel, and mixtures of two or more thereof.

[0036] It is preferred that the catalyst C2 comprises Ni.

[0037] It is preferred that after (7) and prior to (10), preferably after (7) and prior to (9), the pressure of the stream S5 is increased, preferably by means of a compressor.

[0038] It is preferred that 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. It is preferred that 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.

[0039] 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, 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.

[0040] It is preferred that separation in (4) or (4.3) is achieved by distillation, preferably by fractionated distillation.

[0041] It is preferred that the stream S3 obtained in (5) 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.

[0042] It is preferred that steam cracking in (6) 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.

[0043] It is preferred that steam cracking in (6) 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.

[0044] It is preferred that separation in (7) is achieved by distillation, preferably by fractionated distillation.

[0045] It is preferred that after (6) and prior to the separation in (7), the stream S4 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.

[0046] It is preferred that the stream S6 obtained in (9) 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.

[0047] It is preferred that contacting in (10) is conducted at a temperature in the range of from 500 to 1 ,050 °C, preferably from 600 to 1 ,000 °C, more preferably from 650 to 980 °C, more preferably from 700 to 950 °C, more preferably from 750 to 920 °C, and more preferably from 800 to 900 °C.

[0048] It is preferred that contacting in (10) is conducted at a pressure in the range of from 5 to 50 bara, preferably from 10 to 40 bara, more preferably from 15 to 35 bara, and more preferably from 20 to 30 bara.

[0049] It is preferred that contacting in (10) is conducted at a gas hourly space velocity in the range of from 1 ,000 to 40,000 IT1, preferably 2,000 to 30,000 IT1, more preferably from 3,000 to 10.000 IT1. It is preferred that (1) comprises, preferably consists of,

[0050] (1) preparing a feed F1 comprising, preferably consisting of, one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains, preferably one or more C@ to C28 alkyl chains, more preferably one or more C@ to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains.

[0051] 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.

[0052] 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, 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.-%.

[0053] 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 F1 , preferably from 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%.

[0054] 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.

[0055] Yet further, it is preferred that the one or more oxygen containing compounds comprise, preferably consists of, waste materials, preferably of waste materials of biomaterials and / or plastics, more preferably waste materials selected from the group consisting of vegetable oils, animal fats, pyrolysis oils and derivatives thereof.

[0056] Sustainable cracking feedstocks

[0057] It is possible that a feedstock obtained from the recycling of mixed chemical waste is used as feed stock for the inventive hydrocracking process. The chemical recycling of mixed plastic waste leads to a recycled oil, generally referred to as pyrolysis oil. Major components of such mixed plastic waste may include, but are not limited to, polyethylenes, polypropylenes, polyethylene terephthalates, polystyrenes, copolymers of one or more of the foregoing, block polymers of one or more of the foregoing, graft copolymers of one or more of the foregoing, and mixtures of two or more of the foregoing. Prior to using a pyrolysis oil as feedstock for a cracker process, it may be necessary to subject it to a suitable purification including, but not being restricted to, catalytic methods and / or adsorption methods. It is also possible that bionaphtha is used as feedstock for the cracking process. Bionaphtha may be preferably produced from vegetable oils, preferably from waste food vegetable oil and / or non-food vegetable oil. Typically, it is obtained by transesterification of the vegetable oil by reaction of the oil with an alcohol, such as usually methanol, in the presence of a suitable catalyst. The reaction results in the formation of fatty acid methyl esters (FAMEs), which are the main component of bionaphtha. Vegetable oils which may be used include, but are not limited to, soybean oil, canola oil, sunflower oil, rapeseed oil, corn oil, palm oil, peanut oil, cottonseed oil, jatropha oil, algal oil.

[0058] Yet 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.

[0059] In the case where 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 vegetable oil is selected from the group consisting of palm oil, soybean oil, rapeseed oil, sunflower oil, linseed oil, rice bran oil, maize oil, olive oil, castor oil, sesame oil, pine oil, peanut oil, mustard oil, palm kernel oil, hempseed oil, coconut oil, babassu oil, cottonseed oil, jatropha oil, used cooking oils, oils derived from algae, corn oil, safflower oil, sunflower oil, almond oil, beech nut oil, brazil nut oil, cashew oil, hazelnut oil, macadamia oil, mongongo nut oil, pecan oil, pistachio oil, walnut oil, pumpkin seed oil, amaranth oil, argan oil, ben oil, date seed oil, dika oil, false flax oil, grape seed oil, hemp oil, kapok seed oil, kenaf seed oil, marula oil, meadowfoam seed oil, okra seed oil, perilla seed oil, persimmon seed oil, pequi oil, pili nut oil, poppyseed oil, pracaxi oil, quinoa oil, colza oil, radish oil, safflower oil, tigernut oil, tung oil and mixtures of two or more thereof.

[0060] In the case where 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 fat is selected from the group consisting of tallow, lard, grease, fish oil, butterfat, milk fat, and mixtures of two or more thereof.

[0061] It is preferred that the feed F 1 in (1 ) comprises 50 wt.-% or more of fatty acid esters and / or free fatty acids, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more of fatty acid esters and / or free fatty acids.

[0062] In the case where 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, preferably hydrogenated.

[0063] In the case where 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, preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

[0064] In the case where the feed F1 in (1) comprises, preferably consists of, pyrolysis oil of biogenic nature, it is preferred that the pyrolysis oil of biogenic nature is selected from the group consisting of wood, straw, scrap wood, and mixtures of two or more thereof.

[0065] In the case where 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, preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms.

[0066] In the case where the feed F1 in (1 ) comprises, preferably consists of, pyrolysis oil, it is preferred that the feed F1 in (1 ) comprises 50 wt.-% or more of pyrolysis oil, preferably 60 wt.-% or more, more preferably 70 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more, more preferably 95 wt.-% or more of pyrolysis oil.

[0067] It is preferred that the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the ze- olitic material is loaded with the one or more metals.

[0068] In the case where 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, 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.

[0069] In the case where the catalyst C1 in (2) comprises a zeolitic material, 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, preferably zeolite beta. In the case where the zeolitic material in (2) has a BEA type framework structure, it is preferred that the SIC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 35, more preferably from 20 to 30.

[0070] As a first alternative, in the case where the catalyst C1 in (2) comprises a zeolitic material, 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 , preferably mordenite.

[0071] In the case where the zeolitic material in (2) has a MOR type framework structure, it is preferred that the SiO2:AhO3 molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 30, more preferably from 15 to 25.

[0072] As a second alternative, in the case where the catalyst C1 in (2) comprises a zeolitic material, it is preferred that 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, [Al- Ge-O]-FAU, zeolite X, zeolite Y, Na-X, ZSM-3, CSZ-1 , CSZ-3, zeolite Y dealuminated, SAPO- 37, US-Y, LZ-210, ECR-30, ZSM-20, Na-Y, [Ga-AI-Si-O]-FAU, [Ga-Si-O]-FAU and Li-LSX, preferably US-Y.

[0073] In the case where the zeolitic material in (2) has a FAU type framework structure, it is preferred that the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

[0074] As a third alternative, in the case where the catalyst C1 in (2) comprises a zeolitic material, 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, 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, En- cilite, NU-4, TSZ-III, ZBH, [Fe-Si-O]-M Fl , H-ZSM-5, [Ga-Si-O]-MFI, [As-Si-O]-MFI, Mutinaite, MnS-1 , FeS-1 and ZSM-5 dealuminated, preferably ZSM-5.

[0075] In the case where the zeolitic material in (2) has a MFI type framework structure, it is preferred that the SiC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 60, more preferably from 5 to 50, more preferably from 20 to 40, more preferably from 25 to 35.

[0076] 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, preferably one or more unbranched alkanes. In the case where 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 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.

[0077] Yet 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, preferably from 1 :2 to 1 :4.5, more preferably from 1 :3 to 1 :4.

[0078] Alternatively, in the case where 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 , preferably from 1.5:1 to 3.5:1 , more preferably from 2:1 to 3:1.

[0079] Yet further, it is preferred that 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.

[0080] In the case where the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the ze- olitic material is loaded with the one or more metals, it is preferred that the one or more metals loaded on the zeolitic material in (2) are selected from the group consisting of Li, Na, K, Cs, Mg, Ca, Sr, Ba, La, Ce, Y, V, Mo, W, Nb, Sn, P, Sb, S, Se, Fe, Ni, Co, Pt, Pd, Rh and mixtures thereof, preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof.

[0081] Alternatively, in the case where the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the zeolitic material is loaded with the one or more metals, it is preferred that the one or more metals loaded on the zeolitic material in (2) are group 9 to 11 metals, preferably group 10 metals, more preferably selected from the group consisting of Fe, Ni, Co, Pt, Pd, Rh, and mixtures thereof, more preferably Ni, Pt, and mixtures thereof, more preferably Ni or Pt.

[0082] In the case where the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the zeolitic material is loaded with the one or more metals, it is preferred that the catalyst in (2) contains Pt, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Pt, wherein more preferably the zeolitic material has a Pt content in the range of from 0.001 to 5 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.01 to 2 wt.-%, more preferably from 0.1 to 1 .5 wt.-%, more preferably from 0.5 to 1 .3 wt.-%, more preferably from 0.8 to 1 .2 wt.-%, more preferably from 0.9 to 1 .1 wt.-%. In the case where the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the ze- olitic material is loaded with the one or more metals, it is preferred that the catalyst in (2) contains Ni, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Ni, wherein more preferably the zeolitic material has a Ni content in the range of from 0.01 to 10 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.1 to 9 wt.-%, more preferably from 1 to 8 wt.-%, more preferably from 2 to 7 wt.-%, more preferably from 3 to 6 wt.-%, more preferably from 4 to 5.5 wt.-%.

[0083] In the case where the catalyst C1 in (2) comprises a zeolitic material, 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.

[0084] In the case where the zeolitic material in (2) comprises YO2 and X2O3 in its framework structure, it is preferred that X is selected from the group consisting of Al, B, Ga and combinations thereof, wherein X is preferably Al.

[0085] Yet further, it is preferred that Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is preferably Si.

[0086] In the case where 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, 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.

[0087] It is preferred that the heterogeneous catalyst in (2) further comprises a binder, wherein the binder preferably comprises, more preferably consists of, one or more selected from the group consisting of titania, zirconia, alumina, silica, silica-alumina, titania-silica, titania-alumina, zirco- nia-silica, zirconia-alumina, and titania-zirconia, more preferably from the group consisting of silica-alumina, titania-silica, titania-alumina, zirconia-silica, zirconia-alumina, and titania-zirconia, wherein more preferably the binder comprises, more preferably consists of, silica, alumina or mixtures thereof.

[0088] It is preferred that the heterogeneous catalyst in (2) is provided as a shaped body, preferably as an extrudate.

[0089] Alternatively, it is preferred that the heterogeneous catalyst in (2) is provided as a shaped body, preferably a 3D printed structure.

[0090] In case where the heterogeneous catalyst in (2) is provided as a shaped body, it is preferred that the heterogeneous catalyst has a cross-sectional profile, wherein the cross-sectional profile is circular, hexagonal, rectangular, quadratic, triangular, oval, a star-shaped polygon having 3, 4, 5, 6, 7, or 8 tips, a trilobe or a quadrilobe, preferably a trilobe or a quadrilobe. In the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that from 95 to 100 wt.-% of the heterogeneous catalyst provided in (2) consists of the 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.

[0091] Yet further, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the binder content of the heterogeneous catalyst in (2) ranges of from 10 to 90 wt.-%, preferably from 14 to 80 wt.-%, more preferably from 16 to 70 wt.-%, more preferably from 18 to 60 wt.-%, more preferably from 20 to 50 wt.-%.

[0092] Yet further, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the preparation of the heterogeneous catalyst according to (2) comprises, (2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture Ma;

[0093] (2.b) extruding the mixture Maobtained according to (2a);

[0094] (2.c) optionally drying the extrudate obtained according to (2.b);

[0095] (2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

[0096] (2.3) optionally reducing the extrudate obtained according to (2.b), (2.c) or (2.d);

[0097] (2.f) optionally passivating the extrudate obtained according to (2.b), (2.c), (2.d) or (2.e).

[0098] Alternatively, in the case where the heterogeneous catalyst in (2) further comprises a binder, it is preferred that the preparation of the heterogeneous catalyst C1 according to (2) comprises, (2. a’) mixing a binder and a zeolitic material, obtaining a mixture Ma;

[0099] (2.b’) extruding the mixture Maobtained according to (2. a’);

[0100] (2.c’) optionally drying the extrudate obtained according to (2.b’);

[0101] (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;

[0102] (2.e’) optionally drying the impregnated extrudate obtained according to (2.d’);

[0103] (2.f) optionally calcining the impregnated extrudate obtained according to (2.d’), preferably obtained according to (2.e’);

[0104] (2.g’) optionally reducing the impregnated extrudate obtained according to (2.d’), preferably according to (2.e’), more preferably according to (2.f);

[0105] (2.h’) optionally passivating the extrudate obtained according to (2.d’), (2.e’), (2.f) or (2.g’).

[0106] In the case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that the binder is a colloid or a colloidal dispersion.

[0107] In the case where (2) comprises steps (2. a) to (2.f), it is preferred that prior to (2. a) the binder is subject to a peptization step. In the case where the binder is a colloid or a colloid dispersion, it is preferred that the solid content of the colloidal dispersion is in the range of from 1 to 40 wt.-%, based on 100 wt.-% of the colloidal dispersion, preferably in the range of from 5 to 30 wt.-%, more preferably in the range of from 10 to 20 wt.-%.

[0108] In the case where the catalyst C1 in (2) comprises a zeolitic material, it is preferred that 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.-%.

[0109] 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 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.

[0110] It is preferred that contacting in (3) is conducted in a fixed bed reactor or a fluidized bed reactor, preferably in a fixed bed reactor.

[0111] It is preferred that the Fh-containing atmosphere in (3) consists of hydrogen.

[0112] In the case where the Fh-containing atmosphere in (3) consists of hydrogen, it is preferred that in (3) the Fh-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.

[0113] It is preferred that 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.

[0114] It is preferred that 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.

[0115] 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, 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.

[0116] It is preferred that the feed F1 in (1) is a feed stream and contacting in (3) is conducted as a continuous process. It is preferred that the feed F1 provided in (1) and contacted with the catalyst C1 (3) is in the liquid phase and / or the gas phase, preferably in the gas phase.

[0117] It is preferred that 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.

[0118] It is preferred that 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.

[0119] It is preferred that 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.

[0120] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is conducted at a temperature in the range of from 50 to 300 °C, preferably from 100 to 200 °C, more preferably from 120 to 180 °C, more preferably from 130 to 170 °C, more preferably from 140 to 160 °C.

[0121] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.c) or (2.e’) preferably comprises an inert gas, preferably nitrogen and / or argon, more preferably comprises nitrogen.

[0122] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other drying in (2.c) or (2.e’) is conducted for a period ranging from 6 to 48 h, preferably from 12 to 36 h, more preferably from 20 to 28 h.

[0123] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is conducted at a temperature in the range of from 100 to 500 °C, preferably from 200 to 400 °C, more preferably from 240 to 360 °C, more preferably from 260 to 340 °C, more preferably from 280 to 320 °C.

[0124] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is performed under a gas atmosphere, wherein the gas atmosphere in (2.e) or (2.g’) preferably comprises a reducing gas, more preferably comprises hydrogen.

[0125] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other reducing in (2.e) or (2.g’) is conducted for a period ranging from 6 to 36 h, preferably from 8 to 24 h, more preferably from 10 to 14 h.

[0126] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other passivating in (2.f) or (2.h’) is conducted at a temperature in the range of from 50 to 200 °C, preferably from 60 to 150 °C, more preferably from 70 to 100 °C.

[0127] In case where (2) comprises steps (2. a) to (2.f) or (2. a’) to (2.h’), it is preferred that independently from each other passivating in (2.f) or (2.h’) us conducted for a period ranging from 1 to 36 h, preferably from 3 to 28 h, more preferably from 6 to 20 h.

[0128] It is preferred that 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.

[0129] It is preferred that contacting in (3) is conducted in a trickle-bed reactor or an ebullated bed reactor, preferably a plug-flow trickle-bed reactor.

[0130] In the case where contacting in (3) is conducted in a trickle-bed reactor, it is preferred that the trickle-bed reactor comprises a structured catalyst bed which comprises stacked layers of the catalyst according to (2).

[0131] In the case where the trickle-bed reactor comprises a structured catalyst bed, it is preferred that the number of stacked layers is in the range of from 2 to 30, preferably from 3 to 20, more preferably from 4 to 10.

[0132] In the case where contacting in (3) is conducted in a trickle-bed reactor, it is preferred that the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers. Within the meaning of the present invention, the term “positive binder gradient" refers to a binder content change from a lower binder content of a first layer to a higher binder content of a second layer, wherein the second layer is located at a higher position in the stacked layers of the catalyst than the first layer.

[0133] In the case where 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 tricklebed reactor, wherein each upper layer has a slightly higher binder content than the adjacent lower layer. Alternatively, in the case where the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers, it is preferred that binder gradient is the binder gradient is non- uniform, wherein the binder content of an upper layer is higher than the binder content of a lower layer.

[0134] It is preferred that 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.

[0135] It is preferred that the feed F1 according to (1 ) is a merged feed of two or more sub-feeds, wherein at least one of the two or more sub-feeds comprises one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more CG to C30 alkyl chains, preferably one or more CG to C28 alkyl chains, more preferably one or more CG to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains.

[0136] In the case where the feed F1 according to (1) is a merged feed of two or more sub-feeds, it is preferred that at least one of the two or more sub-feeds comprises one or more compounds selected from the group consisting of CG to C30 alkanes, preferably CG to C28 alkanes, more preferably CG to C22 alkanes, and more preferably Cs to C20 alkanes.

[0137] Yet further, in the case where the feed F1 according to (1) is a merged feed of two or more subfeeds, it is preferred that at least one of the two or more sub-feeds is substantially free of oxygen containing compounds, preferably wherein, independently from one another, at least one of the two or more sub-feeds contains 1 wt.-% or less of oxygen containing compounds, more preferably 0.1 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.001 wt.-% or less, based on the total weight of the respective sub-feed.

[0138] It is preferred that (1 ) comprises, preferably consists of,

[0139] (1 ) preparing a feed comprising, preferably consisting of, one or more compounds selected from the group consisting of CG to C30 alkanes, preferably CG to C28 alkanes, more preferably CG to C22 alkanes, and more preferably Cs to C20 alkanes.

[0140] It is preferred that after (4) and prior to (5) the one or more compounds selected from the group consisting of Ci to C4 alkanes obtained from separation in (4) is added to the stream S2.

[0141] 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 integrated process of any 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.

[0142] 1 . An integrated process for the production of Ci to C4 alkanes, olefins, and aromatic hydrocarbons, comprising, preferably consisting of,

[0143] (1 ) preparing a feed F1 comprising, preferably consisting of, one or more compounds selected from the group consisting of C@ to C30 alkanes and oxygen containing compounds comprising one or more C@ to C30 alkyl chains;

[0144] (2) providing a catalyst C1 , preferably a heterogeneous catalyst C1 , comprising one or more metals, preferably one or more transition metals;

[0145] (3) contacting the feed F1 provided in (1 ) with the catalyst C1 in an Fh-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;

[0146] (4) separating at least part of the one or more compounds selected from the group consisting of Ci to C4 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 C5 to C12 alkanes;

[0147] (5) adding H2O to the stream S2, obtaining a stream S3;

[0148] (6) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S3 by heating the stream S3, obtaining a stream S4 comprising H2, methane, ethane, olefins, and aromatic hydrocarbons;

[0149] (7) separating at least part of the H2, methane, and ethane from the stream S4, obtaining a stream S5 comprising, preferably consisting of, the separated H2, methane, and ethane;

[0150] (8) providing a catalyst C2 comprising one or more metals selected from the group consisting of Ni, Pt, Pd, Rh, Ru, Os, and Ir;

[0151] (9) adding H2O to the stream S5, obtaining a stream S6;

[0152] (10) contacting the stream S6 with the catalyst C2, obtaining a stream S7 comprising H2 and CO2;

[0153] (11 Separating at least part of the CO2 from the stream S7, obtaining a stream S8 comprising, preferably consisting of, Fh;

[0154] (12) providing the stream S8 to (3) as a source of H2 for the Fh-containing atmosphere in (3).

[0155] 2. The integrated process of embodiment 1 , wherein (4) comprises, preferably consists of,

[0156] (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 Fh;

[0157] (4.2) providing the gaseous fraction GF1 to (3) as a source of H2 for the Fh-contain- ing atmosphere in (3); (4.3) 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 C5 to C12 alkanes.

[0158] 3. The integrated process of embodiment 2, wherein in (4.3) CO2 is separated in addition to the one or more compounds selected from the group consisting of Ci to C4 alkanes from the liquid fraction LF1 obtained in (4.1 ).

[0159] 4. The integrated process of embodiment 2 or 3, wherein (4.3) 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 C@ to C30 alkyl chains 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 C5 to C12 alkanes.

[0160] 5. The integrated process of any of embodiments 2 to 4, wherein (4) further comprises

[0161] (4.4) 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 C@ to C30 alkyl chains obtained in (4.3) to (1) as a source of one or more compounds selected from the group consisting of C13 to C30 alkanes and / or of one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains for preparing the feed F1 in (1).

[0162] 6. The integrated process of any of embodiments 1 to 5, 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.

[0163] 7. The integrated process of any of embodiments 1 to 6, wherein the catalyst C2 further comprises one or more promoter metals, wherein the one or more promoter metals are preferably selected from the group consisting of W, Fe, V, Na, Li, K, Ca, Sr, Ba, Mg, Al, B, and Ga, including combinations of two or more thereof, more preferably from the group consisting of W, Fe, and V, including combinations of two or more thereof, wherein more preferably the one or more promoter metals are Fe and / or V.

[0164] 8. The integrated process of any of embodiments 1 to 7, wherein the catalyst C2 comprises one or more support materials, wherein the one or more metals and / or the one or more promoter metals, preferably the one or more metals and the one or more promoter metals are supported on the one or more support materials, wherein the one or more support materials are preferably selected from the group consisting of zirconia, alumina, sil- ica, titanium oxide, silica-alumina, silicon carbide, magnesium aluminum spinel, and mixtures of two or more thereof, more preferably wherein the one or more support materials are selected from the group consisting of zirconia, alumina, silica, silica-alumina, silicon carbide, magnesium aluminum spinel, and mixtures of two or more thereof.

[0165] 9. The integrated process of any of embodiments 1 to 8, wherein the catalyst C2 comprises Ni.

[0166] 10. The integrated process of any of embodiments 1 to 9, wherein after (7) and prior to (10), preferably after (7) and prior to (9), the pressure of the stream S5 is increased, preferably by means of a compressor.

[0167] 11 . The integrated process of any of embodiments 1 to 10, 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.

[0168] 12. The integrated process of any of embodiments 1 to 11 , 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.

[0169] 13. The integrated process of any of embodiments 1 to 12, 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.

[0170] 14. The integrated process of any of embodiments 1 to 13, wherein separation in (4) or (4.3) is achieved by distillation, preferably by fractionated distillation.

[0171] 15. The integrated process of any of embodiments 1 to 14, wherein the stream S3 obtained in (5) 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.

[0172] 16. The integrated process of any of embodiments 1 to 15, wherein steam cracking in (6) 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.

[0173] 17. The integrated process of any of embodiments 1 to 16, wherein steam cracking in (6) 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. 18. The integrated process of any of embodiments 1 to 17, wherein separation in (7) is achieved by distillation, preferably by fractionated distillation.

[0174] 19. The integrated process of any of embodiments 1 to 18, wherein after (6) and prior to the separation in (7), the stream S4 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.

[0175] 20. The integrated process of any of embodiments 1 to 19, wherein the stream S6 obtained in (9) 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.

[0176] 21 . The integrated process of any of embodiments 1 to 20, wherein contacting in (10) is conducted at a temperature in the range of from 500 to 1 ,050 °C, preferably from 600 to

[0177] 1 ,000 °C, more preferably from 650 to 980 °C, more preferably from 700 to 950 °C, more preferably from 750 to 920 °C, and more preferably from 800 to 900 °C.

[0178] 22. The integrated process of any of embodiments 1 to 21 , wherein contacting in (10) is conducted at a pressure in the range of from 5 to 50 bara, preferably from 10 to 40 bara, more preferably from 15 to 35 bara, and more preferably from 20 to 30 bara.

[0179] 23. The integrated process of any of embodiments 1 to 22, wherein contacting in (10) is conducted at a gas hourly space velocity in the range of from 1 ,000 to 40,000 IT1, preferably 2,000 to 30,000 IT1, more preferably from 3,000 to 10.000 IT1.

[0180] 24. The integrated process of any of embodiments 1 to 23, wherein (1) comprises, preferably consists of,

[0181] (1 ) preparing a feed F1 comprising, preferably consisting of, one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains, preferably one or more C@ to C28 alkyl chains, more preferably one or more C@ to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains.

[0182] 25. The process according to any one of embodiments 1 to 24, 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.

[0183] 26. The process according to any one of embodiments 1 to 25, 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.-%.

[0184] 27. The process according to any of embodiments 1 to 26, 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

[0185] 10 to 90 wt.-%, more preferably from 20 to 80 wt.-%.

[0186] 28. The process according to any of embodiments 1 to 27, 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.

[0187] 29. The process according to embodiment 28, 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.

[0188] 30. The process according to embodiment 28 or 29, 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.

[0189] 31 . The process according to any of embodiments 28 to 30, wherein the vegetable oil is selected from the group consisting of palm oil, soybean oil, rapeseed oil, sunflower oil, linseed oil, rice bran oil, maize oil, olive oil, castor oil, sesame oil, pine oil, peanut oil, mustard oil, palm kernel oil, hempseed oil, coconut oil, babassu oil, cottonseed oil, jatropha oil, used cooking oils, oils derived from algae, corn oil, safflower oil, sunflower oil, almond oil, beech nut oil, brazil nut oil, cashew oil, hazelnut oil, macadamia oil, mongongo nut oil, pecan oil, pistachio oil, walnut oil, pumpkin seed oil, amaranth oil, argan oil, ben oil, date seed oil, dika oil, false flax oil, grape seed oil, hemp oil, kapok seed oil, kenaf seed oil, marula oil, meadowfoam seed oil, okra seed oil, peri Ila 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.

[0190] 32. The process according to any of embodiments 28 to 31 , 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.

[0191] 33. The process according to any of embodiments 1 to 32, 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.

[0192] 34. The process according to embodiments 28 to 33, wherein the animal fats and vegetable oils are at least partially hydrogenated, preferably hydrogenated.

[0193] 35. The process according to embodiment 28, wherein the feed F1 in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil of biogenic nature.

[0194] 36. The process according to embodiment 35, 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.

[0195] 37. The process according to any of embodiments 28 to 36, wherein the feed F1 in (1) comprises, preferably consists of, pyrolysis oil, preferably pyrolysis oil from plastic waste forms.

[0196] 38. The process according to any of embodiments 35 to 37, 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.

[0197] 39. The process according to any of embodiments 1 to 38, wherein the catalyst C1 in (2) comprises a zeolitic material, wherein preferably the zeolitic material is loaded with the one or more metals.

[0198] 40. The process according to embodiment 39, 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. 41 . The process according to embodiment 39 or 40, 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.

[0199] 42. The process according to embodiment 41 , wherein the SIC^AhOs molar ratio of the zeolitic material is in the range of from 1 to 70, preferably from 2 to 50, more preferably from 5 to 40, more preferably from 10 to 35, more preferably from 20 to 30.

[0200] 43. The process according to embodiment 39 or 40, 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 sili- cious, LZ-211 , [Ga-Si-O]-MOR, Maricopaite and RMA-1 , preferably mordenite.

[0201] 44. The process according to embodiment 43, 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.

[0202] 45. The process according to embodiment 39 or 40, 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.

[0203] 46. The process according to embodiment 45, 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.

[0204] 47. The process according to embodiment 39 or 40, 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.

[0205] 48. The process according to embodiment 47, 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. 49. The process according to any of embodiments 1 to 48, 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.

[0206] 50. The process according to embodiment 49, 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.

[0207] 51 . The process according to embodiment 49 or 50, 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.

[0208] 52. The process according to embodiment 49, 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 .

[0209] 53. The process according to embodiment 49 or 52, 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 .

[0210] 54. The process according to any of embodiments 39 to 53, 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.

[0211] 55. The process according to any of embodiments 39 to 53, 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.

[0212] 56. The process according to any of embodiments 39 to 55, wherein the catalyst in (2) contains Pt, wherein preferably the zeolitic material comprised in the heterogeneous catalyst in (2) is loaded with Pt, wherein more preferably the zeolitic material has a Pt content in the range of from 0.001 to 5 wt.-%, based on 100 wt.% of the metal loaded zeolitic material, preferably from 0.01 to 2 wt.-%, more preferably from 0.1 to 1.5 wt.-%, more preferably from 0.5 to 1 .3 wt.-%, more preferably from 0.8 to 1 .2 wt.-%, more preferably from 0.9 to 1.1 wt.-%. 57. The process according to any of embodiments 39 to 56, wherein the catalyst in (2) contains N i , 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.- 0 / / o.

[0213] 58. The process according to any of embodiments 39 to 57, 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.

[0214] 59. The process according to embodiment 58, wherein X is selected from the group consisting of Al, B, Ga and combinations thereof, wherein X is preferably Al.

[0215] 60. The process according to embodiment 58 or 59, wherein Y is selected from the group consisting of Si, Ti, Sn, Ge and combinations thereof, wherein Y is preferably Si.

[0216] 61 . The process according to any of embodiments 39 to 60, 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.

[0217] 62. The process according to any of embodiments 1 to 61 , 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.

[0218] 63. The process according to any of embodiments 1 to 62, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably as an extrudate.

[0219] 64. The process according to any of embodiments 1 to 62, wherein the heterogeneous catalyst in (2) is provided as a shaped body, preferably a 3D printed structure. 65. The process according to embodiment 63 or 64, 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.

[0220] 66. The process according to any of embodiments 62 to 65, 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.

[0221] 67. The process according to any of embodiments 62 to 66, 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.-%.

[0222] 68. The process according to any of embodiments 62 to 67, wherein the preparation of the heterogeneous catalyst according to (2) comprises,

[0223] (2. a) mixing a binder and a zeolitic material comprising one or more metals, obtaining a mixture Ma;

[0224] (2.b) extruding the mixture Maobtained according to (2a);

[0225] (2.c) optionally drying the extrudate obtained according to (2.b);

[0226] (2.d) optionally calcining the extrudate obtained according to (2.b) or (2.c);

[0227] (2.3) optionally reducing the extrudate obtained according to (2.b), (2.c) or (2.d);

[0228] (2.f) optionally passivating the extrudate obtained according to (2.b), (2.c), (2.d) or (2.e).

[0229] 69. The process according to any of embodiments 62 to 67, wherein the preparation of the heterogeneous catalyst C1 according to (2) comprises,

[0230] (2. a’) mixing a binder and a zeolitic material, obtaining a mixture Ma;

[0231] (2.b’) extruding the mixture Maobtained according to (2. a’);

[0232] (2.c’) optionally drying the extrudate obtained according to (2.b’);

[0233] (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;

[0234] (2.e’) optionally drying the impregnated extrudate obtained according to (2.d’);

[0235] (2.f) optionally calcining the impregnated extrudate obtained according to (2.d’), preferably obtained according to (2.e’);

[0236] (2.g’) optionally reducing the impregnated extrudate obtained according to (2.d’), preferably according to (2.e’), more preferably according to (2.f);

[0237] (2.h’) optionally passivating the extrudate obtained according to (2.d’), (2.e’), (2.f) or (2.g’). The process according to embodiment 68 or 69, wherein the binder is a colloid or a colloidal dispersion. The process according to embodiment 68 or 70, wherein prior to (2. a) the binder is subject to a peptization step. The process according to embodiment 70, 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.-%. The process according to any of embodiments 39 to 72, wherein the zeolitic material content of the heterogeneous catalyst in (2) ranges of from 20 to 90 wt.-%, preferably from 30 to 86 wt.-%, more preferably from 40 to 84 wt.-%, more preferably from 50 to 82 wt.-%, more preferably from 60 to 80 wt.-%. The process according to any of embodiments 1 to 73, 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. The process according to any of embodiments 1 to 74, wherein contacting in (3) is conducted in a fixed bed reactor or a fluidized bed reactor, preferably in a fixed bed reactor. The process according to any of embodiments 1 to 75, wherein the Fh-containing atmosphere in (3) consists of hydrogen. The process according to embodiment 76, wherein in (3) the Fh-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. The process according to any of embodiments 1 to 77, 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. The process according to any of embodiments 1 to 78, 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.

[0238] 80. The process according to any of embodiments 1 to 79, 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.

[0239] 81 . The process according to any of embodiments 1 to 80, wherein the feed F1 in (1) is a feed stream and contacting in (3) is conducted as a continuous process.

[0240] 82. The process according to any of embodiments 1 to 81 , wherein the feed F1 provided in (1 ) and contacted with the catalyst C1 (3) is in the liquid phase and / or the gas phase, preferably in the gas phase.

[0241] 83. The process according to any of embodiments 1 to 82, 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.

[0242] 84. The process according to any of embodiments 1 to 83, 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.

[0243] 85. The process according to any of embodiments 1 to 83, 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.

[0244] 86. The process according to any of embodiments 68 to 85, 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. 87. The process according to any of embodiments 68 to 86, 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.

[0245] 88. The process according to any of embodiments 68 to 87, 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.

[0246] 89. The process according to any of embodiments 68 to 88, 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.

[0247] 90. The process according to any of embodiments 68 to 89, 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.

[0248] 91 . The process according to any of embodiments 68 to 90, 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.

[0249] 92. The process according to any of embodiments 68 to 91 , 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.

[0250] 93. The process according to any of embodiments 68 to 92, 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.

[0251] 94. The process according to any of embodiments 1 to 93, 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] 95. The process according to any of embodiments 1 to 94, wherein contacting in (3) is conducted in a trickle-bed reactor or an ebullated bed reactor, preferably a plug-flow tricklebed reactor.

[0253] 96. The process according to embodiment 95, wherein trickle-bed reactor comprises a structured catalyst bed which comprises stacked layers of the catalyst according to (2). 97. The process according to embodiment 96, 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.

[0254] 98. The process according to any of embodiments 95 to 97, wherein the trickle-bed reactor is operated over a positive binder gradient from lower to upper layers.

[0255] 99. The process according to embodiment 98, 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.

[0256] 100. The process according to embodiment 99, 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.

[0257] 101. The process according to any of embodiments 1 to 100, 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.

[0258] 102. The process according to any of embodiments 1 to 101 , wherein the feed F1 according to (1 ) is a merged feed of two or more sub-feeds, wherein at least one of the two or more sub-feeds comprises one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains, preferably one or more C@ to C28 alkyl chains, more preferably one or more C@ to C22 alkyl chains, and more preferably one or more Cs to C20 alkyl chains.

[0259] 103. The process according to embodiment 102, wherein at least one of the two or more subfeeds comprises one or more compounds selected from the group consisting of C@ to C30 alkanes, preferably C@ to C28 alkanes, more preferably C@ to C22 alkanes, and more preferably Cs to C20 alkanes.

[0260] 104. The process according to embodiment 102 or 103, wherein at least one of the two or more sub-feeds is substantially free of oxygen containing compounds, preferably wherein, independently from one another, at least one of the two or more sub-feeds contains 1 wt.-% or less of oxygen containing compounds, more preferably 0.1 wt.-% or less, more preferably 0.01 wt.-% or less, more preferably 0.001 wt.-% or less, based on the total weight of the respective sub-feed.

[0261] 105. The integrated process of any of embodiments 1 to 23, wherein (1 ) comprises, preferably consists of,

[0262] (1 ) preparing a feed comprising, preferably consisting of, one or more compounds selected from the group consisting of C@ to C30 alkanes, preferably C@ to C28 alkanes, more preferably C@ to C22 alkanes, and more preferably Cs to C20 alkanes. 106. The integrated process of any of embodiments 1 to 105, wherein after (4) and prior to (5) the one or more compounds selected from the group consisting of Ci to C4 alkanes obtained from separation in (4) is added to the stream S2.

[0263] The present invention is further illustrated by the following reference examples, examples and comparative examples.

[0264] EXAMPLES

[0265] Reference Example 1 : Preparation of the zeolite catalyst

[0266] Binder preparation:

[0267] 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.

[0268] Conversion of zeolite into H-form:

[0269] Table 1 : Overview of the zeolites as commercially obtained from Zeolyst.

[0270] 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.

[0271] Mixing zeolite and binder:

[0272] 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.

[0273] Freeze drying: The mixture was transferred into liquid nitrogen to shock freeze it. The now solid mixture was transferred into a precooled freeze dryer (-30 °C) and freeze dried for 7-10 days at -10 °C at 2.56 mbar. The resulting solid was dried at 20 °C and 2.56 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).

[0274] Shaping:

[0275] 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.

[0276] 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.

[0277] Impregnation:

[0278] 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.

[0279] Calcination:

[0280] The dried sample was calcined in a 2-step calcination process under air in a muffle furnace:

[0281] 1 ) Decomposition of nitrates: 220 °C (heating rate 1 K / min, dwell time 3h, air flow 6 L / min)

[0282] 2) Final Calcination: 350°C (heating rate 1 K / min, dwell time 3h, air flow 6 L / min)

[0283] Table 2: Overview of prepared zeolite samples and their properties.

[0284] Reference Exampie 2: Gas Chromatography

[0285] Samples of the liquid product mixture from catalytic experiments were analysed by gas chromatography (HP-5890, Hewlett Packard) equipped with a flame ionization detector and a capillary colum (Restek Rtx®-5, diphenyl-Zdimethylpolysiloxane, 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.

[0286] 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.

[0287] 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.

[0288] Reference Example 3: Stoichiometric calculations for the hydrocracking of n-dodecane

[0289] 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 (m^) and liquid product (mout). Here, cracking products are all hydrocarbons that underwent at least one cracking reaction.

[0290] 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.

[0291] __ ™n-C12out

[0292] An-C12- J- . mn-C12in n100

[0293] 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 miiq.inand the liquid products rDliq-’Out

[0294] Without methane as internal standard the molar flow rates ncnfor gaseous products were calculated according to equation (8).

[0295] 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.

[0296] Reference Example 4: Determination of the surface area

[0297] Nitrogen sorption analysis was performed at 77 K using a Tristar II (Micrometrics Instruments Corporation), and the samples were degassed prior to measurements. The surface area was determined using the Brunauer-Emmett-Teller (BET) method. Reference Example 5: Determination of the Si / AI ratio

[0298] 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.

[0299] Example 16: Catalytic testing

[0300] 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 chromatography. For all experiments, the mass flow rate of reactant and liquid product mixture were detected for mass balancing. Samples of the liquid product mixtures from catalytic experiments were analyzed by gas chromatography (HP-5890, Hewlett Packard) equipped with a flame ionization detector and a capillary column (Restek Rtx®-5, diphenyl-Zdimethylpolysiloxane, 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).

[0301] Table 3: Overview of conversions and selectivities of tested zeolite samples.

[0302] All investigated catalyst are active in the catalytic hydrocracking of the corresponding feed.

[0303] 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. Description of the figures

[0304] Figure 1 is a schematic representation of a production unit used for the process according to an embodiments 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). Water is added to stream S2 obtained in (4) to obtain stream S3, which is fed into a stream cracker (5) to obtain stream S4. At least a part of the H2, methane, and ethane are separated from the stream S4 in the distillation unit (6), obtaining a stream S5. Water is added to stream S5 to obtain stream S6, which is reacted in (7) to obtain stream S7, By removing CO2 from S7, stream S8 is obtained, which is reintroduced as Fh-source in (2).

[0305] REFERENCE NUMBERS IN THE FIGURE

[0306] (1 ) feed

[0307] (2) first reactor comprising C1

[0308] (3) vapor-liquid separator

[0309] (4) distillation unit

[0310] (5) steam cracker

[0311] (6) distillation unit

[0312] (7) second reactor comprising C2

[0313] CITED LITERATURE

[0314] - WO 2019 / 229072 A1

[0315] - US 8692040 B2

[0316] - CN 112678771 A1

[0317] - US 2011 / 263916 A1

[0318] - US 2021 / 198584 A1

Claims

Ciaims1 . An integrated process for the production of Ci to C4 alkanes, olefins, and aromatic hydrocarbons, comprising(1 ) preparing a feed F1 comprising one or more compounds selected from the group consisting of C@ to C30 alkanes and oxygen containing compounds comprising one or more C@ 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 Fh-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 from the stream S1 obtained in (3), obtaining a stream S2 comprising the one or more compounds selected from the group consisting of C5 to C12 alkanes;(5) adding H2O to the stream S2, obtaining a stream S3;(6) steam cracking the one or more compounds selected from the group consisting of C5 to C12 alkanes comprised in the stream S3 by heating the stream S3, obtaining a stream S4 comprising H2, methane, ethane, olefins, and aromatic hydrocarbons;(7) separating at least part of the H2, methane, and ethane from the stream S4, obtaining a stream S5 comprising the separated H2, methane, and ethane;(8) providing a catalyst C2 comprising one or more metals selected from the group consisting of Ni, Pt, Pd, Rh, Ru, Os, and Ir;(9) adding H2O to the stream S5, obtaining a stream S6;(10) contacting the stream S6 with the catalyst C2, obtaining a stream S7 comprising H2 and CO2;(11 Separating at least part of the CO2 from the stream S7, obtaining a stream S8 comprising H2;(12) providing the stream S8 to (3) as a source of H2 for the Fh-containing atmosphere in (3).

2. The integrated process of any of claim 1 , 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.

3. The integrated process of any of claim 1 or 2, wherein the catalyst C2 further comprises one or more promoter metals.

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

5. The integrated process of any of claims 1 to 4, wherein contacting in (3) is conducted at a pressure in the range of from 20 to 200 bara.

6. The integrated process of any of claims 1 to 5, wherein the stream S3 obtained in (5) contains in the range of from 10 to 95 vol.-% of H2O.

7. The integrated process of any of claims 1 to 6, wherein steam cracking in (6) is conducted at a temperature in the range of from 500 to 950 °C.

8. The integrated process of any of claims 1 to 7, wherein steam cracking in (6) is conducted at a pressure in the range of from 1 to 5 bara.

9. The integrated process of any of claims 1 to 8, wherein the stream S6 obtained in (9) contains in the range of from 10 to 95 vol.-% of H2O.

10. The integrated process of any of claims 1 to 9, wherein contacting in (10) is conducted at a temperature in the range of from 500 to 1 ,050 °C.11 . The integrated process of any of claims 1 to 10, wherein contacting in (10) is conducted at a pressure in the range of from 5 to 50 bara.

12. The integrated process of any of claims 1 to 11 , wherein (1) comprises(1 ) preparing a feed F1 comprising one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains.

13. The process according to claim 12, 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.

14. The process according to any of claims 1 to 13, wherein the feed F1 according to (1) is a merged feed of two or more sub-feeds, wherein at least one of the two or more subfeeds comprises one or more compounds selected from the group consisting of oxygen containing compounds comprising one or more C@ to C30 alkyl chains.

15. The integrated process of any of claims 1 to 14, wherein after (4) and prior to (5) the one or more compounds selected from the group consisting of Ci to C4 alkanes obtained from separation in (4) is added to the stream S2.

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