A process for preparing carbon monoxide and hydrogen

Abstract

A process for preparing carbon monoxide and hydrogen A process for preparing carbon monoxide and molecular hydrogen, comprising a) providing a partial oxidation feed stream Spox comprising a hydrolysis oil from hydrolysis of a composite material Mc, the composite material Mc comprising an organic polymeric matrix and a fiber component; b) subjecting the stream Spox to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally one or more of H2S and at least one nitrogen compound, wherein step a) subjecting a composite material MC to hydrolysis conditions in a hydrolysis reactor obtaining a hydrolysis product comprising an aqueous phase, a fiber component and a solid polymeric hydrolysis product; the process further comprising separating the aqueous phase from the fiber component and the polymeric hydrolysis product; contacting the fiber component and the solid polymeric hydrolysis product separated according to with a solvent, thereby dissolving the polymeric hydrolysis product in said solvent, obtaining a mixture comprising the polymeric hydrolysis product dissolved in the solvent and further comprising the fiber component; separating the fiber component from the obtained mixture, obtaining a solution of the polymeric hydrolysis product; separating solvent from the obtained solution, obtaining the hydrolysis oil; wherein the hydrolysis reactor is a closed reactor; wherein the hydrolysis conditions comprise a temperature in the hydrolysis reactor in the range of from 220 to 290°C.

Description

A process for preparing carbon monoxide and hydrogenThe present invention relates to a process for preparing carbon monoxide and molecular hydrogen, comprising the partial oxidation of a feed stream which comprises a hydrolysis oil from the hydrolysis of a composite material which comprises an organic polymeric matrix and a fiber component. Further, the present invention relates to a process for recycling a composite material which comprises an organic polymeric matrix and a fiber component, wherein this recycling process comprises the steps of the process for preparing carbon monoxide and molecular hydrogen. Yet further, the present invention relates to a chemical conversion process comprising preparing carbon monoxide and molecular hydrogen by the above process.Composite materials, such as epoxy composites which are contained, for example, in wind turbine blades, typically comprise a matrix and a fiber component as well as various other components such as adhesives and coatings. Due to their complex composition, they are difficult to recycle. For example, end-of-life wind turbine blades are frequently used for landfill or are incinerated which are not the best solutions in view of carbon footprint. Therefore, there is a constant need to provide a process for suitably treating such composite materials, in particular waste composite materials, so as to render the use of such composite material more sustainable.Thus, it was an object of the present invention to provide an improved process for preparing a stream comprising carbon monoxide (CO) and molecular hydrogen (H2) from a composite material comprising an organic polymeric matrix and a fiber component, preferably for providing anefficient process to use such composite materials as a feedstock for the production of new chemical products in sustainable manner.Surprisingly, it was found the object can be achieved by the partial oxidation of a stream which is obtained from the hydrolysis of such composite materials. Hence, the present invention relates to a process for preparing carbon monoxide and molecular hydrogen, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a composite material Me, the composite material Me comprising an organic polymeric matrix and a fiber component; b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally one or more of H2S and at least one nitrogen compound.The at least one nitrogen compound referred to in b) preferably is one or more of N2, NH3 and HON. Yet further nitrogen compounds may be comprised in the stream S1.Preferably, the organic polymeric matrix comprised in the composite material Me comprises at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups. More preferably, the organic polymeric matrix comprised in the composite material Me is selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin.With regard to the cured epoxy resin, it is preferred that it is obtainable or obtained from one or more of bisphenol-A bisglycidyl ether (DGEBA), bisphenol-F bisglycidyl ether, bisphenol-S bisglycidyl ether (DGEBS), tetraglycidylmethylene dianiline (TGM-DA), epoxy novolaks, cycloaliphatic epoxy resins such as 3,4-epoxycyclohexylmethyl-3,4-epoxycyclohexanecarboxylate and hexahydrophthalic acid diglycidyl ester, and mixtures of two or more thereof. More preferably, it is selected from the group consisting of bisphenol-A bisglycidyl ether (DGEBA), oligomeric bisphenol-A bisglycidyl ether, tetraglycidylmethylene dianiline (TGM-DA), epoxy novolaks, cycloaliphatic epoxy resins and mixtures of two or more thereof. Yet more preferably, the cured epoxy resin is obtainable or obtained from a mixture of one or more non-cured epoxy resins and one or more reactive diluents, wherein the one or more reactive diluents are preferably selected from the group consisting of 1 ,4-butanediol diglycidyl ether, 1 ,6-hexanediol diglycidyl ether, glycidyl neodecanoate, glycidyl versatate, 2-ethylhexyl glycidyl ether, C8-C10 alkyl glycidyl ether, C12-C14 alkyl glycidyl ether, p-tert-butyl glycidyl ether, butyl glycidyl ether, nonylphenyl glycidyl ether, p-tert-butylphenyl glycidyl ether, phenyl glycidyl ether, o-cresyl glycidyl ether, polyoxypropylene glycol diglycidyl ether, trimethylolpropane triglycidyl ether (TMP), glycerin triglycidyl ether, triglycidy l-p-aminophenol (TGPAP), and mixtures of two or more thereof.As far as the curing method is concerned according to which the epoxy resin is obtainable or obtained, a curing method is preferred which uses one or more of an anhydride and an amine, preferably an anhydride or an amine, as curing agent. If an amine is used as curing agent, it is preferred that it is selected from the group consisting of aliphatic amines, aromatic amines, cycloaliphatic amines, adducts of epoxy resins reacted with one or more of said amines, and mixtures thereof, more preferably from the group consisting of ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, polyetheramine, 4,4'-diaminodiphenylmethane, 4,4'-diaminodicyclohexylmethane, 4,4'-diaminodiphenyl sulfone, 2,4-diaminotoluene, isophoronediamine, methylcyclohexane diamine, 1,2-diaminocyclohexane, 1,3-diaminocyclohexane, and 1,4-diaminocyclohexane, polyetheramines, polyamidoamine, adducts of epoxy resins reacted with one or more of said amines, and mixtures of two or more thereof. If an anhydride is used as curing agent, it is preferred that it is selected from the group consisting of tetrahydrophthalic anhydride, hexahydrophthalic anhydride, methyltetrahydrophthalic anhydride, methylhexahydrophthalic anhydride, benzophenone tetracarboxylic dianhydride, nadic anhydride and mixtures of two or more thereof.According to the present invention, it is preferred that from 10 to 80 weight-%, preferably from 20 to 70 weight-%, more preferably from 25 to 60 weight-%, more preferably from 30 to 50 weight-% of the composite material Me consist of the polymeric matrix. Ranges of from 30 to 40 weight-% or from 35 to 45 weight-% or from 40 to 50 weight-% are conceivable.With regard to the fiber component comprised in the composite material Me, it is preferred that it is selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers ceramic fibers and mixtures thereof, more preferably selected from the group consisting of glass fibers, carbon fibers, aramid fibers, basalt fibers and mixtures thereof, more preferably selected from the group consisting of glass fibers, carbon fibers and mixtures of two or more thereof. Yet more preferably, the composite material Me comprises one single fiber type. Still more preferably, the fiber component comprised in the composite material Me comprises, preferably consists of glass fibers.According to the present invention, it is preferred that from 20 to 89 weight-%, more preferably from 25 to 79 weight-%, more preferably from 30 to 70 weight-%, more preferably from 40 to 60 weight-% of the composite material Me consist of the fiber component. Ranges of from 40 to 50 weight-% or from 45 to 55 weight-% or from 50 to 60 weight-% are conceivable.Further according to the present invention, from 60 to 100 weight-%, more preferably from 65 to 98 weight-%, more preferably from 70 to 95 weight-% of the composite material Me consist of the organic polymeric matrix and the fiber component. Ranges of from 70 to 80 weight-% or from 75 to 85 weight-% or from 80 to 90 weight-% or from 85 to 95 weight-% are conceivable.If less than 100 weight-% of the composite material Me consist of the organic polymeric matrix and the fiber component, it is preferred that the composite material Me further comprises one or more of balsa wood and polyethylene terephthalate foam, wherein it is more preferred that from 0.5 to 20 weight-%, more preferably from 0.7 to 15 weight-%, more preferably of from 0.9 to 10 weight-%, more preferably of from 1 to 8 weight-% of the composite material Me consist of the one or more of balsa wood and polyethylene terephthalate foam.Therefore, it is preferred that from 70 to 100 weight-%, more preferably from 75 to 98 weight-%, more preferably from 80 to 95 wt.-% of the composite material Me consist of the polymeric matrix, the fiber component, and the one or more of balsa wood and polyethylene terephthalate foam. Ranges of from 70 to 80 weight-% or from 75 to 85 weight-% or from 80 to 90 weight-% or from 85 to 95 weight-% are conceivable.According to the present invention, it is especially preferred that the composite material Me from which the hydrolysis oil is obtained exhibits a low, more preferably a very low polyvinylchloride content. In particular, it is preferred that at most 0.1 weight-%, preferably at most 0.05 weight-%, more preferably at most 0.01 weight-% of the compositematerial Me consist of polyvinylchloride. Therefore, preferred ranges are from 0 to 0.1 weight-%, more preferably from 0 to 0.05 weight-%, more preferably from 0 to 0.01 weight-%.Preferably, the composite material Me is selected from the group consisting of one or more parts of an air plane, one or more part of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, more preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade.When subjected to hydrolysis, the composite material Me is preferably in the form of particles exhibiting a suitable size and shape in line with the hydrolysis unit used. Preferably, the composite material Me to be subjected to hydrolysis is in the form of particles exhibiting an average length in the range of from 0.1 cm to 3 m, more preferably in the range of from 0.5 cm to 50 cm, more preferably in the range of from 1 cm to 3 cm. Ranges such as from 0.5 to 3 m or from 1 to 2.5 m or from 1.5 to 2 m, or from 5 to 50 cm or from 10 to 40 cm or from 15 to 25 cm are conceivable.Preferably according to the present invention, the hydrolysis oil comprised in the partial oxidation feed stream SPOX is obtainable or obtained by a process comprisinga) providing the composite material Me;p.1 ) subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor.Alternatively or additionally, providing the partial oxidation feed stream SPOX according to a) preferably comprises preparing the hydrolysis oil comprised in SPOX, comprisinga) providing the composite material Me;p.1 ) subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor.With regard to the hydrolysis conditions, it is preferred that subjecting the composite material Me to hydrolysis conditions in the hydrolysis reactor comprises introducing the composite material Me and water into the hydrolysis reactor at a weight ratio of water relative to composite material in the range of from 10:1 to 0.1:1, more preferably in the range of from 5:1 to 0.2:1, more preferably in the range of from 2.5:1 to 0.3:1. Ranges of from 2:1 to 0.5:1 or from 1.5:1 to 1:1 are conceivable.Preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 97 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-% of the mixture to be subjected to hydrolysis conditions in the hydrolysis reactor consist of the composite material Me and water. More preferably, said mixture to be subjected to hydrolysis conditions in the hydrolysis reactor contains less than 4volume-%, more preferably less than 3 volume-%, more preferably less than 2 volume-%, more preferably less than 1 volume-%, more preferably less than 0.5 volume-%, more preferably less than 0.2 volume-%, more preferably less than 0.1 volume-%, more preferably essentially no carbon dioxide in supercritical fluid form, more preferably no carbon dioxide in supercritical form. More preferably, said mixture to be subjected to hydrolysis conditions in the hydrolysis reactor contains less than 4 volume-%, more preferably less than 3 volume-%, more preferably less than 2 volume-%, more preferably less than 1 volume-%, more preferably less than 0.5 volume-%, more preferably less than 0.2 volume-%, more preferably less than 0.1 volume-%, more preferably essentially no ethanol, preferably no alcohol in its superheated state or supercritical fluid form, more preferably no ethanol, preferably no alcohol in its superheated state or supercritical fluid form.Further preferably according to the present invention, no oxygen (O2) is passed into the hydrolysis reactor in addition to any oxygen possibly present in the water and / or the composite material fed into the hydrolysis reactor. Thus, in particular, no separate gas stream comprising or consisting of oxygen is fed into the hydrolysis reactor in addition to the water and the composite material.Further preferably, the hydrolysis reactor used according to the present invention is a closed reactor, more preferably an autoclave, the hydrolysis preferably being carried out under autogenous pressure, preferably the vapor pressure of the water in the hydrolysis reactor.Yet further preferably, the hydrolysis conditions comprise a temperature in the hydrolysis reactor in the range of from 220 to 320 °C, more preferably in the range of from 230 to 300 °C, more preferably in the range of from 240 to 290 °C. Ranges of from 240 to 260 °C or from 250 to 270 °C or from 260 to 280 °C or from 270 to 290 °C are conceivable.Still further preferably, the hydrolysis conditions comprise a hydrolysis time in the range of from 10 to 600 min, preferably in the range of from 10 to 300 min, more preferably in the range of from 10 to 180 min, more preferably in the range of from 10 to 120 min. Ranges of from 10 to 60 min or from 30 to 90 min or from 60 to 120 min are conceivable.According to the present invention, it is also conceivable that the hydrolysis conditions comprise a treatment with superheated steam, for example at a temperature of 300 °C at ambient pressure.Preferably according to the present invention, the hydrolysis conditions comprise the absence of an alkaline hydrolysis catalyst.Preferably according to the present invention, subjecting the composite material Me to hydrolysis according to |3.1) comprises subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor, obtaining ahydrolysis product comprising an aqueous phase, a fiber component and a solid polymeric hydrolysis product, wherein the process further comprisesp.2) separating the aqueous phase from the fiber component and the polymeric hydrolysis product;p.3) contacting the fiber component and the solid polymeric hydrolysis product separated according to p.2) with a solvent, thereby dissolving the polymeric hydrolysis product in said solvent, obtaining a mixture comprising the polymeric hydrolysis product dissolved in the solvent and further comprising the fiber component;p.4) separating the fiber component from the mixture obtained according to p.3), obtaining a solution of the polymeric hydrolysis product;p.5) separating solvent from the solution obtained according to p.4), obtaining the hydrolysis oil.Preferably, the process further comprisesp.2) separating the aqueous phase from the fiber component and the polymeric hydrolysis product;p.3) contacting the fiber component and the solid polymeric hydrolysis product separated according to p.2) with a liquid solvent, thereby dissolving the polymeric hydrolysis product in said liquid solvent, obtaining a mixture comprising the polymeric hydrolysis product dissolved in the liquid solvent and further comprising the fiber component;p.4) separating the fiber component from the mixture obtained according to p.3), obtaining a solution of the polymeric hydrolysis product;p.5) separating the liquid solvent from the solution obtained according to p.4), obtaining the hydrolysis oil.Preferably, separating the aqueous phase according to p.2) comprises one or more of filtration, centrifugation and decantation. Further preferably, separating the aqueous phase according to p.2) is carried out at a temperature of the hydrolysis product in the range of from 5 to 80 °C, preferably in the range of from 15 to 60 °C, more preferably in the range of from 20 to 30 °C.Preferably, the solvent according to p.3) is selected from the group consisting of ethers, monoalcohols, glycols, esters, acids, ketones, amides, and mixture of two or more thereof. More preferably, the solvent according to p.3) is selected from the group consisting of tetrahydrofuran, dioxane, tert-butyl methyl ether, cyclopentyl methyl ether, methanol, ethanol, 1 -propanol, 2-propanol, butanols, monoethylene glycol, diethylene glycol, ethyl acetate, propyl acetate, butyl acetate, gamma-valerolactone, epsilon-caprolactone, formic acid, acetic acid, propionic acid, acetone, methyl ethyl ketone, cyclohexanone, formamide, dimethylformamide, N-alkylpyrrolidones such as N- methylpyrrolidone, or N-butylpyrrolidone, epsilon-caprolactam, sulfolane, one or more suitable solvents from waste streams intended for combustion, and mixtures of two or more thereof. More preferably, the solvent according to p.3) is selected from the group consisting of methanol, ethanol, 1 -propanol, 2-propanol, butanols, monoethylene glycol, diethylene glycol, and mixtures of two or more thereof. Preferably according to p.3), the fiber component and the solid polymeric hydrolysis product are brought in contact with the solvent at the boiling point of the solvent, preferably at a pressure in the range of from 0.9 to 3 bar(abs), more preferably in the range of from 0.95 to 2 bar(abs).Preferably according to the present invention, the fiber component separated according to p.4), optionally after removal of water and / or solvent from the fiber component, is suitably re-used, preferably as a component for preparing an engineering plastics materials, more preferably for preparing an engineering plastics material comprising one or more of polyamide 6 and polyamide 6.6, wherein said plastics material is preferably used in the automotive industry and / or used a part of a wind blade.The hydrolysis oil which is obtained according to p.5) exhibits, at a temperature of the hydrolysis oil of 90 °C, a viscosity preferably in the range of from 10 to 107mPa*s, more preferably in the range of from 10 to 106mPa*s, more preferably in the range of from 10 to 105mPa*s, more preferably in the range of from 10 to 104mPa*s.Preferably according to the present invention, the weight- % ratio of nitrogen comprised in the hydrolysis oil obtained according to p.5) relative to organic nitrogen comprised in the composite material from which said hydrolysis oil is prepared, in each case calculated as elemental N, is at most 0.9:1, preferably at most 0.8:1, more preferably at most 0.7:1, more preferably at most0.6:1.Preferably, the hydrolysis oil obtained according to p.5) exhibits at least one, preferably at least two, more preferably at least three, more preferably at least four, more preferably all of the following features (i) to (v):(i) a carbon content, calculated as elemental C, in the range of from 55 to 80 weight-%;(ii) a hydrogen content, calculated as elemental H, in the range of from 5 to 15 weight-%;(iii) an oxygen content, calculated as elemental O, in the range of from 12 to 25 weight-%;(iv) a nitrogen content, calculated as elemental N, in the range of from 12 to 25 weight-%;(v) a sulphur content, calculated as elemental S, in the range of from 0 to 1 weight-%;in each case based on the total weight of the hydrolysis oil.More preferably, the fiber component content of the hydrolysis oil obtained according to p.5) is in the range of from 0 to 1 weight-%, more preferably in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.01 weight-%, based on the total weight of the hydrolysis oil.In addition to the hydrolysis oil, the partial oxidation feed stream SPOX optionally or preferably further comprises a further component. It is to be understood that according to the present invention, the partial oxidation feed stream SPOX may comprise two or more hydrolysis oils, preferably two or more hydrolysis oils from hydrolysis of at least one composite material Me. Preferably, said further component is selected from the group consisting of one or more non-gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof, wherein said further component more preferably exhibits at least one, more preferably at least two, more preferably at least three, more preferably, more preferably all of the following features:(I') a heating value of at least 20,000 J / g, preferably in the range of from 20,000 to 50,000 J / g, more preferably in the range of from 25,000 to 45,000 J / g, more preferably in the range of from 30,000 to 40,000 J / g, the heating value being measured in accordance with DIN 51900;(II') a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(I I'.1 ) a carbon content, calculated as elemental C, of at least 55 weight-%, preferably in the range of from 55 to 97 weight-%, more preferably in the range of from 70 to 94 weight-%;(I I'.2) an oxygen content, calculated as elemental O, of at most 40 weight-%, preferably in the in the range of from 0 to 40 weight-%, more preferably in the range of from 2 to 25 weight-%;(I I'.3) a nitrogen content, calculated as elemental N, in the range of at most 4 weight-%, preferably in the range of from 0 to 4 weight-%, more preferably in the range of from 0.005 to 2 weight-%; in each case based on the total weight of the respective component.Preferably, the one or more non-gaseous organic components preferably exhibit the further feature (III'):(III') a viscosity in the range of from 1 to 10 mPa»s, as measured at 40 °C in accordance with DIN 53019.If, for example, the further component is a non-gaseous organic component such as a liquid organic component, it is preferred that that hydrolysis oil and the further component are admixed upstream of the partial oxidation reactor or admixed in the partial oxidation reactor. If, for example, the further component is a gaseous organic component, it is preferred that the hydrolysis oil and the gaseous organic component are passed into the partial oxidation reactor separately via the same means, preferably via the same nozzle.Preferably, the one or more non-gaseous organic components are selected from the group consisting of bio oils, pyrolysis oils from pyrolysis of biomass, pyrolysis oils from pyrolysis of plastic waste, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphaltene fractions, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, industrial waste streams, coal dusts, and mixtures of two or more thereof.Preferably, the one or more gaseous organic components are selected from the group consisting of natural gas, biogas, cracker fuel gas, and a mixture of two or more thereof. The term "cracker fuel gas” as used herein refers to a byproduct of the petrochemical industry, specifically from the process of "cracking." "Cracking” is a method used to break down large hydrocarbon molecules into smaller ones, often to produce ethylene, propylene, and other valuable chemicals. The gas produced during this process, known as cracker fuel gas, typically contains a mixture of hydrogen, methane, ethane, and other light hydrocarbons. The term "biogas” as used herein refers to a gaseous renewable energy source produced from raw materials such as agricultural waste, manure, municipal waste, plant material, sewage, green waste, wastewater, and food waste. Biogas is produced by anaerobic digestion with anaerobic organisms or methanogens inside an anaerobic digester, biodigester or a bioreactor. The term "(high) vacuum residue” as used herein refers to a component which is obtainable or obtained by a processcomprising subjecting crude oil, optionally after desalting, the atmospheric distillation, subjecting the atmospheric residue obtained as high-boiling fraction from said atmospheric distillation to vacuum distillation, and obtaining the vacuum residue as high-boiling fraction from said vacuum distillation.According to the present invention, it is possible that the pyrolysis oil referred to hereinabove is obtainable or obtained by a method comprisingo') providing a composite material, optionally a composite as defined herein;p') subjecting the composite material provided according to o') to pyrolysis in a pyrolysis reactor at a temperature in the reactor in the range from 300 to 800 °C, preferably in the range of from 300 to 700 °C, more preferably in the range of from 300 to 600 °C, and a pressure in the reactor in the range of from 0.1 to 50 bar(abs), preferably in the range of from 0.1 to 10 bar(abs), more preferably in the range of from 0.5 to 2 bar(abs), obtaining a crude reactor effluent, comprising a gaseous, liquid and solid phase;y') subjecting the crude reactor effluent obtained according to p') to a separation step or a sequence of separation steps, obtaining the pyrolysis oil;wherein the reactor according to p') is a preferably a batch reactor, a semi-batch reactor, a fixed bed reactor, a shaft reactor, a fluidized bed reactor, a rotary kiln, or a microwave reactor, more preferably a batch reactor, a semi-batch reactor or a fixed bed reactor;wherein the pyrolysis according to p') is preferably conducted continuously.Regarding the composition of the partial oxidation feed stream SPOX, it is preferred that from 50 to 100 weight-%, more preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-% of SPOX consist of the hydrolysis oil and optionally the further component selected from the group consisting of one or more non-gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof. Ranges of from 96 to 100 weight-% or from 97 to 100 weight-% or from 98 to 100 weight-%, or from 99 to 100 weight-% are conceivable.Preferably, the stream SPOX exhibits at least one, preferably at least two, more preferably all of the following five features (I) to (III), and with regard to the feature (III), preferably at least one, more preferably at least two, more preferably at least three, more preferably at least four, more preferably all of the features (III.1) to (III.5):(I) a heating value in the range of from 20,000 to 46,000 J / g, preferably of from 35,400 to 45,300 J / g, more preferably of from 37,000 to 42,000 J / g, as measured in accordance with DIN 51900;(II) an ash content in the range of from 0 to 17,000 mg / kg, as measured in accordance with ISO 6245;(III) a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(111.1) a carbon content, calculated as elemental C, in the range of from 60 to 99 weight-%, preferably in the range of from 70 to 96 weight-%;(111.2) a hydrogen content, calculated as elemental H, in the range of from 1 to 15 weight-%, preferably in the range of from 2 to 10 weight-%;(111.3) an oxygen content, calculated as elemental 0, in the range of from 0 to 25 weight-%, preferably in the range of from 1 to 20 weight-%;(111.4) a sulphur content, calculated as elemental S, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;(111.5) a nitrogen content, calculated as elemental N, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;in each case based on the total weight of the component C, wherein the sum of the amounts of carbon (C), hydrogen (H), oxygen (O), sulphur (S), and nitrogen (N) in the stream SPOX is in the range of from 70 to 100 weigh-%, preferably of from 80 to 99.9 weight-%, more preferably of from 90 to 99.5 weight-%, more preferably of from 95 to 99.5 weight-%, based on the weight of the component C.Especially preferably according to the present invention, the partial oxidation feed stream SPOX is not subjected to hydrotreatment, i.e. treatment with hydrogen (H2), prior to being subjected to partial oxidation according to b). By such hydrotreatment, for example, double bonds and / or conjugated double bonds of compounds comprised in the pyrolysis oil would be at least partially saturated and / or sulphur would be removed by forming H2S.With regard to the partial oxidation according to b), it is preferred that the partial oxidation conditions according to b) comprise a temperature in the partial oxidation reactor in the range of from 400 to 2000 °C, more preferably in the range of from 1000 to 1750 °C, more preferably in the range of from 1250 to 1500 °C. The temperature refers to the temperature of the gas atmosphere in the partial oxidation reactor. Ranges of from 1250 to 1350 °C or from 1300 to 1400 °C or from 1350 to 1450 °C or from 1400 to 1500 °C are conceivable.Further preferably, the partial oxidation conditions according to b) comprise a pressure in the reactor in the range of from 1 to 200 bar(abs), more preferably in the range of from 5 to 150 bar(abs), more preferably in the range of from 10 to 100 bar(abs), more preferably in the range of from 11 to 50 bar(abs). Ranges of from 11 to 30 bar(abs) or from 25 to 35 bar(abs) or from 30 to 40 bar(abs) or from 35 to 45 bar(abs) or from 40 to bar(abs) are conceivable.Further preferably, subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) comprises introducing the partial oxidation feed stream SPOX and oxygen (O2) into the reactor at a weight ratio of O2 relative to SPOX in the range from 0.4:1 to 1.3:1, more preferably in the range of from 0.6:1 to 1.25:1, more preferably in the range of from 0.7:1 to 1.2:1. Ranges of from 0.7:1 to 0.9:1 or from 0.8:1 to 1.0:1 or from 0.9:1 to 1.1:1 or from 1.0:1 to 1.2:1 are conceivable.Further preferably, subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) further comprises introducing steam into the reactor, more preferably at a weight ratio of steam relative to SPOX of at least 0.2:1, preferably in the range of from 0.2:1 to 2:1, more preferably in the range of from 0.3:1 to 2:1, morepreferably in the range of from 0.4:1 to 1.5:1, more preferably in the range of from 0.4:1 to 1:1. Ranges of from 0.4:1 to 0.6:1 or from 0.5:1 to 0.7:1 or from 0.6:1 to 0.8:1 or from 0.7:1 to 0.9:1 or from 0.8:1 to 1:1 are conceivable.Preferably according to the present invention, the process further comprisesc) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprising CO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2’.Preferably, step c) comprisesc-1) subjecting the stream S1 obtained according to b) to a washing step in a washing unit, obtaining a stream S1' depleted in particulate solid compared to S1 and comprising CO, H2, CO2, H2O, CH4, and optionally H2S; c-2) subjecting the stream S1' obtained according to c-1) to a drying step in a drying unit, obtaining a stream S1” depleted in H2O compared to S1 and S1';c-3) subjecting the stream S1” obtained according to c-2) to an acid gas removal step in a CO2 / H2S adsorption unit, obtaining the stream S2.If the process comprises the step d), it is preferred that d) comprisespassing and contacting water with S2 obtained according to c) into a reaction unit for a water gas shift reaction, obtaining a stream S2' depleted in CO compared to S2 and comprising CO, H2, CH4 and CO2, optionally followed by passing S2' into an acid gas removal unit, obtaining a stream S2' depleted in CO2 and comprising CO, H2 and CH4; orpassing and contacting CO2 with S2 obtained according to c) into a reaction unit for a reverse water gas shift reaction, obtaining a stream S2' enriched in CO compared to S2 and comprising CO, H2, CH4 and H2O; or adding H2 to S2 obtained according to c), obtaining a stream S2' enriched in H2 compared to S2 and comprising CO, H2 and CH4, wherein it is more preferred that at least a portion of the added H2 is H2 from a renewable source.Preferably, step e) comprises subjecting S2 or S2' to cryogenic separation, obtaining S3, S4 and preferably a gas stream S5 comprising CH4 and being depleted in CO and H2 compared to S2, optionally S2’. The cryogenic separation according to e) can be performed by a method known in the art, such as disclosed in Ullmann's Encyclopedia of Industrial Chemistry, Carbon Monoxide, Chapter 4.3.2, p.685-686.Further according to the present invention, it is possible, preferably preferred, that the process further comprises f) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products.Therefore, the present invention also relates to a chemical conversion process, comprising preparing carbon monoxide (CO) and molecular hydrogen (H2) by a process according to a process as defined hereinabove, and further comprising the subsequent step f):f) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products.According to f), the carbon monoxide CO and / or the hydrogen H2 used in f) is / are blended with CO and / or H2 from other sources.Preferably, step f) comprisesf-1) bringing in contact CO comprised in S3 with methanol and subjecting CO and methanol to a chemical conversion, obtaining a stream S6 comprising a first chemical product being methyl formate;f-2) optionally bringing in contact at least a portion of S6 obtained according to f-1) with ammonia and subjecting said portion of S6 and ammonia to a chemical conversion, obtaining a stream S8 comprising methanol and a second chemical product being formamide;f-3) optionally separating formamide from methanol comprised in S7 obtained according to f-2) and optionally recycling methanol to f-1), obtaining a stream S7' being depleted in methanol compared to S7 and comprising formamide;f-4) optionally subjecting at least a portion of S7 obtained according to f-2) or at least a portion of S7' obtained according to f-3) to a thermal decomposition and subsequent water removal, obtaining a stream S8 comprising a third chemical compound being hydrogen cyanide.Yet further preferably, downstream of f-4), f) further comprisesf-5) bringing in contact at least a portion of S8 obtained according to f-4) with isophorone and subjecting to a chemical conversion, being a Michael addition reaction, obtaining a stream S9 comprising isophorone nitrile;f-6) optionally subjecting at least a portion of S9 obtained according to f-5) to hydrogenation, preferably using H2 obtained in accordance with e), in the presence of ammonia, obtaining a stream P comprising a chemical product being isophorone diamine.Also preferably, step f) comprises subjecting an alcohol, a ketone, or an aldehyde to a chemical conversion with ammonia, a primary or secondary amine in the presence of H2 obtained according to e), and a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being an amine.Also preferably, step f) f) comprises subjecting an organic nitrile to a hydrogenation reaction in the presence of H2 obtained according to e), and a heterogeneous catalyst, obtaining a chemical product being an amine. More preferably, the organic nitrile is obtainable or obtained by a process comprising subjecting an alkene to a chemical conversion with hydrogen cyanide obtained according to f-4) as defined herein. It is to be understood that according to the present invention, the alkene referred to above is neither a butadiene nor a pentenenitrile. For the avoidance of doubt, the chemical conversion of a butadiene and / or a pentenenitrile with hydrogen cyanide obtained in accordance with f-4) is explicitly excluded from the subject-matter and scope of this invention.Also preferably, step f) comprises hydrogenating an organic nitro compound with H2 obtained according to e), obtaining a chemical product being an amine.Also preferably, step f) comprises subjecting CO obtained according to e) to a chemical conversion with gaseous chlorine, obtaining a chemical product being phosgene, and optionally subjecting at least a portion of the obtained phosgene to a chemical conversion with an amine, obtaining a further chemical product being an isocyanate. More preferably, the amine is obtainable or obtained by process as defined herein.Also preferably, step f) comprises subjecting a mixture of CO obtained according to e) and H2 obtained according to e) to a chemical conversion in the presence of a heterogeneous catalyst, obtaining a chemical product being methanol. More preferably, f) further comprises subjecting at least a portion of the obtained methanol to a partial oxidation reaction, obtaining a chemical product being formaldehyde. More preferably, f) further comprises subjecting at least a portion of the obtained formaldehyde to a chemical conversion, being a Reppe reaction, with acetylene, obtaining a chemical product being 1 ,4-butyndiole, and optionally subjecting at least a portion of the obtained 1,4-butyndiole to hydrogenation, preferably using H2 obtained according to e), obtaining a chemical product being 1,4-butanediole, and optionally subjecting at least a portion of the obtained 1 ,4-butandiole to a chemical conversion with epichlorohydrin, obtaining a chemical product being 1 ,4-butanediol-diglycidylether. Further more preferably, f) further comprises subjecting at least a portion of the obtained methanol to a chemical conversion in the presence of a zeolite catalyst, obtaining a mixture comprising ethylene and propylene, and subjecting the obtained mixture to one or more separation steps, obtaining a first chemical product being ethylene and a second chemical product being propylene. Further more preferably, f) comprises subjecting a mixture of CO and H2, CO and / or H2, preferably CO and H2, beingobtained according to e), to a Fischer-Tropsch synthesis, obtaining a mixture of hydrocarbons, and subjecting the obtained mixture of hydrocarbons to one or more separation steps, obtaining chemical products being one or more alkenes, preferably one or more of ethylene and propylene.Also preferably, f) comprises subjecting a polyether alcohol to a chemical conversion with ammonia in the presence of H2 obtained according to e) and further in the presence of a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being a polyether amine. More preferably, the polyether alcohol is selected from the group consisting of polypropylene glycols, polyethylene glycols and polypropylene ethylene glycol copolymers, said polyether alcohol being obtainable or obtained by a process comprising subjecting ethylene and / or propylene to a partial oxidation, obtaining ethylene oxide and / or propylene oxide, and subjecting the obtained ethylene oxide and / or propylene oxide to a polymerization reaction, obtaining the respective polyether alcohol, wherein f) comprises subjecting a mixture of CO and H2, CO and / or H2, preferably CO and H2, being obtained according to e), to a Fischer-Tropsch synthesis, obtaining a mixture of hydrocarbons, and subjecting the obtained mixture of hydrocarbons to one or more separation steps, obtaining chemical products being one or more alkenes, preferably one or more of ethylene and propylene. More preferably, the polyether alcohol is a polypropylene glycol having a number average molecular weight in the range from 200 to 3000 g / mol, preferably in the range from 210 to 2100 g / mol, more preferably in the range from 210 to 500 g / mol.Also preferably, step f) comprises:providing an epoxy resin and an amine;providing a fiber component selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers, ceramic fibers, mixtures thereof, preferably the fiber component is selected from glass fibers, carbon fibers, aramid fibers, basalt fibers, mixtures thereof, more preferably the fiber component is selected from glass fibers, carbon fibers, and mixtures thereof;curing the epoxy resin with the amine in the presence of the fiber component, obtaining a chemical product being a composite material;wherein at least one of the following two conditions applies:the epoxy resin is 1 ,4-butanediol diglycidylether as defined herein;the amine is an amine obtained as defined herein.Further, the present invention relates to a recycling process for providing a hydrolysis oil and optionally a pyrolysis oil, comprising providing a material comprising a chemical product manufactured according to the process as defined herein; subjecting the material to a shredding step or a sequence of shredding steps to obtain a shredded material; and subjecting the shredded material to hydrolysis to obtain the hydrolysis oil and optionally to pyrolysis to obtain the pyrolysis oil.Yet further, the present invention relates to a process for recycling a first composite material, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a first composite material Mei comprising an organic polymeric matrix and a fiber component, wherein the organic polymeric matrix comprised in the composite material Mei comprises preferably at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups, wherein the organic polymeric matrix comprised in the composite material Me is more preferably selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin;b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally H2S;c) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprising CO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2';f) preparing a second composite material Mc2, comprisingsubjecting at least a portion of S3 comprising CO obtained according to e) and / or at least a portion of S4 comprising H2 obtained according to e) to a sequence of chemical conversions, obtaining one or more precursors of the second composite material Mc2;reacting the one or more precursors with a fiber component, obtaining the second composite material MC2‘According to another aspect of the present invention relates to a process, preferably a process as defined hereinabove, comprising the step of converting a chemical material obtainable or obtained by said process as defined hereinabove, to obtain a product Q.Preferably, the product Q is selected from:building block or monomer; orpolymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orindustrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; oragrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; oraqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; orcosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; orpolymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Preferably, the content of the chemical material in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / orthe content of the chemical material in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1, which is incorporated herein by reference in its entirety. Preferably, the product Q referred to in the preceding paragraph is a product as described in Reference RF1; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process for the production of a product, preferably product Q.The converting step to obtain the product Q preferably comprises one or more step(s) as de-scribed below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from:recycling, preferably depolymerizing, gasifying, pyrolyzing, and / or steam cracking; and / orpurifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, ab-sorbing, adsorbing and / or subjecting to ion exchanger; and / orassembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / orforming, preferably foaming, extruding and / or molding; and / orfinishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1; paragraphs

[1000] to

[8005] ,The term "building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a high-er structural complexity and / or higher molecular weight than the building block on which the sec-ondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic com-pounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term "monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acry lie acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term "intermediate com-pound”, as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate com-pound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, prefer-ably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI).The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term "polymer A”, as used in the context of the product Q herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1.The term "polymer composition A”, as used in the context of the product Q herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. rein-forcement, colorant, modifier and / or flame retardant, and is defined in more detail in paragraph

[2008] of Reference RF1.The term "polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is de-fined in more detail in paragraphs

[2009] and

[2010] of Reference RF1.The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably poly-mer composition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1.The term "industrial use polymer”, as used in the context of the product Q herein, comprises rhe-ology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term "industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1. The term "industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1. The term "industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1. The term "industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1. The term "industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Reference RF1. The term "composition and / or formulation thereof' with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Reference RF1. The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1.The term "agrochemical composition”, as used in the context of the product Q herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agro-chemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1, paragraph

[4001] ,The agrochemical composition may take the form of any customary formulation. The agro-chemical compositions are prepared in a known manner, e.g. described by Mollet and Grube-mann, Formulation technology, Wiley VCH, Weinheim, 2001; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be con-ducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to com-pounds mentioned in sections "Polymer” and "Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof' may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used in the context of the product Q herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used in the context of the product Q herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in para-graph

[5001] of Reference RF1.The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used in the con-text of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrrolidone-copolymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1.The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used in the context of the product Q here-in, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more de-tail in paragraph

[5003] of Reference RF1.The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term "aqueous polymer dispersion”, as used in the context of the product Q herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled "aqueous polymer dispersion” of Reference RF1. The dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term "emulsion polymer”, as used herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

[6002] entitled "Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth)acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term "polymeric dispersant”, as used in the context of the product Q herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled "Polymeric dispersant” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled "Emulsion polymerization” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled "Process for the preparation of aqueous poly-urethane dispersions” and section [6017)] entitled "Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1.Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 :section

[6004] entitled "Uses of aqueous polymer dispersions”,section

[6005] entitled "Binders for architectural and construction coatings”section

[6006] entitled "Binders for paper coating”section

[6007] entitled "Binders for fiber bonding”section

[6008] entitled "Adhesive polymers and adhesive compositions”section

[6015] entitled "Aqueous polyurethane dispersions suitable for use in coating compositions”section

[6016] entitled "Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions”section

[6017] entitled "Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them”section

[6018] entitled "Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositionsUV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled "UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hot melt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1.Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled "Polyisocyanates” of Reference RF1.Hyperbranched polyester polyol(s) and its / their uses are defined in more detail in section

[6011] entitled "Organic solvent based hyperbranched polyester polyols suitable for use in coating com-positions” of Reference RF1. The converting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

[6012] entitled "Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1. Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled "Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsatu-rated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled "Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1.100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1.Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1. The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1. The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1. The term "inorganic binder composition” comprising the polymeric dispersant(s), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Reference RF1 entitled "Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1.The term "cosmetic surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1. The term "emollient”, as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1. The term "wax”, as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1. The term "cosmetic polymer”, as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term "UV filter”, as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1. The term "further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Com-mission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term "composition and / or formulation thereof” with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1. The converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1.The terms "polymer B”, "polymer composition B”, "coating composition”, "other functional com-position”, "foil”, "molded body”, "coating” and "coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.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 instancewhere a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 3", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1, 2 and 3". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.1. A process for preparing carbon monoxide and molecular hydrogen, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a composite material Me, the composite material Me comprising an organic polymeric matrix and a fiber component;b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally one or more of H2S and at least one nitrogen compound.2. The process of embodiment 1 , wherein the organic polymeric matrix comprised in the composite material Me comprises at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups, wherein the organic polymeric matrix comprised in the composite material Me is preferably selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin.3. The process of embodiment 2, wherein the cured epoxy resin is obtainable or obtained from one or more of bisphenol-A bisglycidyl ether (DGEBA), bisphenol-F bisglycidyl ether, bisphenol-S bisglycidyl ether (DGEBS), tetraglycidylmethylene dianiline (TGM-DA), epoxy novolaks, cycloaliphatic epoxy resins such as 3,4- epoxycyclohexylmethyl-3,4-epoxycyclohexanecarboxylate and hexahydrophthalic acid diglycidyl ester, and mixtures of two or more thereof, preferably selected from the group consisting of bisphenol-A bisglycidyl ether (DGEBA), oligomeric bisphenol-A bisglycidyl ether, tetraglycidylmethylene dianiline (TGM-DA), epoxy novolaks, cycloaliphatic epoxy resins and mixtures of two or more thereof.4. The process of embodiment 2 or 3, wherein the cured epoxy resin is obtainable or obtained from a mixture of one or more non-cured epoxy resins and one or more reactive diluents, wherein the one or more reactive diluents are preferably selected from the group consisting of 1,4-butanediol diglycidyl ether, 1 ,6-hexanediol diglycidyl ether, glycidyl neodecanoate, glycidyl versatate, 2-ethylhexyl glycidyl ether, C8-C10 alkyl glycidyl ether, C12-C14 alkyl glycidyl ether, p-tert-butyl glycidyl ether, butyl glycidyl ether, nonylphenyl glycidyl ether,p-tert-butylphenyl glycidyl ether, phenyl glycidyl ether, o-cresyl glycidyl ether, polyoxypropylene glycol diglycidyl ether, trimethylolpropane triglycidyl ether (TMP), glycerin triglycidyl ether, triglycidy l-p-aminophenol (TGPAP), and mixtures of two or more thereof.5. The process of any one of embodiments 2 to 4, wherein the cured epoxy resin is obtainable or obtained by a curing method using one or more of an anhydride and an amine, preferably an anhydride or an amine, as curing agent.6. The process of embodiment 5, wherein the amine used as curing agent is selected from the group consisting of aliphatic amines, aromatic amines, cycloaliphatic amines, adducts of epoxy resins reacted with one or more of said amines, and mixtures thereof, preferably from the group consisting of ethylenediamine, diethylenetriamine, triethylenetetramine, tetraethylenepentamine, polyetheramine, 4,4'- diaminodiphenylmethane, 4,4'-diaminodicyclohexylmethane, 4,4'-diaminodiphenyl sulfone, 2,4- diaminotoluene, isophoronediamine, methylcyclohexane diamine, 1,2-diaminocyclohexane, 1,3- diaminocyclohexane, and 1,4-diaminocyclohexane, polyetheramines, polyamidoamine, adducts of epoxy resins reacted with one or more of said amines, and mixtures of two or more thereof.7. The process of embodiment 5 or 6, wherein the anhydride used as curing agent is selected from the group consisting of tetrahydrophthalic anhydride, hexahydrophthalic anhydride, methyltetrahydrophthalic anhydride, methylhexahydrophthalic anhydride, benzophenone tetracarboxylic dianhydride, nadic anhydride and mixtures of two or more thereof.8. The process of any one of embodiments 1 to 7, wherein from 10 to 80 weight-%, preferably from 20 to 70 weight-%, more preferably from 25 to 60 weight-%, more preferably from 30 to 50 weight-% of the composite material Me consist of the polymeric matrix.9. The process of any one of embodiments 1 to 8, wherein the fiber component comprised in the composite material Me is selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers ceramic fibers and mixtures thereof, preferably selected from the group consisting of glass fibers, carbon fibers, aramid fibers, basalt fibers and mixtures thereof, more preferably selected from the group consisting of glass fibers, carbon fibers and mixtures of two or more thereof.10. The process of any one of embodiments 1 to 9, wherein the composite material Me comprises one single fiber type.11. The process of embodiment 9 or 10, wherein the fiber component comprised in the composite material Me comprises, preferably consists of glass fibers.The process of any one of embodiments 1 to 11 , wherein from 20 to 89 weight-%, preferably from 25 to 79 weight-%, more preferably from 30 to 70 weight-%, more preferably from 40 to 60 weight-% of the composite material Me consist of the fiber component.The process of any one of embodiments 1 to 12, wherein from 60 to 100 weight-%, preferably from 65 to 98 weight-%, more preferably from 70 to 95 weight-% of the composite material Me consist of the organic polymeric matrix and the fiber component.The process of any one of embodiments 1 to 13 wherein the composite material Me further comprises one or more of balsa wood and polyethylene terephthalate foam.The process of embodiment 14, wherein from 0.5 to 20 weight-%, preferably from 0.7 to 15 weight-%, more preferably of from 0.9 to 10 weight-%, more preferably of from 1 to 8 weight-% of the composite material Me consist of the one or more of balsa wood and polyethylene terephthalate foam.The process of embodiment 14 or 15, wherein from 70 to 100 weight-%, preferably from 75 to 98 weight-%, more preferably from 80 to 95 wt.-% of the composite material Me consist of the polymeric matrix, the fiber component, and the one or more of balsa wood and polyethylene terephthalate foam.The process of any one of embodiments 1 to 16, wherein at most 0.1 weight-%, preferably at most 0.05 weight-%, more preferably at most 0.01 weight-% of the composite material Me consist of polyvinylchloride.The process of any one of embodiments 1 to 17, wherein the composite material Me is selected from the group consisting of one or more parts of an air plane, one or more part of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade.The process of any one of embodiments 1 to 18, wherein the composite material Me is in the form of particles exhibiting an average length in the range of from 0.1 cm to 3 m, preferably in the range of from 0.5 cm to 50 cm, more preferably in the range of from 1 cm to 3 cm.The process of any one of embodiments 1 to 19, wherein the hydrolysis oil comprised in the partial oxidation feed stream SPOX is obtainable or obtained by a process comprisinga) providing the composite material Me;p.1 ) subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor.The process of any one of embodiments 1 to 20, wherein providing the partial oxidation feed stream SPOX according to a) comprises preparing the hydrolysis oil comprised in SPOX, comprisinga) providing the composite material Me;p.1 ) subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor.The process of any one of embodiments 20 and 21 , wherein subjecting the composite material Me to hydrolysis conditions in the hydrolysis reactor comprise introducing the composite material Me and water into the hydrolysis reactor at a weight ratio of water relative to composite material in the range of from 10:1 to 0.1:1, preferably in the range of from 5:1 to 0.2:1, more preferably in the range of from 2.5:1 to 0.3:1.The process of any one of embodiments 20 to 22, wherein the hydrolysis reactor is a closed reactor, preferably an autoclave, the hydrolysis preferably being carried out under autogenous pressure, preferably the vapor pressure of the water in the hydrolysis reactor.The process of any one of embodiments 20 to 23, wherein the hydrolysis conditions comprise a temperature in the hydrolysis reactor in the range of from 220 to 320 °C, preferably in the range of from 230 to 300 °C, more preferably in the range of from 240 to 290 °C.The process of any one of embodiments 20 to 24, wherein the hydrolysis conditions comprise a hydrolysis time in the range of from 10 to 600 min, preferably in the range of from 10 to 300 min, more preferably in the range of from 10 to 180 min, more preferably in the range of from 10 to 120 min.The process of any one of embodiments 20 to 25, wherein p.1) comprises subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor, obtaining a hydrolysis product comprising an aqueous phase, a fiber component and a solid polymeric hydrolysis product, the process further comprising p.2) separating the aqueous phase from the fiber component and the polymeric hydrolysis product; p.3) contacting the fiber component and the solid polymeric hydrolysis product separated according to p.2) with a solvent, thereby dissolving the polymeric hydrolysis product in said solvent, obtaining a mixture comprising the polymeric hydrolysis product dissolved in the solvent and further comprising the fiber component;p.4) separating the fiber component from the mixture obtained according to p.3), obtaining a solution of the polymeric hydrolysis product;p.5) separating solvent from the solution obtained according to p.4), obtaining the hydrolysis oil.The process of embodiment 26, wherein separating the aqueous phase according to p.2) comprises one or more of filtration, centrifugation and decantation.The process of embodiment 26 or 27, wherein separating the aqueous phase according to p.2) is carried out at a temperature of the hydrolysis product in the range of from 5 to 80 °C, preferably in the range of from 15 to 60 °C, more preferably in the range of from 20 to 30 °C.The process of any one of embodiments 26 to 28, wherein the solvent according to p.3) is selected from the group consisting of ethers, monoalcohols, glycols, esters, acids, ketones, amides, and mixture of two or more thereof.The process of any one of embodiments 26 to 29, wherein the solvent according to p.3) is selected from the group consisting of tetrahydrofuran, dioxane, tert-butyl methyl ether, cyclopentyl methyl ether, methanol, ethanol, 1 -propanol, 2-propanol, butanols, monoethylene glycol, diethylene glycol, ethyl acetate, propyl acetate, butyl acetate, gamma-valerolactone, epsilon-caprolactone, formic acid, acetic acid, propionic acid, acetone, methyl ethyl ketone, cyclohexanone, formamide, dimethylformamide, N-alkylpyrrolidones such as N- methylpyrrolidone, or N-butylpyrrolidone, epsilon-caprolactam, sulfolane, one or more suitable solvents from waste streams intended for combustion, and mixtures of two or more thereof, preferably selected from the group consisting of methanol, ethanol, 1-propanol, 2-propanol, butanols, monoethylene glycol, diethylene glycol, and mixtures of two or more thereof.The process of any one of embodiments 26 to 30, wherein according to p.3), the fiber component and the solid polymeric hydrolysis product are brought in contact with the solvent at the boiling point of the solvent, preferably at a pressure in the range of from 0.9 to 3 bar(abs), more preferably in the range of from 0.95 to 2 bar(abs).The process of any one of embodiments 26 to 31 , further comprising subjecting the fiber component separated according to p.4), optionally after removal of water and / or solvent from the fiber component, to suitable re-use, preferably for preparing an engineering plastics materials, more preferably for preparing an engineering plastics material comprising one or more of polyamide 6 and polyamide 6.6.The process of any one of embodiments 26 to 32, wherein the hydrolysis oil obtained according to p.5) exhibits, at a temperature of the hydrolysis oil of 90 °C, a viscosity in the range of from 10 to 107mPa*s, preferably in the range of from 10 to 105mPa*s, more preferably in the range of from 10 to 104mPa*s.The process of any one of embodiments 26 to 33, wherein the weight-% ratio of nitrogen comprised in the hydrolysis oil obtained according to p.5) relative to organic nitrogen comprised in the composite material fromwhich said hydrolysis oil is prepared, in each case calculated as elemental N, is at most 0.9:1, preferably at most 0.8:1, more preferably at most 0.7:1, more preferably at most 0.6:1.The process of any one of embodiments 26 to 34, wherein the hydrolysis oil obtained according to p.5) exhibits at least one, preferably at least two, more preferably at least three, more preferably at least four, more preferably all of the following features (i) to (v):(i) a carbon content, calculated as elemental C, in the range of from 55 to 80 weight-%;(ii) a hydrogen content, calculated as elemental H, in the range of from 5 to 15 weight-%;(iii) an oxygen content, calculated as elemental O, in the range of from 12 to 25 weight-%;(iv) a nitrogen content, calculated as elemental N, in the range of from 12 to 25 weight-%;(v) a sulphur content, calculated as elemental S, in the range of from 0 to 1 weight-%;in each case based on the total weight of the hydrolysis oil.The process of any one of embodiments 26 to 35, wherein the fiber component content of the hydrolysis oil obtained according to p.5) is in the range of from 0 to 1 weight-%, preferably in the range of from 0 to 0.1 weight-%, more preferably in the range of from 0 to 0.05 weight-%, more preferably in the range of from 0 to 0.01 weight-%, based on the total weight of the hydrolysis oil.The process of any one of embodiments 1 or 36, wherein in addition to the hydrolysis oil, the partial oxidation feed stream SPOX further comprises a further component selected from the group consisting of one or more non-gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof, wherein said further component preferably exhibits at least one, more preferably at least two, more preferably at least three, more preferably, more preferably all of the following features:(I') a heating value of at least 20,000 J / g, preferably in the range of from 20,000 to 50,000 J / g, more preferably in the range of from 25,000 to 45,000 J / g, more preferably in the range of from 30,000 to 40,000 J / g, the heating value being measured in accordance with DIN 51900;(II') a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(I I'.1 ) a carbon content, calculated as elemental C, of at least 55 weight-%, preferably in the range of from 55 to 97 weight-%, more preferably in the range of from 70 to 94 weight-%;(I l'.2) an oxygen content, calculated as elemental O, of at most 40 weight-%, preferably in the in the range of from 0 to 40 weight-%, more preferably in the range of from 2 to 25 weight-%;(I l'.3) a nitrogen content, calculated as elemental N, in the range of at most 4 weight-%, preferably in the range of from 0 to 4 weight-%, more preferably in the range of from 0.005 to 2 weight-%; in each case based on the total weight of the respective component.The process of embodiment, wherein the one or more non-gaseous organic components preferably exhibit the further feature (III'):(III') a viscosity in the range of from 1 to 10 mPa»s, as measured at 40 °C in accordance with DIN 53019.39. The process of embodiment 37 or 38, wherein the one or more non-gaseous organic components are selected from the group consisting of bio oils, pyrolysis oils from pyrolysis of biomass, pyrolysis oils from pyrolysis of plastic waste, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphaltene fractions, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, industrial waste streams, coal dusts, and mixtures of two or more thereof.40. The process of any one of embodiments 37 to 39, wherein the one or more gaseous organic components are selected from the group consisting of natural gas, biogas, cracker fuel gas, and mixtures of two or more thereof.41. The process of any one of embodiments 1 to 40, wherein from 50 to 100 weight-%, preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-% of the partial oxidation feed stream SPOX consist of the hydrolysis oil and optionally the further component selected from the group consisting of one or more non-gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof.42. The process of any one of embodiments 1 to 41 , wherein the stream SPOX exhibits at least one, preferably at least two, more preferably all of the following five features (I) to (III):(I) a heating value in the range of from 20,000 to 46,000 J / g, preferably of from 35,400 to 45,300 J / g, more preferably of from 37,000 to 42,000 J / g, as measured in accordance with DIN 51900; (II) an ash content in the range of from 0 to 17,000 mg / kg, as measured in accordance with ISO 6245; (III) a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(111.1) a carbon content, calculated as elemental C, in the range of from 60 to 99 weight-%, preferably in the range of from 70 to 96 weight-%;(111.2) a hydrogen content, calculated as elemental H, in the range of from 1 to 15 weight-%, preferably in the range of from 2 to 10 weight-%;(111.3) an oxygen content, calculated as elemental O, in the range of from 0 to 25 weight-%, preferably in the range of from 1 to 20 weight-%;(111.4) a sulphur content, calculated as elemental S, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;(111.5) a nitrogen content, calculated as elemental N, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;in each case based on the total weight of the component C, wherein the sum of the amounts of carbon (C), hydrogen (H), oxygen (O), sulphur (S), and nitrogen (N) in the stream SPOX is in the range of from70 to 100 weigh-%, preferably of from 80 to 99.9 weight-%, more preferably of from 90 to 99.5 weight- %, more preferably of from 95 to 99.5 weight-%, based on the weight of the component C.The process of any one of embodiments 1 to 42, wherein prior to being subjected to partial oxidation according to b), the partial oxidation feed stream SPOX is not subjected to hydrotreatment.The process of any one of embodiments 1 to 43, wherein the partial oxidation conditions according to b) comprise a temperature in the reactor in the range of from 400 to 2000 °C, preferably in the range of from 1000 to 1750 °C, more preferably in the range of from 1250 to 1500 °C.The process of any one of embodiments 1 to 44, wherein the partial oxidation conditions according to b) comprise a pressure in the reactor in the range of from 1 to 200 bar(abs), preferably in the range of from 5 to 150 bar(abs), more preferably in the range of from 10 to 100 bar(abs), more preferably in the range of from 11 to 50 bar(abs).The process of any one of embodiments 1 to 45, wherein subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) comprises introducing the partial oxidation feed stream SPOX and oxygen (O2) into the reactor at a weight ratio of O2 relative to SPOX in the range from 0.4: 1 to 1.3: 1 , preferably in the range of from 0.6:1 to 1.25:1, more preferably in the range of from 0.7 to 1.2:1.The process of any one of embodiments 1 to 46, wherein subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) further comprises introducing steam into the reactor, preferably at a weight ratio of steam relative to SPOX of at least 0.2: 1 , more preferably in the range of from 0.2:1 to 2:1, more preferably in the range of from 0.3:1 to 2:1, more preferably in the range of from 0.4:1 to 1.5:1, more preferably in the range of from 0.4:1 to 1:1.The process of any one of embodiments 1 to 47, further comprisingc) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprisingCO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2’.The process of embodiment 48, wherein c) comprisesc-1) subjecting the stream S1 obtained according to b) to a washing step in a washing unit, obtaining a stream ST depleted in particulate solid compared to S1 and comprising CO, H2, CO2, H2O, CH4, and optionally H2S;c-2) subjecting the stream ST obtained according to c-1) to a drying step in a drying unit, obtaining a stream ST' depleted in H2O compared to S1 and ST;c-3) subjecting the stream ST' obtained according to c-2) to an acid gas removal step in a CO2 / H2S adsorption unit, obtaining the stream S2.The process of embodiment 48 or 49, comprisingd) changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;wherein d) comprisespassing and contacting water with S2 obtained according to c) into a reaction unit for a water gas shift reaction, obtaining a stream S2' depleted in CO compared to S2 and comprising CO, H2, CH4 and CO2, optionally followed by passing S2' into an acid gas removal unit, obtaining a stream S2' depleted in CO2 and comprising CO, H2 and CH4; orpassing and contacting CO2 with S2 obtained according to c) into a reaction unit for a reverse water gas shift reaction, obtaining a stream S2' enriched in CO compared to S2 and comprising CO, H2, CH4 and H2O; oradding H2 to S2 obtained according to c), obtaining a stream S2' enriched in H2 compared to S2 and comprising CO, H2 and CH4, wherein at least a portion of the added H2 is H2 from a renewable source.The process of any one of embodiments 48 to 50, wherein e) comprises subjecting S2 or S2' to cryogenic separation, obtaining S3, S4 and preferably a gas stream S5 comprising CH4 and being depleted in CO and H2 compared to S2, optionally S2’.The process of any one of embodiment 48 to 51 , comprisingf) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products;and / ora chemical conversion process, comprising preparing carbon monoxide and molecular hydrogen by a process according to any of embodiments 48 to 51 and further comprisingf) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products.53. The process of embodiment 52, wherein f) comprisesf-1) bringing in contact CO comprised in S3 with methanol and subjecting CO and methanol to a chemical conversion, obtaining a stream S6 comprising a first chemical product being methyl formate;f-2) optionally bringing in contact at least a portion of S6 obtained according to f-1) with ammonia and subjecting said portion of S6 and ammonia to a chemical conversion, obtaining a stream S8 comprising methanol and a second chemical product being formamide;f-3) optionally separating formamide from methanol comprised in S7 obtained according to f-2) and optionally recycling methanol to f-1), obtaining a stream S7' being depleted in methanol compared to S7 and comprising formamide;f-4) optionally subjecting at least a portion of S7 obtained according to f-2) or at least a portion of S7' obtained according to f-3) to a thermal decomposition and subsequent water removal, obtaining a stream S8 comprising a third chemical compound being hydrogen cyanide.54. The process of embodiment 53, wherein f) further comprisesf-5) bringing in contact at least a portion of S8 obtained according to f-4) with isophorone and subjecting to a chemical conversion, being a Michael addition reaction, obtaining a stream S9 comprising isophorone nitrile;f-6) optionally subjecting at least a portion of S9 obtained according to f-5) to hydrogenation, preferably using H2 obtained in accordance with e), in the presence of ammonia, obtaining a stream P comprising a chemical product being isophorone diamine.55. The process of any one of embodiments 52 to 54, wherein f) comprises subjecting a mixture of CO obtained according to e) and H2 obtained according to e) to a chemical conversion in the presence of a heterogeneous catalyst, obtaining a chemical product being methanol.56. The process of embodiment 55, wherein f) further comprises subjecting at least a portion of the obtained methanol to a partial oxidation reaction, obtaining a chemical product being formaldehyde.57. The process of embodiment 56, wherein f) further comprises subjecting at least a portion of the obtained formaldehyde to a chemical conversion, being a Reppe reaction, with acetylene, obtaining a chemical product being 1 ,4-butyndiole, and optionally subjecting at least a portion of the obtained 1 ,4-butyndiole to hydrogenation, preferably using H2 obtained according to e), obtaining a chemical product being 1,4-butanediole, and optionally subjecting at least a portion of the obtained 1 ,4-butandiole to a chemical conversion with epichlorohydrin, obtaining a chemical product being 1 ,4-butanediol-diglycidylether.The process of any one of embodiments 52 to 57, wherein f) comprises subjecting a polyether alcohol to a chemical conversion with ammonia in the presence of H2 obtained according to e) and further in the presence of a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being a polyether amine.The process of embodiment 58, wherein the polyether alcohol is selected from the group consisting of polypropylene glycols, polyethylene glycols and polypropylene ethylene glycol copolymers, said polyether alcohol being obtainable or obtained by a process comprising subjecting ethylene and / or propylene to a partial oxidation, obtaining ethylene oxide and / or propylene oxide, and subjecting the obtained ethylene oxide and / or propylene oxide to a polymerization reaction, obtaining the respective polyether alcohol, wherein f) comprises subjecting a mixture of CO and H2, CO and / or H2, preferably CO and H2, being obtained according to e), to a Fischer-Tropsch synthesis, obtaining a mixture of hydrocarbons, and subjecting the obtained mixture of hydrocarbons to one or more separation steps, obtaining chemical products being one or more alkenes, preferably one or more of ethylene and propylene.The process of embodiment 58 or 59, wherein the polyether alcohol is a polypropylene glycol having a number average molecular weight in the range from 200 to 3000 g / mol, preferably in the range from 210 to 2100 g / mol, more preferably in the range from 210 to 500 g / mol.A recycling process for providing a hydrolysis oil and optionally a pyrolysis oil, comprising providing a material comprising a chemical product manufactured according to the process of any one of embodiments 52 to 60; subjecting the material to a shredding step or a sequence of shredding steps to obtain a shredded material; and subjecting the shredded material to hydrolysis to obtain the hydrolysis oil and optionally to pyrolysis to obtain the pyrolysis oil.A process for recycling a composite material, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a first composite material Mei comprising an organic polymeric matrix and a fiber component, wherein the organic polymeric matrix comprised in the composite material Mei comprises preferably at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups, wherein the organic polymeric matrix comprised in the composite material Me is more preferably selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin;b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally H2S;c) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprising CO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2';f) preparing a second composite material Mc2, comprisingsubjecting at least a portion of S3 comprising CO obtained according to e) and / or at least a portion of S4 comprising H2 obtained according to e) to a sequence of chemical conversions, obtaining one or more precursors of the second composite material Mc2;reacting the one or more precursors with a fiber component, obtaining the second composite material Mc2.A process, preferably according to any one of embodiments 1 to 60, comprising the step of converting a chemical material obtainable or obtained by the process according to any one of embodiments 1 to 60 to obtain a product Q.The process of embodiment 63, wherein the product Q is selected from:building block or monomer; orpolymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orindustrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; oraqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; orpolymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.65. The process of embodiment 63 or 64,wherein the content of the chemical material in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight- % or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the chemical material in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight- % or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.It is explicitly noted that the above 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 is not the set of claims of the present invention.In the context of the present invention, a term "X is one or more of A, B and C”, wherein X is a given feature and each of A, B and C stands for specific realization of said feature, is to be understood as disclosing that X is either A, or B, or C, or A and B, or A and C, or B and C, or A and B and C. In this regard, it is noted that the skilled person is capable of transfer to above abstract term to a concrete example, e.g. where X is a chemical element and A, B and C are concrete elements such as Li, Na, and K, or X is a temperature and A, B and C are concrete temperatures such as 10 °C, 20 °C, and 30 °C. In this regard, it is further noted that the skilled person is capable of extending the above term to less specific realizations of said feature, e.g. "X is one or more of A and B” disclosing that X is either A, or B, or A and B, or to more specific realizations of said feature, e.g. "X is one or more of A, B, C and D”, disclosing that X is either A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D.The present invention is further illustrated by the following examples.ExamplesReference ExampleThe CHNO analyses according to the examples were carried out as follows:CHN analysis: The respective sample (1 - 10 mg) was combusted in a helium / oxygen atmosphere on a CuO catalyst and the formed NOx was subsequently reduced to N2 on a Cu contact. After separation of the combustion gases, nitrogen was determined as N2, carbon as CO2 and hydrogen as H2O and then calculated as elements (values in the tables of the examples below). The detection and quantification was done via thermal conductivity. Analyzer: Elementar, model Vario EL Cube.0 analysis: The respective sample (1 - 10 mg) was pyrolysed / reduced in a forming gas (5 vol.-% H2 in N2) atmosphere on a soot contact, the oxygen was converted hereby to carbon monoxide (CO). The carbon monoxide was detected and quantified via IR spectrometry. Analyzer: Elementar, model rapid OXY cube.Example 1 : Step a)60 g of epoxy composite containing material containing glass fibers (taken from the root of an end-of-life wind blade from which other components were mechanically visually separated, followed by shredding in a pin mill) were treated with 150 g of water in a 250 ml autoclave vessel and heated to 280 °C. The autoclave was maintained at this temperature for two hours, during which a pressure of 68 bar was established, and then cooled to room temperature. A slurry of glass fibers mixed with clumps of organic material and water was obtained. The water was filtered / decanted, and the residue was first washed three times with 150 ml of methanol each and then three times with 50 ml of THE each. The solvents of the organic phases and the aqueous phase were removed in a rotary evaporator, and the glass fibers were dried in a vacuum. The following yields were obtained:Table 1Yields according to Example 1The person skilled in the art will recognize that the organic material can also be extracted directly with refluxing THF without methanol. Other solvents such as ethanol, acetone, ethyl acetate, dioxane, tert-butyl methyl ether can also be used instead of THF.Example 2: Step a)60 g shredded epoxy composite material (the same material as used for example 1) were treated with 60 g of water for 2 h at 280 °C using a 250 ml autoclave. A pressure of 62 bar was observed. The resulting mixture from the autoclave was taken out and residues were washed out with 5 ml of water and with 90 ml of ethanol. The resulting mixture was given into a Soxhlett extraction sleeve and 500 ml of ethanol were added. A soxhlett extraction was carried out. After 4 extractions the resulting solution was colorless and the process was stopped. The liquids were evaporated and 19.1 g brown oil was received as one fraction and 39.5 g of glass fibers (after drying under vacuum) as solid fraction. A CHNO analysis of the oil showed the following results:Table 2Composition according to Example 2Example 3: Partial oxidationThe partial oxidation step b) according to the present invention and further downstream stages are illustrated by simulations performed via the flow sheet simulation platform Aspen Plus V14.0. The seven examples as shown in the following Table 3 illustrate a one-step entrained flow gasification process, converting a feed stream A1 consisting of one or two liquid feedstocks (an oil refinery residue and a hydrolysis oil) into synthesis gas. The entrained flow gasifier is fed with the feed stream in various weighted mass ratios with comprising specifics A at 47 bar(abs) and100 °C. Additionally, gasification agents are injected into the entrained flow gasifier, enabling the gasification reaction at the given temperature E. The gasification agents are steam with a given mass flow ratio C at 47 bar(abs) and 400 °C, as well as an oxygen mass ratio B at 25 °C and 47 bar(abs). The resulting high-temperature synthesis gas, comprising CO, H2O, CO2, H2, CH4 and N2, is washed with water and dried in order to reduce the amount of ash and tars. The raw synthesis gas exits the washing and drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine wash, is used to separate acids like CO2 and H2S. The mass and molar ratios of H2, CO, H2S, CO2 and N2 are given in Table 4 below.Table 3Results according to Example 3Table 4Mass and molar ratios according to Example 3The following definitions and abbreviations are used:Syngas defined as: metric tonnes of H2 + metric tonnes of CO in the synthesis gasA1 : feed ratio oil refinery residue : hydrolysis oil in wt-% and elemental analysis of the feed stream in wt-% A2: feed ratio in t(feed) I t(syngas)B: pure oxygen ratio in t(oxygen) 11 (syngas)C: steam ratio in t(steam) 11 (syngas)D: pressure at gasifier outlet in barE: temperature at the gasifier outlet in °CF: CO2 produced in t(C02) I t(syngas)G: H2 / CO molar ratio in mol(H2) I mol(CO)H: H2 ratio in t(H2) I t(syngas)I: CO ratio in t(CO) I t(syngas)J: CH4 ratio in t(CH4) I t(syngas)K: H2S ratio in t(H2S) I t(syngas)L: N2 ratio in t(N2) I t(syngas)Comparative Example: Two-step gasification processThe process according to the comparative example is illustrated by simulations performed via the flow sheet simulation platform Aspen Plus V14.0.The comparing example shows a two-step gasification process, comprising a fluidized bed gasification as first step, followed by a high temperature entrained flow gasifier as a second step. This two-step gasification process is converting a solid feed stream consisting of sorted glass fiber shredder residue into synthesis gas. Therefore, the fluidized bed gasifier is fed with the feed stream at 3.8 bar and 35 °C, which the following specification: Carbon 50.4 wt-%, Hydrogen 6.3 wt-%, Oxygen 37.5 wt-%, Nitrogen 2.9 wt-% and ash 2.3 wt-%. Additionally, gasification agents are injected into the fluidized bed gasifier, enabling the gasification reaction at the given temperature E of 800 °C. The gasification agents are steam with a given mass flow ratio C at 5.4 bar and 180 °C, as well as an oxygen mass ratio B at 20 °C and 5 bar. The raw synthesis gas is injected into the entrained flow gasifier and further heated up to a temperature E4 of 1350 °C at a pressure E3 of 3 bar. Therefore, additional oxygen is needed in a mass ratio of E2 at 20 °C and 5 bar. The resulting high-temperature synthesis gas, comprising CO, H2O, CO2, H2, CH4 and N2, is washed with water and dried in order to reduce the amount of ash and tars. The raw synthesis gas exits the washing and drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine wash, is used to separate acids like CO2 and H2S. The mass and molar ratios of H2, CO, H2S, CO2 and N2 are given in Table 5 below:Table 5Mass and molar ratios according to the Comparative Example

Claims

Claims1. A process for preparing carbon monoxide and molecular hydrogen, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a composite material Me, the composite material Me comprising an organic polymeric matrix and a fiber component;b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally one or more of H2S and at least one nitrogen compound;wherein providing the partial oxidation feed stream SPOX according to a) comprises preparing the hydrolysis oil comprised in SPOX, comprisinga) providing the composite material Me;|3.1 ) subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor;wherein p.1) comprises subjecting the composite material Me to hydrolysis conditions in a hydrolysis reactor, obtaining a hydrolysis product comprising an aqueous phase, a fiber component and a solid polymeric hydrolysis product;the process further comprisingp.2) separating the aqueous phase from the fiber component and the polymeric hydrolysis product; p.3) contacting the fiber component and the solid polymeric hydrolysis product separated according to p.2) with a solvent, thereby dissolving the polymeric hydrolysis product in said solvent, obtaining a mixture comprising the polymeric hydrolysis product dissolved in the solvent and further comprising the fiber component;p.4) separating the fiber component from the mixture obtained according to p.3), obtaining a solution of the polymeric hydrolysis product;p.5) separating solvent from the solution obtained according to p.4), obtaining the hydrolysis oil; wherein the hydrolysis reactor is a closed reactor;wherein the hydrolysis conditions comprise a temperature in the hydrolysis reactor in the range of from 220 to 290 °C.

2. The process of claim 1 , wherein the organic polymeric matrix comprised in the composite material Me comprises at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups, wherein the organic polymeric matrix comprised in the composite material Me is preferably selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin; andwherein the fiber component comprised in the composite material Me is selected from the group consisting of glass fibers, carbon fibers, aramid fibers, natural fibers, basalt fibers ceramic fibers and mixtures thereof, preferably selected from the group consisting of glass fibers, carbon fibers, aramid fibers, basalt fibers and mixtures thereof, more preferably selected from the group consisting of glass fibers, carbon fibers and mixtures of two or more thereof;wherein preferably from 20 to 89 weight-%, more preferably from 25 to 79 weight-%, more preferably from 30 to 70 weight-%, more preferably from 40 to 60 weight-% of the composite material Me consist of the fiber component; and wherein preferably from 60 to 100 weight-%, more preferably from 65 to 98 weight-%, more preferably from 70 to 95 weight-% of the composite material Me consist of the organic polymeric matrix and the fiber component.

3. The process of claim 1 or 2, wherein the composite material Me is selected from the group consisting of one or more parts of an air plane, one or more part of a car, one or more parts of a ship, one or more parts of a wind turbine blade, and a mixture of two or more thereof, preferably from the group consisting of one or more end-of-life parts of an air plane, one or more end-of-life parts of a car, one or more end-of-life parts of a ship, one or more end-of-life parts of a wind turbine blade, and a mixture of two or more thereof, wherein more preferably, the composite material comprises, more preferably consists of one or more parts of an end-of-life wind turbine blade.

4. The process of any one of claims 1 to 3,wherein subjecting the composite material Me to hydrolysis conditions in the hydrolysis reactor comprises introducing the composite material Me and water into the hydrolysis reactor at a weight ratio of water relative to composite material in the range of from 10:1 to 0.1:1, preferably in the range of from 5:1 to 0.2:1, more preferably in the range of from 2.5:1 to 0.3:1;wherein the hydrolysis reactor is an autoclave, the hydrolysis preferably being carried out under autogenous pressure in the hydrolysis reactor;wherein the hydrolysis conditions comprise a temperature in the hydrolysis reactor in the range of from 230 to 290 °C, preferably in the range of from 240 to 290 °C.

5. The process of claim 4,wherein separating the aqueous phase according to p.2) comprises one or more of filtration, centrifugation and decantation;wherein separating the aqueous phase according to p.2) is carried out at a temperature of the hydrolysis product in the range of from 5 to 80 °C, preferably in the range of from 15 to 60 °C, more preferably in the range of from 20 to 30 °C;wherein the solvent according to p.3) is selected from the group consisting of ethers, monoalcohols, glycols, esters, acids, ketones, amides, and mixture of two or more thereof.

6. The process of claim 5, wherein the hydrolysis oil obtained according to p.5) exhibits at least one, preferably at least two, more preferably at least three, more preferably at least four, more preferably all of the following features (i) to (v):(i) a carbon content, calculated as elemental C, in the range of from 55 to 80 weight-%;(ii) a hydrogen content, calculated as elemental H, in the range of from 5 to 15 weight-%;(iii) an oxygen content, calculated as elemental 0, in the range of from 12 to 25 weight-%;(iv) a nitrogen content, calculated as elemental N, in the range of from 12 to 25 weight-%;(v) a sulphur content, calculated as elemental S, in the range of from 0 to 1 weight-%;in each case based on the total weight of the hydrolysis oil.

7. The process of any one of claims 1 to 6, wherein in addition to the hydrolysis oil, the partial oxidation feed stream SPOX further comprises a further component selected from the group consisting of one or more non- gaseous organic components, one or more gaseous organic components, and a mixture of two or more thereof, wherein said further component preferably exhibits at least one, more preferably at least two, more preferably at least three, more preferably, more preferably all of the following features:(I') a heating value of at least 20,000 J / g, preferably in the range of from 20,000 to 50,000 J / g, more preferably in the range of from 25,000 to 45,000 J / g, more preferably in the range of from 30,000 to 40,000 J / g, the heating value being measured in accordance with DIN 51900;(II’) a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(I I'.1 ) a carbon content, calculated as elemental C, of at least 55 weight-%, preferably in the range of from 55 to 97 weight-%, more preferably in the range of from 70 to 94 weight-%;(I I'.2) an oxygen content, calculated as elemental O, of at most 40 weight-%, preferably in the in the range of from 0 to 40 weight-%, more preferably in the range of from 2 to 25 weight-%;(I I'.3) a nitrogen content, calculated as elemental N, in the range of at most 4 weight-%, preferably in the range of from 0 to 4 weight-%, more preferably in the range of from 0.005 to 2 weight-%; in each case based on the total weight of the respective component;wherein the one or more non-gaseous organic components are preferably selected from the group consisting of bio oils, pyrolysis oils from pyrolysis of biomass, pyrolysis oils from pyrolysis of plastic waste, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphaltene fractions, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, industrial waste streams, coal dusts, and mixtures of two or more thereof;wherein the one or more gaseous organic components are preferably selected from the group consisting of natural gas, biogas, cracker fuel gas, and mixtures of two or more thereof.

8. The process of any one of claims 1 to 7, wherein the stream SPOX exhibits at least one, preferably at least two, more preferably all of the following five features (I) to (III):(I) a heating value in the range of from 20,000 to 46,000 J / g, preferably of from 35,400 to 45,300 J / g, more preferably of from 37,000 to 42,000 J / g, as measured in accordance with DIN 51900; (II) an ash content in the range of from 0 to 17,000 mg / kg, as measured in accordance with ISO 6245; (III) a content of carbon, hydrogen, oxygen, sulphur and nitrogen as follows:(111.1) a carbon content, calculated as elemental C, in the range of from 60 to 99 weight-%, preferably in the range of from 70 to 96 weight-%;(111.2) a hydrogen content, calculated as elemental H, in the range of from 1 to 15 weight-%, preferably in the range of from 2 to 10 weight-%;(111.3) an oxygen content, calculated as elemental O, in the range of from 0 to 25 weight-%, preferably in the range of from 1 to 20 weight-%;(111.4) a sulphur content, calculated as elemental S, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;(111.5) a nitrogen content, calculated as elemental N, in the range of from 0 to 5 weight-%, preferably in the range of from 0.005 to 4 weight-%;in each case based on the total weight of the component C, wherein the sum of the amounts of carbon (C), hydrogen (H), oxygen (O), sulphur (S), and nitrogen (N) in the stream SPOX is in the range of from 70 to 100 weigh-%, preferably of from 80 to 99.9 weight-%, more preferably of from 90 to 99.5 weight- %, more preferably of from 95 to 99.5 weight-%, based on the weight of the component C.

9. The process of any one of claims 1 to 8, wherein the partial oxidation conditions according to b) comprise a temperature in the reactor in the range of from 400 to 2000 °C, preferably in the range of from 1000 to 1750 °C, more preferably in the range of from 1250 to 1500 °C;wherein the partial oxidation conditions according to b) preferably comprise a pressure in the reactor in the range of from 1 to 200 bar(abs), more preferably in the range of from 5 to 150 bar(abs), more preferably in the range of from 10 to 100 bar(abs), more preferably in the range of from 11 to 50 bar(abs).

10. The process of any one of claims 1 to 9, wherein subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) comprises introducing the partial oxidation feed stream SPOX and oxygen (O2) into the reactor at a weight ratio of O2 relative to SPOX in the range from 0.4:1 to 1.3:1, preferably in the range of from 0.6:1 to 1.25:1, more preferably in the range of from 0.7 to 1.2:1;wherein subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor according to b) preferably further comprises introducing steam into the reactor, more preferably at a weight ratio of steam relative to SPOX of at least 0.2:1, more preferably in the range of from 0.2:1 to 2:1, more preferably in the range of from 0.3:1 to 2:1, more preferably in the range of from 0.4:1 to 1.5:1, more preferably in the range of from 0.4:1 to 1:1.

11. The process of any one of claims 1 to 10, further comprisingc) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprising CO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2’.

12. The process of claim 11 , comprisingf) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products;and / ora chemical conversion process, comprising preparing carbon monoxide (CO) and molecular hydrogen (H2) by a process according to claim 11 and further comprisingf) subjecting one or more of at least a portion of S3 obtained according to e) and at least a portion of S4 obtained according to e) to chemical conversion or sequence of chemical conversions, obtaining one or more chemical products.

13. The process of claim 12,• wherein f) comprisesf-1) bringing in contact CO comprised in S3 with methanol and subjecting CO and methanol to a chemical conversion, obtaining a stream S6 comprising a first chemical product being methyl formate;f-2) optionally bringing in contact at least a portion of S6 obtained according to f-1) with ammonia and subjecting said portion of S6 and ammonia to a chemical conversion, obtaining a stream S8 comprising methanol and a second chemical product being formamide;f-3) optionally separating formamide from methanol comprised in S7 obtained according to f-2) and optionally recycling methanol to f-1), obtaining a stream S7' being depleted in methanol compared to S7 and comprising formamide;f-4) optionally subjecting at least a portion of S7 obtained according to f-2) or at least a portion of S7' obtained according to f-3) to a thermal decomposition and subsequent water removal, obtaining a stream S8 comprising a third chemical compound being hydrogen cyanide; wherein f) preferably further comprisesf-5) bringing in contact at least a portion of S8 obtained according to f-4) with isophorone and subjecting to a chemical conversion, being a Michael addition reaction, obtaining a stream S9 comprising isophorone nitrile;f-6) optionally subjecting at least a portion of S9 obtained according to f-5) to hydrogenation, preferably using H2 obtained in accordance with e), in the presence of ammonia, obtaining a stream P comprising a chemical product being isophorone diamine;and / or• wherein f) comprises subjecting a mixture of CO obtained according to e) and H2 obtained according to e) to a chemical conversion in the presence of a heterogeneous catalyst, obtaining a chemical product being methanol, wherein f) preferably further comprises subjecting at least a portion of the obtained methanol to a partial oxidation reaction, obtaining a chemical product being formaldehyde, and wherein more preferably, f) further comprises subjecting at least a portion of the obtained formaldehyde to a chemical conversion, being a Reppe reaction, with acetylene, obtaining a chemical product being 1,4- butyndiole, and optionally subjecting at least a portion of the obtained 1 ,4-butyndiole to hydrogenation, preferably using H2 obtained according to e), obtaining a chemical product being 1 ,4-butanediole, and optionally subjecting at least a portion of the obtained 1 ,4-butandiole to a chemical conversion with epichlorohydrin, obtaining a chemical product being 1 ,4-butanediol-diglycidylether;and / or• wherein f) comprises subjecting a polyether alcohol to a chemical conversion with ammonia in the presence of H2 obtained according to e) and further in the presence of a catalyst, preferably a heterogeneous catalyst, obtaining a chemical product being a polyether amine, wherein the polyether alcohol is preferably selected from the group consisting of polypropylene glycols, polyethylene glycols and polypropylene ethylene glycol copolymers, said polyether alcohol being obtainable or obtained by a process comprising subjecting ethylene and / or propylene to a partial oxidation, obtaining ethylene oxide and / or propylene oxide, and subjecting the obtained ethylene oxide and / or propylene oxide to a polymerization reaction, obtaining the respective polyether alcohol, wherein f) preferably comprises subjecting a mixture of CO and H2, CO and / or H2, preferably CO and H2, being obtained according to e), to a Fischer-Tropsch synthesis, obtaining a mixture of hydrocarbons, and subjecting the obtained mixture of hydrocarbons to one or more separation steps, obtaining chemical products being one or more alkenes, preferably one or more of ethylene and propylene.

14. A process for recycling a composite material, comprisinga) providing a partial oxidation feed stream SPOX comprising a hydrolysis oil from hydrolysis of a first composite material Mei comprising an organic polymeric matrix and a fiber component, wherein the organic polymeric matrix comprised in the composite material Mei comprises preferably at least one of ether groups, ester groups, hydroxy groups, secondary amine groups and tertiary amine groups, wherein the organic polymeric matrix comprised in the composite material Me is more preferably selected from the group consisting of cured epoxy resins, unsaturated polyester resins and mixtures thereof, more preferably from the group consisting of cured epoxy resins and unsaturated polyester resins, wherein more preferably, the polymeric matrix comprised in the composite material comprises, more preferably is a cured epoxy resin;b) subjecting the stream SPOX to partial oxidation conditions in a partial oxidation reactor at a temperature in the reactor of at least 400 °C and at a pressure in the reactor of at least 1 bar(abs), obtaining a gas stream S1 comprising CO and H2 and further comprising CO2, H2O, CH4, solid particulates and optionally H2S;c) subjecting S1 obtained according to b) to a first purification stage, obtaining a gas stream S2 comprising CO, H2 and CH4, and being depleted, compared to S1, in CO2, H2O and, if present, solid particulates, said first purification stage preferably comprisingc-1) a washing step for removing solid particulates;c-2) a drying step for removing H2O;c-3) an acid gas removal step for removing CO2 and, if present, H2S;d) optionally changing the molar ratio of CO relative to H2 in S2 obtained according to c), obtaining a gas stream S2' having a modified molar ratio of CO relative to H2;e) subjecting the purified gas stream S2 obtained according to c), optionally the modified gas stream S2' obtained according to d), to a second purification stage, obtaining at least a gas stream S3 comprising CO and being depleted in H2 and CH4 compared to S2, optionally S2', and a gas stream S4 comprising H2 and being depleted in CO and CH4 compared to S2, optionally S2';f) preparing a second composite material Mc2, comprisingsubjecting at least a portion of S3 comprising CO obtained according to e) and / or at least a portion of S4 comprising H2 obtained according to e) to a sequence of chemical conversions, obtaining one or more precursors of the second composite material Mc2;reacting the one or more precursors with a fiber component, obtaining the second composite material Mc2.

15. A process, preferably according to any one of claims 1 to 14, comprising the step of converting a chemical material obtainable or obtained by the process according to any one of claims 1 to 14 to obtain a product Q.

Images