Process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material

Abstract

The present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, processes for preparing valuable components using one or more of the prepared CO and H2, and a recycling unit for carrying out said process for preparing CO and H2 from a textile material.

Description

Process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile materialThe present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, processes for preparing valuable components using one or more of the prepared CO and H2, and a recycling unit for carrying out said process for preparing CO and H2 from a textile material.Various processes for recycling end-of-life textiles have been developed in the past to produce chemical intermediates from the used textiles that can serve as raw materials for the production of new textiles, which allow for the recycling of a specific polymers or its monomer(s). The most important recycling processes have been developed for polyethylene terephthalate (PET), polyamide 6 (PA6), and cellulose. However, such processes focus on only a minor fraction of the components of textile waste material and the rejects, comprising components other than the typical PET, PA6 and cellulose or the residue fractions, from the recycling processes, are incinerated, leading to CO2 emissions which are dangerous for the environment. Therefore, there is a need to provide improved and sustainable processes for recycling textile materials.Therefore, it was an object of the present invention to provide an improved process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, such as pieces of textile waste material, rejects or residues preferably not containing the valuable recyclable polymers PET, PA6 and cellulose, said process providing an efficient way to use textile waste materials as a feedstock for the production of new chemical products in more sustainable way. Indeed, it was an object to flexibly reintroduce end-of-life textiles, including the residue fractions and rejects textile fractions, into the chemical production process for improving sustainability of the textile industry.Therefore, the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, and optionally the feedstock A, into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, and optionally the feedstock A, fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S ;a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), and optionally the feedstock B fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a-6), and if no feedstock A is fed into the first gasification reactor according to a-1), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of S11 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, wherein the one or more pieces of the textile material are obtainable or obtained by a process comprising (i) and wherein the one or more rejects textile fractions are obtainable or obtained by a process comprising (i) and (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions;wherein the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.In particular, the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor;wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a-6), and if no feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of S11 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, wherein the one or more pieces of the textile material are obtainable or obtained by a process comprising (i) and wherein the one or more rejects textile fractions are obtainable or obtained by a process comprising (i) and (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.Further, the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising COand H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a-6), and if no feedstock A is fed into the first gasification reactor according to a-1), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3;d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of S11 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, the process further comprising (i) and optionally (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.Further, the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfermeans linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a-6), and if no feedstock A is fed into the first gasification reactor according to a-1), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of S11 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, wherein the one or more pieces of the textile material are obtainable or obtained by a process comprising (i) and wherein the one or more rejects textile fractions are obtainable or obtained by a process comprising (i) and (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, the process further comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.Further, the present invention relates to a process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a-6), and ifno feedstock A is fed into the first gasification reactor according to a-1), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of S11 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, the process further comprising (i) and optionally (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, the process further comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.According to the present invention, it may be preferred that according to a-1), from 50 to 100 weight-%, more preferably from 75 to 100 weight-%, more preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-% of what is fed into the first gasification reactor consist of the RDF and optionally the feedstock A. Preferred ranges of from 96 to 100 weight-% or 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.According to the present invention, it may be preferred that according to a-6), from 50 to 100 weight-%, more preferably from 75 to 100 weight-%, more preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-% of what is fed into the second gasification reactor consist of the feedstock B. Preferred ranges of from 96 to 100 weight-% or 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.In the context of the present invention, the term “refuse derived fuel” (RDF) refers to a solid fuel, originated from municipal solid waste. Such term is known in the art and commonly used in this particular technical field as illustrated by Yan Yang et aL, Gasification of refuse-derived fuel from municipal solid waste for energy production: a review, Environmental Chemistry Letters (2021) 19:2127-2140.In the context of the present invention, the term “solid particulates” refers to solid particulates such as ash, slag components, dust, and so on.Feedstock A and feedstock BPreferably, the textile waste material used in (i) comprises one or more of pre-consumer textile waste material and post-consumer textile waste material. Optionally, the textile waste material used in (i) consists of one or more of pre-consumer textile waste material and post-consumer textile waste material. In the context of the present invention, the term “pre-consumer textile waste material” refers to a textile waste material which is obtained, for example, from a manufacturer of textile materials in the form as, for example, textile scraps, and / or from a retailer of textile materials.Preferably, the shredding and / or cutting according to (i) is performed with one or more of a shredder, a guillotine and a cutting mill, more preferably with a shredder. Preferably, the shredder is a double-shaft shredder or a four-shaft shredder. Examples of suitable shredders are disclosed, for example, in WO 2023 / 28014 A1 .Preferably, sorting according to (ii) is performed manually or is automated.Preferably, sorting according to (ii) comprises, more preferably is an optical sorting, more preferably a hyperspectral or infrared sorting, more preferably a near-infrared sorting or a mid-infrared sorting, more preferably a near-infrared sorting.Preferably, prior to sorting, the pieces of textile waste material are spread for improving the sorting, preferably on at least one conveyor. Preferably, spreading is performed manually or is automated.Preferably, providing the one or more recyclable polymer-enriched textile fractions according to (j) comprises (i) and (ii).Preferably, prior to (jj) and optionally simultaneously with sorting according to (ii), the process for obtaining the feedstock B further comprises removing one or more of metals, stones and dust from the at least one recyclable polymer-enriched fraction. Said removing is preferably performed using one or more of an inductive sorting unit, a magnetic removal unit, an eddy current separator unit and a density sorting unit.Preferably, the chemical recycling process according to (jj) comprises, more preferably is one or more of a hydrolytic depolymerisation, an alkaline depolymerisation, an acidic depolymerisation, a methanolysis, a glycolysis, an ammonolysis, an aminolysis, and an enzymatic depolymerisation.In the context of the present invention, the term “recyclable polymer-enriched fraction” refers to a fraction comprising at least 50 weight-%, more preferably more than 50 weight-%, more preferably at least 70 weight-%, more preferably more than 70%, more preferably at least 80 weight-%, more preferably more than 80 weight-% of the recyclable polymer.Preferably, the feedstock B comprises one or more residue fractions obtained from the recycling of polyamide 6 enriched textile fractions and / or PET enriched textile fractions and / or cellulose- material enriched textile fractions.Preferably, the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising(j) providing one or more polyamide 6 enriched textile fractions;(jj) subjecting the one or more polyamide 6 enriched textile fractions provided according to (j) to a chemical recycling process, preferably comprising a depolymerisation, obtaining one or more of e-caprolactam oligomers and / or monomers, and further obtaining one or more residue fractions.The depolymerisation of polyamide 6 is preferably performed according to one or more processes known in the art, such as disclosed in EP 0 575 860 A1 , EP 0 568 882 A 1 , WO 96 / 8614 A1 , WO 96 / 18612 A1 , WO 2023 / 187045 A1 , WO 2023 / 187049 A1 , WO 2023 / 187036 A1 and WO2023 / 187043 A1.Also preferably, the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising(j) providing one or more polyethylene terephtalate enriched textile fractions;(jj) subjecting the one or more polyethylene terephtalate (PET) enriched textile fractions provided according to (j) to a chemical recycling process, preferably comprising one or more of methanolysis, glycolysis, hydrolysis, ammonolysis, and aminolysis, obtaining one or more of terephtalic acid (TPA) and dimethyl terephthalate (DMT), and further obtaining one or more residue fractions.The chemical recycling of PET is preferably performed according to one or more processes known in the art, such as those disclosed in Elaine Barnard et aL, Chemolytic depolymerisation of PET: a review, Green Chem., 2021 , 23, 3765; Ademola Bolanle Raheem et aL, Current developments in chemical recycling of post-consumer polyethylene terephthalate wastes for new materials production: A review, Journal of Cleaner Production 225 (2019) 1052-1064; Daniel Paszum et al., Chemical Recycling of Polyethylene terephthalate), Ind. Eng. Chem. Res. 1997, 36, 1373.Also preferably the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising (j) providing one or more cellulose-material enriched textile fractions;(jj) subjecting the one or more cellulose-material enriched textile fractions provided according to (j) to a chemical recycling process, preferably comprising an enzymatic depolymerisation, obtaining one or more of glucose and cellulose nanocrystal, and further obtaining one or more residue fractions.The enzymatic depolymerisation of cellulose is preferably performed according to one or more processes known in the art, such as disclosed in Fabien Hammerer et aL, Solvent-Free Enzyme Activity: Quick, High-Yielding Mechano-enzymatic Hydrolysis of Cellulose into Glucose, Angew. Chem. Int. Ed. 2018, 57, 2621-2624 and Angew. Chem. 2018, 130, 2651-2654.Feedstock C and feedstock DAccording to the present invention, it is preferred that the partial oxidation according to a-1) to a- 3) comprises a-1 ) feeding the RDF, at least one feedstock C and optionally the feedstock A into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, the at least one feedstock C and optionally the feedstock A, fed into the first gasification reactor according to a-1), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S.The at least one feedstock C according to a-1) preferably comprises at least one of automotive shredder residue (ASR) and municipal solid waste (MSW). It is conceivable that the at least one feedstock C according to a-1 ) consists of at least one of automotive shredder residue (ASR) and municipal solid waste (MSW).Further according to the present invention, it is preferred that the partial oxidation according to a-6) and a-7) comprises a-6) feeding the at least one feedstock D and optionally the feedstock B into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a-4) with oxygen fed into the reactor according to a-5), the at least one feedstock D and optionally the feedstock B, fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2.The at least lone feedstock D according to a-6) preferably comprises at least one high-caloric gas. The term “high-caloric gas” as used in this context of the present invention relates to a gas exhibiting a heating value preferably in the range of from 18 to 142 MJ / kg (Megajoule per kg). More preferably, the at least one feedstock D preferably consists of at least one high-caloric gas, the at least one high-caloric gas preferably being preferably selected from the group consisting of at least one natural gas, at least one biogas, and a mixture of two or more thereof. The term “biogas” as used in this context of the present invention relates to a gaseous renewable energy source produced from biomass raw materials such as agricultural waste, manure, municipal waste, plant material, sewage, green waste, wastewater, and food waste. Biogas is preferably produced by anaerobic digestion with anaerobic organisms or methanogens inside an anaerobic digester, biodigester or a bioreactor. More preferably, the biogas essentially consists of is primarily methane and carbon monoxide.Therefore, according to the present invention, it is preferred that the partial oxidation according to a comprises a-1 ) feeding the RDF, at least one feedstock C and optionally the feedstock A into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, the at least one feedstock C and optionally the feedstock A, fed into the first gasification reactor according to a-1), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor;a-6) feeding the at least one feedstock D and optionally the feedstock B into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a-4) with oxygen fed into the reactor according to a-5), the at least one feedstock D and optionally the feedstock B, fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2. a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor.Step a)Preferably, the fluidized bed reactor has a capacity in the range from 500 kg / h to 15 t / h (metric tons) of RDF and the feedstock A, if present, and the at least one feedstock C, if present.Preferably, the entrained flow reactor has a capacity in the range from 500 kg / h to 30 t / h (metric tons) of the intermediate gas stream S1 of step a-3) and the feedstock B, if present, and the at least one feedstock D, if present.Preferably, the partial oxidation in the first gasification reactor is conducted at a temperature in the range from 600 to 1000 °C. Preferred ranges of from 600 to 800 °C or from 700 to 900 °C or from 800 to 1000 °C are conceivable.Preferably, the partial oxidation in the first gasification reactor is conducted at a pressure of in the range of from 1 to 10 bar(abs), more preferably in the range of from 1 .5 to 8 bar(abs), more preferably in the range of from 2 to 5 bar(abs).Preferably, the partial oxidation in the second gasification reactor is conducted at a temperature in the range from 1100 to 1450 °C. Preferred ranges of from 1100 to 1300 °C or from 1200 to 1400 °C or from 1300 to 1450 °C are conceivable.Preferably, the partial oxidation in the second gasification reactor is conducted at a pressure of in the range of from 1 to 50 bar(abs), more preferably in the range of from 3 to 45 bar(abs), more preferably in the range of from 8 to 40 bar(abs).Preferably, RDF and the feedstock A, if present, and the at least one feedstock C, if present, are fed according to a-1 ) into the first gasification reactor at the middle portion of the reactor. Feeding according to a-1 ) may be carried out, for example, using a hopper system.Preferably, if the feedstock A is employed, the weight ratio of RDF relative to feedstock A introduced in the first gasification reactor is of 1 :1 or more, more preferably 2:1 or more, more preferably 5:1 or more, more preferably 10:1 or more.Preferably, the weight ratio of RDF relative to oxygen introduced in the first gasification reactor is 2:1 or more, more preferably 6:1 or more, more preferably 10:1 or more.In the context of the present invention, in a gasification reactor, the top portion is adjacent to the middle portion, the middle portion is adjacent to the bottom portion such that the middle portion is between the top portion and the bottom portion of the gasification reactor.In the context of the present invention, without wanting to be bound to any theory, it is believed that realizing a temperature of S1 during the transfer via the transfer means being in a range of from 500 to 900 °C, preferably in the range of from 650 to 900 °C, more preferably in the range of from 750 to 900 °C, more preferably in the range of from 850 to 900 °C, permits to avoid blockage, deposits, condensation of tars / cokes in the transfer means.Preferably, the transfer means used according to a-4) comprises, more preferably is a pipe, preferably an insulated pipe.Optionally, according to a-5), steam is further fed to the second gasification reactor.Preferably, the transfer means used according to a-4) is used in conjunction with a means for mixing S1 , oxygen and optionally steam, and for introducing into the second gasification reactor, said means preferably comprising, more preferably being an external mixing fluid atomizer or a fluid nozzle. In the context of the present invention, oxygen and steam, if used, are preferably introduced via the same inlet means into the atomizer or nozzle.Preferably, if the feedstock B is further added according to a-6), the means for mixing S1 , oxygen, optionally steam, and the feedstock B and for introducing into the second gasification reactor comprises, more preferably is a fluid nozzle, more preferably a three-fluid nozzle. Preferably, if the at least one feedstock D is further added according to a-6), the means for mixing S1 , oxygen, optionally steam, and the at least one feedstock D, and optionally the feedstock B, and for introducing into the second gasification reactor comprises, more preferably is a fluid nozzle, more preferably a three-fluid nozzle.Preferably, if the feedstock B is not added to the second gasification unit, the means for mixing S1 and oxygen, and optionally steam, and for introducing into the second gasification reactor comprises, more preferably is a mixing fluid atomizer, more preferably an external mixing fluid atomizer. Said atomizer can be a mixing twin-fluid atomizer, in particular an external-mixing twin-fluid atomizer. Preferably, if neither the feedstock B nor the at least one feedstock D is added to the second gasification unit, the means for mixing S1 and oxygen, and optionally steam, and for introducing into the second gasification reactor comprises, more preferably is a mixing fluid atomizer, more preferably an external mixing fluid atomizer. Said atomizer can be a mixing twin-fluid atomizer, in particular an external-mixing twin-fluid atomizer.Preferably, if the feedstock B is employed, the weight ratio of S1 relative to feedstock B introduced in the first gasification reactor is in the range of from 100 to 5000 kg / h, more preferably in the range of from 500 to 4000 kg / h, more preferably in the range of from 1000 to 3000 kg / h.Step b)Preferably, the purification stage according to b) comprises b-1 ) subjecting the stream S2 obtained according to a) to a washing step in a washing unit, obtaining a stream S21 depleted in particulate solid compared to S2 and comprising CO, H2, CO2, H2O, and optionally H2S; b-2) subjecting the stream S21 obtained according to b-1 ) to a drying step in a drying unit, obtaining a stream S22 depleted in H2O compared to S21 and S2; b-3) subjecting the stream S22 obtained according to b-2) to an acid gas removal step in a CO2 / H2S adsorption unit, obtaining the stream S3.Preferably, b-1 ) comprises contacting S2 with water in the washing unit. The washing can be performed, for example, as disclosed in WO 2023 / 161302 A1. Preferably, S21 has a temperature in the range of from 80 to 100 °C.Preferably, the drying unit used in b-2) is a water separation unit.Preferably, b-2) comprises cooling the stream S21 obtained according to b-1 ), obtaining S22, a gaseous stream separated from water condensate. The drying according to b-2) can be performed, for example, as disclosed in WO 2023 / 161302 A1.Preferably, the acid gas removal step according to b-3) comprises, more preferably is an amine scrubbing. More preferably, b-3) the amine used comprises one or more of monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA) and diglycolamine (DGA) in the CO2 / H2S adsorption unit, more preferably in the absorption column. The acid gas removal can be performed, for example, as disclosed in WO 2023 / 161302 A1.Preferably, b-3) comprises subjecting the stream S22 obtained according to b-2) to an acid gas removal step in a CO2 / H2S adsorption unit, wherein the CO2 / H2S adsorption unit preferably comprises, more preferably is an absorption column, obtaining the stream S3 and a stream Sco2 comprising CO2.Preferably, Sco2 is recycled in the process of the present invention. More preferably, Sco2 is recycled to c-2) as at least a portion of the source of CO2 in c-2).Optionally, S2 comprises CH4, wherein, if present, the CH4 content in S3 is preferably at most 1 volume-%, more preferably at most 0.5 volume-%, more preferably at most 0. 1 volume-%, based on the total volume of S2.Optionally, S2 comprises N2 and / or NH3, wherein, if present, the N2 and / or NH3 content in S2 is preferably at most 1 volume-%, more preferably at most 0.1 volume-%, based on the total volume of S2.Step c)Preferably, c) comprises c-1 ) passing and contacting water with the purified gas stream S3 obtained according to b) into a reaction unit RU(1 ) for a water gas shift reaction, obtaining a stream S3’(1 ) depleted in CO compared to S2 and comprising CO, H2, and CO2; or c-2) passing and contacting CO2 with the purified gas stream S3 obtained according to b) into a reaction unit RU(2) for a reverse water gas shift reaction, obtaining a stream S3’(2) enriched in CO compared to S2 and comprising CO and H2; or c-3) adding H2 to the purified gas stream S3 obtained according to b), obtaining a stream S3’(3) enriched in H2 compared to S2 and comprising CO and H2.The water gas shift reaction according to c-1 ) is preferably performed according to known processes in the art, such as for example those described in Wei-Hsin Chen, et aL, “Water gas shift reaction for hydrogen production and carbon dioxide capture”, Applied Energy 258 (2020) 114078, https: / / doi.Org / 10.1016 / j.apenergy.2019.114078.The reverse water gas shift reaction according to c-2) is preferably performed according to known processes in the art such as for example those described in E.Rezaei, S. Dzuryk "Techno-economic comparison of reverse water gas shift reaction to steam and dry methane reforming reactions for syngas production", Chemical Engineering Research and Design, Vol 144 (2019), S. 354-369; EP 2 175 986; CN 103183346; and US 8,946,308.Preferably, if c-1 ) is performed, the process further comprises passing S3’(1 ) in an acid gas removal unit, obtaining a stream S3’(11) depleted in CO2 compared to S3’(1 ) and comprising CO and H2.Optionally according to c-3), at least a portion of the added H2 is renewably sourced H2.Step d)Optionally, S3 comprises CH4, wherein, if present, the CH4 content in S3 is preferably at most 1 volume-%, more preferably at most 0.5 volume-%, more preferably at most 0.1 volume-% based on the total volume of S3.Optionally, S3 comprises N2 and / or NH3, wherein, if present, the N2 and / or NH3 content in S3 is preferably at most 1 volume-%, more preferably at most 0.1 volume-%, based on the total volume of S3.Preferably, d) comprises subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, preferably comprising introducing S3 or S3’ in a cold box, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2. Using a cold box, CO and H2 are separated via cryogenic separation, and two separate streams are obtained.If S3 further comprises CH4, d) preferably comprises subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, comprising introducing S3 or S3’ in a cold box, obtaining CO in a gas stream SI1 , H2 in a gas stream SI2 and CHdn a gas stream SI3. Using a cold box, CO, H2 and CH4 are separated via cryogenic separation, and three separate streams are obtained.The cryogenic separation according to d) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2001 Wiley-VCH Verlag GmbH & Co. KGaA, Carbon Monoxide, Chapter 4.3.2, pp. 685-686.Optionally, at least a portion of S11 and / or at least a portion of SI2 obtained according to d) is stored prior to e).Step e)Preferably, the CO and / or H2 used in e) is / are blended or used interchangeably with CO and / or H2 from another source.Preferably, e) comprises e-1 ) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) is / are used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) are used for this mixture; e-2) subjecting at least a portion of the methanol according to e-1 ) to a partial oxidation reaction, obtaining formaldehyde; e-3) subjecting at least a portion of the formaldehyde obtained according to e-2) to a chemical conversion, being a Reppe reaction, with acetylene, obtaining 1 ,4-butyndiol; e-4) subjecting at least a portion of the 1 ,4-butyndiole obtained according to e-3) to hydrogenation, more preferably using H2 obtained according to d), obtaining 1 ,4-butanediol; e-5) subjecting at least a portion of the 1 ,4-butanediol obtained according to e-4) to cyclization in presence of a catalyst, obtaining tetra hydrofuran (THF) as a chemical product.The synthesis of methanol according to e-1) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, ed. 2012, Wiley-VCH Verlag GmbH & Co. KGaA, “Methanol”, Chapter 5.The synthesis of formaldehyde according to e-2) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, ed. 2016, Wiley-VCH Verlag GmbH & Co. KGaA, “Formaldehyde”, Chapter 4.1 and 4.2.The synthesis of butanediol according to e-3 and e-4) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, ed. 2019, Wiley- VCH Verlag GmbH & Co. KGaA, Chapter “Butanediols, Butenediol and Butynediol”.The synthesis of tetrahydrofuran according to e-5) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, ed. 2012, Wiley-VCH Verlag GmbH & Co. KGaA, “Tetrahydrofuran”, Chapter 4.1 , p.48.Preferably, e) further comprises e-6) subjecting the tetrahydrofuran obtained according to e-5) to polymerization, obtaining poly(tetrahydrofuran) as a chemical product.The synthesis of poly(tetrahydrofuran) according to e-6) can be performed by methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2012 Wiley- VCH Verlag GmbH & Co. KGaA, Polyoxyalkylenes, Chapter 3.Also preferably, e) comprises e-1 ’) subjecting benzene to catalytic hydrogenation with at least a portion of SI2 comprising H2 obtained according to d) in the presence of a nickel-, a palladium-, or a platinum-containing catalyst, preferably a nickel-containing catalyst, obtaining cyclohexane; e-2’) subjecting the cyclohexane obtained according to e-1 ’) to oxidation in presence of a catalyst, preferably a metal salt catalyst, obtaining cyclohexanone; e-3’) subjecting the cyclohexanone obtained according to e-2’) to ammoximation reaction in presence of a hydroxylamine, obtaining cyclohexanone oxime; e-4‘) subjecting the cyclohexanone oxime obtained according to e-3‘) to a Beckmann rearrangement, obtaining e-caprolactam; e-5’) subjecting the e-caprolactam obtained according to e-4’) to polymerization in presence of water, obtaining polyamide 6.Step e-1 ’) can be performed according to methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2012 Wiley-VCH Verlag GmbH & Co. KGaA, “Cyclohexane”, Chapter 4, p. 42-46.Preferably, e-2’) comprises e-2’.1 ) subjecting the cyclohexane obtained according to e-1 ’) to oxidation in presence of a catalyst, preferably a metal salt catalyst, obtaining cyclohexanone and cyclohexanol; e-2’.2) subjecting the cyclohexanol obtained according to e-2’.1) to dehydrogenation, obtaining cyclohexanone.Step e-4’) can be performed according to methods known in the art, such as disclosed in Kirk- Othmer Encyclopedia of Chemical Technology, “Caprolactam”; https: / / onlinelbrary.wiley.eom / doi / 10.1002 / 0471238961 .0301161806091908. a01 ,pub2Step e-4’) can be performed according to methods known in the art, such as disclosed in Ullmann’s Encyclopedia of Industrial Chemistry, ed. 2020 Wiley-VCH Verlag GmbH & Co. KGaA, “Polyamides”, Chapter 5.5, p. 22-25.Preferably, e) comprises e-1 ”) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) is used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) is used for this mixture; e-2”) subjecting at least a portion of the methanol according to e-1 ”) to a partial oxidation reaction, obtaining formaldehyde; e-3”) subjecting aniline and the formaldehyde obtained according to e-2”) to condensation in presence of a catalyst, obtaining methylenedianiline (MDA); e-4”) reacting the methylenedianiline obtained according to e-3”) with phosgene in a reactor unit, obtaining methylene diphenyl diisocyanate (MDI) as the chemical product.Preferably, the phosgene used according to e-4”) is prepared via a process comprising reacting CI2 with CO, more preferably obtained according to d), in the presence of a catalyst, preferably activated carbon catalyst. Generally, phosgene can be prepared by methods known in the art, such as those disclosed in Ullmann’s Encyclopedia of industrial chemistry, Chapter „Phosgene“ 5thed., Vol. A 19, p 413 ft. , VCH Verlagsgesellschaft mbH, Weinheim, 1991 ; and C. Ryan et.al. "Phosgene and related carbonyl halides", Elsevier Science, 1996, ISBN 978-0-08-053880-8.Preferably, the process further comprises, after d) or e), f) converting a product stream comprising H2 and / or CO, obtained according to d), obtaining a monomer, polymer or polymer product.Preferably, the monomer according to f) is a di- or polyol; more preferably butandiol; aldehyde; preferably formaldehyde; di- or polyisocyanate; more preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (I PDI); amide; more preferably caprolactam; alkene; more preferably styrene, ethene and norbornene; alkyne, (di)ester; more preferably methyl methacrylate; mono or diacid; more preferably adipic acid or terephthalic acid; diamine; more preferably hexamethylenediamine, nonanediamine; or sulfones; more preferably 4,4'-dichlorodiphenyl sulfone.Preferably, the polymer according to f) is and / or the polymer product according to f) comprise(s)polyamide (PA); more preferably PA6 or PA66; polyisocyanate polyaddition product; more preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate coterephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PH A), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymer or a mixture thereof.Preferably, the polymer according to f) and / or the polymer product according to f) is / are or is / are a part of: a part of a car; more preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing, housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part, part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, cushion, or coating; a cloth; more preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part; more preferably electrical or electronic passive or active component, circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, microswitch, microbutton, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hook (snap-in), or spring tongue; a consumer, agricultural product or pharmaceutical product; more preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion, insulation, detergent, dishwasher tabs or powder, shampoo, body wash, shower gel, soap, fertilizer, fungicide, or pesticide;a packaging for the food industry; more preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, or laminating film; or a part of a construction; more preferably a rotor blade, insulating material, frame, housing, wall, coating, or separating wall.Preferably, the content of the obtained H2 and / or CO according to d) in the monomer, polymer and / or polymer product is 1 weight-% or more, 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 the content of the obtained H2 and / or CO in the monomer, polymer and / or polymer product is 100 weight-% or less, more 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; wherein more preferably, the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, more preferably based on mass balance, more preferably the International Sustainability and Carbon Certification (ISCC) standard.The present invention further relates to a process for preparing a polyurethane, comprising using methylene diphenyl diisocyanate and poly(tetrahydrofuran), wherein the methylene diphenyl diisocyanate is obtained according to e-4”) of the process according to the present invention and / or the poly(tetrahydrofuran) is obtained according to e-6) of the process according to the present invention.The present invention further relates to the use of methylene diphenyl diisocyanate and poly(tet- rahydrofuran), wherein the methylene diphenyl diisocyanate is obtained according to e-4”) of the process according to the present invention and / or the poly(tetrahydrofuran) is obtained according to e-6) of the process according to the present invention, for preparing a polyurethane.The present invention further relates to a process for preparing a textile material, comprising using polyamide 6 and / or a polyurethane, wherein the polyamide 6 is obtained according to e- 3’) of the process according to the present invention and / or the polyurethane is obtained according to the process according to the present invention.The present invention further relates to a recycling unit for carrying out the process for preparing CO and H2 from a textile material according to the present invention, the unit comprising a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion an inlet means for feeding the RDF into the first gasification reactor; optionally an inlet means for feeding the feedstock A into the first gasification reactor;optionally at least one inlet means for feeding the at least one feedstock C into the first gasification reactor; an inlet means for feeding oxygen and steam into the first gasification reactor at the bottom, or middle, portion of said reactor; an outlet means for removing S1 from the first gasification reactor; a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion; a transfer means for transferring S1 from the first gasification reactor to the second gasification reactor; an inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor; an inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor; optionally an inlet means for feeding the feedstock B into the second gasification reactor; optionally at least one inlet means for feeding the at least one feedstock D into the second gasification reactor; an outlet means for removing S2 from the second gasification reactor at the bottom portion of the reactor; one or more means for operating the purification stage; optionally a means for adjusting the CO to H2 molar ratio in S3; one or more means for operating the separation stage; optionally a means for operating the chemical conversion or the sequence of chemical conversions of S11 and / or SI2.Preferably, the inlet means for feeding the RDF into the first gasification reactor, optionally the inlet means for feeding the feedstock A into the first gasification reactor, and optionally the at least one inlet means for feeding the at least one feedstock C into the first gasification reactor comprise a hopper system. Preferably, the inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor, the inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor and optionally the inlet means for feeding the feedstock B and the at least one feedstock D into the second gasification reactor are one single unit, more preferably a nozzle or an atomizer. The nozzle is preferably a three-fluid nozzle, and the atomizer is preferably a mixing twin-fluid atomizer.According to another aspect, 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. According to yet another aspect, the present invention relates to a process, comprising using the recycling unit as defined hereinabove to obtain a chemical material; and preferably converting at least a part of the chemical material 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; or industrial 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; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acry- late 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; or polymer 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 / or 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.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 described 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, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, 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 higher structural complexity and / or higher molecular weight than the building block on which the secondary 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)acry- lates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acrylic 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 compound”, 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 compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably 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. reinforcement, 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 defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1.The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer 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, poly- ether-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 agrochemical 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 agrochemical 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 conducted 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 compounds 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 paragraph

[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 beveragestabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrrolidone-co- polymer. 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 polymers) 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 dispersions) 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 dispersants), 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 nonionic, 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 Commission 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 present invention is further illustrated by the following set of embodiments and combina-tions of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 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 (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a-4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at apressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a- 6), and if no feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is fed into the second gasification reactor according to a-6); b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, wherein the one or more pieces of the textile material are obtainable or obtained by a process comprising (i) and wherein the one or more rejects textile fractions are obtainable or obtained by a process comprising (i) and (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomersand / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.2. The process of embodiment 1 , the partial oxidation according to a-1 ) to a-3) comprising a-1 ) feeding the RDF, at least one feedstock C and optionally the feedstock A into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion, said at least one feedstock C preferably comprising at least one of automotive shredder residue (ASR) and municipal solid waste (MSW); a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, the at least one feedstock C and optionally the feedstock A, fed into the first gasification reactor according to a-1), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S.3. The process of embodiment 1 or 2, the partial oxidation according to a-6) and a-7) comprising a-6) feeding the at least one feedstock D and optionally the feedstock B into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a- 4) with oxygen fed into the reactor according to a-5), the at least one feedstock D and optionally the feedstock B, fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2, said at least one feedstock D preferably comprising at least one high-caloric gas.4. The process of any one of embodiments 1 to 3, wherein the textile waste material used in (i) includes comprises and one or more of consumer textile waste material and post-consumer textile waste material.5. The process of any one of embodiments 1 to 4, wherein the shredding and / or cutting according to (i) is performed with one or more of a shredder, a guillotine and a cutting mill, preferably a shredder.6. The process of any one of embodiments 1 to 5, wherein sorting according to (ii) comprises, more preferably is an optical sorting, more preferably a hyperspectral or infrared sorting, more preferably a near-infrared sorting or a mid-infrared sorting, more preferably a near-infrared sorting.7. The process of any one of embodiments 1 to 6, wherein providing the one or more recyclable polymer-enriched textile fractions according to (j) comprises (i) and (ii).8. The process of any one of embodiments 1 to 7, wherein the chemical recycling process according to (jj) comprises, more preferably is one or more of a hydrolytic depolymerisation, an alkaline depolymerisation, an acidic depolymerisation, a methanolysis, a glycolysis, an ammonolysis, an aminolysis, and an enzymatic depolymerisation.9. The process of any one of embodiments 1 to 8, wherein the fluidized bed reactor has a capacity in the range from 500 kg / h to 15 t / h and feedstock A, if present.10. The process of any one of embodiments 1 to 9, wherein the entrained flow reactor has a capacity in the range from 500 kg / h to 30 t / h of the intermediate gas stream S1 of step a- 3) and the feedstock B, if present.11 . The process of any one of embodiments 1 to 10, wherein the partial oxidation in the first gasification reactor is conducted at a temperature in the range from 600 to 1000 °C.12. The process of any one of embodiments 1 to 11 , wherein the partial oxidation in the first gasification reactor is conducted at a pressure of in the range of from 1 to 10 bar(abs), preferably in the range of from 1 .5 to 8 bar(abs), more preferably in the range of from 2 to 5 bar(abs).13. The process of any one of embodiments 1 to 12, wherein the partial oxidation in the second gasification reactor is conducted at a temperature in the range from 1100 to 1450 °C.14. The process of any one of embodiments 1 to 13, wherein the partial oxidation in the second gasification reactor is conducted at a pressure of in the range of from 1 to 50 bar(abs), preferably in the range of from 3 to 45 bar(abs), more preferably in the range of from 8 to 40 bar(abs).15. The process of any one of embodiments 1 to 14, wherein the purification stage according to b) comprises b-1 ) subjecting the stream S2 obtained according to a) to a washing step in a washing unit, obtaining a stream S21 depleted in particulate solid compared to S2 and comprising CO, H2, CO2, H2O, and optionally H2S; b-2) subjecting the stream S21 obtained according to b-1) to a drying step in a drying unit, obtaining a stream S22 depleted in H2O compared to S21 and S2; b-3) subjecting the stream S22 obtained according to b-2) to an acid gas removal step in a CO2 / H2S adsorption unit, obtaining the stream S3.16. The process of any one of embodiments 1 to 15, wherein c) comprisesc-1 ) passing and contacting water with the purified gas stream S3 obtained according to b) into a reaction unit RU(1) for a water gas shift reaction, obtaining a stream S3’(1 ) depleted in CO compared to S2 and comprising CO, H2, and CO2; or c-2) passing and contacting CO2 with the purified gas stream S3 obtained according to b) into a reaction unit RU(2) for a reverse water gas shift reaction, obtaining a stream S3’(2) enriched in CO compared to S2 and comprising CO and H2; or c-3) adding H2 to the purified gas stream S3 obtained according to b), obtaining a stream S3’(3) enriched in H2 compared to S2 and comprising CO and H2.17. The process of embodiment 16, wherein, if c-1 ) is performed, the process further comprises passing S3’(1 ) in an acid gas removal unit, obtaining a stream S3’(11) depleted in CO2 compared to S3’(1 ) and comprising CO and H2.18. The process of embodiment 16 or 17, wherein according to c-3), at least a portion of the added H2 is renewably sourced H2.19. The process of any one of embodiments 1 to 18, wherein d) comprises subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, preferably comprising introducing S3 or S3’ in a cold box, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.20. The process of any one of embodiments 1 to 19, wherein the CO and / or H2 used in e) is / are blended or used interchangeably with CO and / or H2 from another source.21 . The process of any one of embodiments 1 to 20, wherein e) comprises e-1 ) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) is / are used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) are used for this mixture; e-2) subjecting at least a portion of the methanol according to e-1) to a partial oxidation reaction, obtaining formaldehyde; e-3) subjecting at least a portion of the formaldehyde obtained according to e-2) to a chemical conversion, being a Reppe reaction, with acetylene, obtaining 1 ,4-butyn- diol; e-4) subjecting at least a portion of the 1 ,4-butyndiole obtained according to e-3) to hydrogenation, more preferably using H2 obtained according to d), obtaining 1 ,4-bu- tanediol; e-5) subjecting at least a portion of the 1 ,4-butanediol obtained according to e-4) to cyclization in presence of a catalyst, obtaining tetra hydrofuran (THF) as a chemical product.22. The process of embodiment 21 , wherein e) further comprises e-6) subjecting the tetrahydrofuran obtained according to e-5) to polymerization, obtaining poly(tetrahydrofuran) as a chemical product.23. The process of any one of embodiments 1 to 20, wherein e) comprises e-1 ’) subjecting benzene to catalytic hydrogenation with at least a portion of SI2 comprising H2 obtained according to d) in the presence of a nickel-, palladium-, or platinum containing catalyst, preferably a nickel-containing catalyst, obtaining cyclohexane; e-2’) subjecting the cyclohexane obtained according to e-1 ’) to oxidation in presence of a catalyst, preferably a metal salt catalyst, obtaining cyclohexanone; e-3’) subjecting the cyclohexanone obtained according to e-2’) to ammoximation reaction in presence of a hydroxylamine, obtaining cyclohexanone oxime; e-4‘) subjecting the cyclohexanone oxime obtained according to e-3‘) to a Beckmann rearrangement, obtaining e-caprolactam; e-5’) subjecting the e-caprolactam obtained according to e-4’) to polymerization in presence of water, obtaining polyamide 6.24. The process of any one of embodiments 1 to 23, wherein e) comprises e-1 ”) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) is used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) is used for this mixture; e-2”) subjecting at least a portion of the methanol according to e-1 ”) to a partial oxidation reaction, obtaining formaldehyde; e-3”) subjecting aniline and the formaldehyde obtained according to e-2”) to condensation in presence of a catalyst, obtaining methylenedianiline (MDA); e-4”) reacting the methylenedianiline obtained according to e-3”) with phosgene in a reactor unit, obtaining methylene diphenyl diisocyanate (MDI) as the chemical product.25. The process of embodiment 24, wherein the phosgene used according to e-4”) is obtained by a process comprising reacting CI2 with CO, preferably obtained according to d), in presence of a catalyst, preferably an activated carbon catalyst.26. The process of any one of embodiments 1 to 20, further comprising after d) or e): f) converting a product stream comprising H2 and / or CO, obtained according to d), obtaining a monomer, polymer or polymer product.27. The process of embodiment 26, wherein the monomer is a di- or polyol; preferably bu- tandiol; aldehyde; preferably formaldehyde; di- or polyisocyanate; preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (IPDI);amide; preferably caprolactam; alkene; preferably styrene, ethene and norbornene; alkyne, (di)ester; preferably methyl methacrylate; mono or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine; or sulfones; preferably 4,4'-dichlorodiphenyl sulfone. The process of embodiment 26 or 27, wherein the polymer is and / or the polymer product comprises polyamide (PA); preferably PA6 or PA66; polyisocyanate polyaddition product; preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocy- anurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1 ,4- isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate coterephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxy- butyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymer or a mixture thereof. The process of any one of embodiments 26 to 28, wherein the polymer and / or the polymer product is / are or is / are a part of: a part of a car; preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing, housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part, part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, cushion, or coating; a cloth; preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part; preferably electrical or electronic passive or active component, circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, microswitch, microbutton, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hook (snap-in), or spring tongue;a consumer, agricultural product or pharmaceutical product; preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion, insulation, detergent, dishwasher tabs or powder, shampoo, body wash, shower gel, soap, fertilizer, fungicide, or pesticide; a packaging for the food industry; preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, or laminating film; or a part of a construction; preferably a rotor blade, insulating material, frame, housing, wall, coating, or separating wall.30. The process of any one of claims 26 to 29, wherein the content of the obtained H2 and / or CO according to d) in the monomer, polymer and / or polymer product 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 obtained H2 and / or CO in the monomer, polymer and / or polymer product 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.31 . A process for preparing a polyurethane, comprising using methylene diphenyl diisocyanate and poly(tetrahydrofuran), wherein the methylene diphenyl diisocyanate is obtained according to e-4”) of the process of embodiment 24 or 25 and / or the poly(tetrahydrofuran) is obtained according to e-6) of the process of embodiment 22.32. A process for preparing a textile material, comprising using polyamide 6 and / or a polyurethane, wherein the polyamide 6 is obtained according to e-3’) of the process of embodiment 23 and / or the polyurethane is obtained according to the process of embodiment 31 .33. A recycling unit for carrying out the process for preparing CO and H2 from a textile material according to any one of embodiments 1 to 30, the unit comprising a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion an inlet means for feeding the RDF into the first gasification reactor;optionally an inlet means for feeding the feedstock A into the first gasification reactor; optionally at least one inlet means for feeding the at least one feedstock C into the first gasification reactor; an inlet means for feeding oxygen and steam into the first gasification reactor at the bottom, or middle, portion of said reactor; an outlet means for removing S1 from the first gasification reactor; a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion; a transfer means for transferring S1 from the first gasification reactor to the second gasification reactor; an inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor; an inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor; optionally an inlet means for feeding the feedstock B into the second gasification reactor; optionally at least one inlet means for feeding the at least one feedstock D into the second gasification reactor; an outlet means for removing S2 from the second gasification reactor at the bottom portion of the reactor; one or more means for operating the purification stage; optionally a means for adjusting the CO to H2 molar ratio in S3; one or more means for operating the separation stage; optionally a means for operating the chemical conversion or the sequence of chemical conversions of SI1 and / or SI2. The recycling unit of embodiment 33, wherein the inlet means for feeding the RDF into the first gasification reactor, optionally the inlet means for feeding the feedstock A into the first gasification reactor, and optionally the at least one inlet means for feeding the at least one feedstock C into the first gasification reactor preferably comprise a hopper system, and wherein the inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor, the inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor and optionally the inlet means for feeding the feedstock B and the at least one feedstock D into the second gasification reactor are preferably one single unit, more preferably a nozzle or an atomizer, wherein the nozzle is preferably a three-fluid nozzle and the atomizer is preferably a mixing twin-fluid atomizer. A process, preferably according to any one of embodiments 1 to 25, comprising the step of converting a chemical material obtainable or obtained by the process according to any one of embodiments 1 to 25 to obtain a product Q. A process, comprising using the recycling unit according to embodiment 33 or 34 to obtaina chemical material; and preferably converting at least a part of the chemical material to obtain a product Q.37. The process of embodiment 35 or 36, wherein the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition 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; or aqueous 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; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.38. The process of any one of embodiments 35 to 37, 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 does not represent the 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 agiven 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 example.ExamplesThe examples are based on simulations performed via the flow sheet simulation platform Aspen Plus V14.0.The pieces of textile material used as feedstock A in the following examples are obtained from textile waste material which has been shredded and passed through a means for removing any metals and inerts, such as stones, dirt, etc..The textile recycling residues are the residue fractions obtained after having recycled one or more of PA6, PET and cellulose-material enriched textile fractions (cf. the definition of feedstock B herein above).Example 1The first example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting a feed stream F1 of refuse derived fuel and pieces of textile material (feedstock A) into a synthesis gas. The fluidized bed reactor is fed with the feed stream F1 (having a weight ratio of refuse derived fuel relative to pure textile waste of 50:50) at a mass flow of 10 t / h at 4 bar(abs) and 35 °C. The feed stream F1 comprises 46.1 weight-% carbon, 6.6 weight-% hydrogen, 45.1 weight-% oxygen and 2.2 weight-% nitrogen. Additionally, gasification agents are injected into the fluidized bed reactor, enabling a gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.58 t / h at -30 °C at 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of the entrained flow gasifier whereby being kept at a temperature of 800 °C as a second stage and injected via the burner (= an external-mixing atomizer). Here, additional oxygen at a mass flow of 2.9 t / h at 6 bar(abs) and 100 °C is used to increase the temperature up to 1350 °C at the gasifier outlet and convert remaining hydrocarbons, tars, and soot into synthesis gas. The resulting high-temperature synthesisgas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine scrubbing, is used to separate acids like CO2 with a mass flow of 6.2 t / h from the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises 46.7 volume-% H2, 52.6 volume-% CO, 0.7 volume-% H2O at a total mass flow of 7.3 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Example 2The second example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting a feed stream F1 of refuse derived fuel and pieces of textile material (feedstock A) into synthesis gas. The fluidized bed reactor is fed with the feed stream (having a weight ratio of refuse derived fuel relative to pure textile waste of 90:10) at a mass flow of 10 t / h at 4 bar(abs) and 35 °C. The feed stream F1 comprises 41 .2 weight-% carbon, 7.7 weight-% hydrogen, 49.0 weight-% oxygen and 2.1 weight-% nitrogen. Additionally, gasification agents are injected into the fluidized bed gasifier, enabling the gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.75 t / h at -30 °C at 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of an entrained flow gasifier whereby being kept at a temperature of 800 °C as a second stage and injected via the burner (= an external-mixing atomizer). Here, additional oxygen at a mass flow of 2.7 t / h at 6 bar(abs) and 100 °C is used to increase the temperature up to 1350 °C at the gasifier outlet and convert remaining hydrocarbons, tars, and soot into synthesis gas. The resulting high-tempera- ture synthesis gas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of water, ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine scrubbing, is used to separate acids like CO2 with a mass flow of 6.1 t / h from the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises of 50.3 volume- % H2, 48.9 volume-% CO, 0.8 volume-% H2O at a total mass flow of 6.2 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Example 3The third example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting two feed streams: stream F1 consisting of refuse derived fuel and pieces of textile material (feedstock A) as well as stream F2 (=feedstock B) of textile recycling residues into a synthesis gas. The fluidized bed reactor is fed with the first feed stream F1 (having a weight ratio of refuse derived fuel relative to pure textile waste of 50:50) at a mass flow of 10 t / h with 4 bar and 35 °C. The feed stream F1 comprises 46.1 weight-% carbon, 6.6 weight-% hydrogen, 45.1 weight-% oxygen and 2.2 weight-% nitrogen. Additionally,gasification agents are injected into the fluidized bed reactor, enabling a gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.65 t / h at -30 °C and 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of the entrained flow gasifier whereby being kept at a temperature of 800 °C as a second stage and injected via a burner (=three-fluid nozzle). In the burner, the second feed stream F2 (= feedstock B of textile recycling residue) is added with a mass flow of 10 t / h at 100°C and 5 bar(abs). The second feed stream F2 (=feedstock B) is atomized with additional oxygen at a mass flow of 10.8 t / h at 6 bar(abs) and 100 °C, which is used to increase the temperature up to 1350 °C at the gasifier outlet and convert the second feed stream and remaining hydrocarbons, tars, and soot into a synthesis gas. The resulting high-temperature synthesis gas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of water, ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine scrubbing, is used to separate acids like CO2 with a mass flow of 6.8 t / h from the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises 45.1 volume-% H2, 51.4 volume-% CO, 3.5 volume-% H2O at a total mass flow of 23.9 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Example 4The fourth example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting two feed streams: a stream F1 of refuse derived fuel and pieces of textile material (feedstock A) as well as a stream F2 textile recycling residues (feedstock B) into a synthesis gas. Therefore, the fluidized bed reactor is fed with the first feed stream (having a weight ratio of refuse derived fuel relative to pure textile waste of 50:50) at a mass flow of 10 t / h at 4 bar(abs) and 35 °C. The feed stream F1 comprises 46.1 weight-% carbon, 6.6 weight-% hydrogen, 45.1 weight-% oxygen and 2.2 weight-% nitrogen. Additionally, gasification agents are injected into the fluidized bed gasifier, enabling a gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.65 t / h at -30°C and 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of the entrained flow gasifier whereby being kept at a temperature of 800 °C as a second stage and injected via a burner (=three-fluid nozzle). In the burner, the second feed stream F2 (=feedstock B - textile recycling residue) is added with a mass flow of 1 t / h at 100 °C and 5 bar(abs). The second feed stream F2 is atomized with additional oxygen at a mass flow of 3.7 t / h at 6 bar(abs) and 100°C, which is used to increase the temperature up to 1350 °C at the gasifier outlet and convert the second feed stream and remaining hydrocarbons, tars, and soot into a synthesis gas. The resulting high-temperature synthesis gas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine wash, is used to separate acids like CO2 with a mass flow of 6.3 t / hfrom the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises 46.2 vol- ume-% H2, 52.3 volume-% CO, 1 .5 volume-% H2O at a total mass flow of 8.9 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Example 5The fifth example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting two feed streams: F1 of refuse derived fuel and pieces of textile material (feedstock A) as well as a stream F2 (= feedstock B) of textile recycling residues into a synthesis gas. The fluidized bed reactor is fed with the first feed stream F1 (having a weight ratio of refuse derived fuel relative to pure textile waste of 90:10) at a mass flow of 10 t / h at 4 bar(abs) and 35 °C. The feed stream F1 comprises 41 .2 weight-% carbon, 7.7 weight-% hydrogen, 49.0 weight-% oxygen and 2.1 weight-% nitrogen. Additionally, gasification agents are injected into the fluidized bed gasifier, enabling a gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.75 t / h at -30 °C at 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of an entrained flow gasifier whereby being kept at a temperature of 800 °C as second stage and injected via a burner (=three-fluid nozzle). In the burner, the second feed stream F2 (=feedstock B - textile recycling residue) is added with a mass flow of 10 t / h at 100 °C and 5 bar(abs). The second feed stream F2 is atomized with additional oxygen at a mass flow of 10.5 t / h at 6 bar and 100°C, which is used to increase the temperature up to 1350 °C at the gasifier outlet and convert the second feed stream and remaining hydrocarbons, tars, and soot into a synthesis gas. The resulting high-temperature synthesis gas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of water, ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25 °C. The acid gas removal, enabled by an amine scrubbing, is used to separate acids like CO2 with a mass flow of 7.1 t / h from the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises of 46.9 volume-% H2, 49.5 volume-% CO, 3.6 volume-% H2O at a total mass flow of 22.7 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Example 6The sixth example is a two-step gasification process comprising a fluidized bed reactor, followed by an entrained flow gasifier, converting two feed streams: F1 of refuse derived fuel and pieces of textile material (feedstock A) as well as a stream F2 (= feedstock B) of textile recycling residues into a synthesis gas. The fluidized bed reactor is fed with the first feed stream F1 (having a weight ratio of refuse derived fuel relative to pure textile waste of 90:10) at a mass flow of 10 t / h at 4 bar(abs) and 35 °C. The feed stream F1 comprises 41.2 weight-% carbon, 7.7 weight-% hydrogen, 49.0 weight-% oxygen and 2.1 weight-% nitrogen. Additionally, gasificationagents are injected into the fluidized bed gasifier, enabling the gasification reaction at a temperature of 800 °C. The gasification agents are steam with a mass flow of 5 t / h at 5.4 bar(abs) and 180 °C, as well as oxygen with a mass flow of 2.75 t / h at -30 °C and 6 bar(abs). The resulting raw synthesis gas stream S1 is sent to the top of the entrained flow gasifier whereby being kept at a temperature of 800 °C as a second stage and injected via a burner (=three-fluid nozzle). In the burner, the second feed stream F2 (=feedstock B of textile recycling residue) is added with a mass flow of 1 t / h at 100 °C and 5 bar(abs). The second feed stream F2 is atomized with additional oxygen at a mass flow of 3.5 t / h at 6 bar(abs) and 100 °C, which is used to increase the temperature up to 1350 °C at the gasifier outlet and convert the second feed stream and remaining hydrocarbons, tars, and soot into synthesis gas. The resulting high-temperature synthesis gas stream S2, comprising CO, H2O, CO2, H2, and traces of CH4, N2 and NH3, is washed with water and dried in order to reduce the amount of ash and tars. The raw synthesis gas exits the wash & drying step at a temperature of 25°C. The acid gas removal, enabled by an amine scrubbing, is used to separate acids like CO2 with a mass flow of 6.3 t / h from the raw synthesis gas. The obtained clean synthesis gas stream S3 comprises of 49.5 volume-% H2, 49.0 volume- % CO, 1 .5 volume-% H2O at a total mass flow of 7.8 t / h. Subsequently, the stream S3 was subjected to a separation stage, using a cold box, for obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.Description of the figureFigure 1 is a schematic representation of the process according to embodiments of the present invention. The gaseous stream F1 comprising O2 and steam is introduced into GR1 (first gasification reactor = fluidized bed reactor) together with RDF (refused derived fuel) and subjected to gasification at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in GR1 . The stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S is then withdrawn from GR1 and transferred to GR2 (second gasification reactor = entrained flow reactor) via a transfer means, preferably a pipe, and introduced, preferably with a nozzle or atomizer, in GR2. The temperature in the pipe during the transfer is in the range of from 500 to 900 °C. A gaseous stream F2 comprising O2 is introduced into GR2. The gasification in GR2 is performed at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs) for obtaining the raw synthesis gas stream S2 comprising in addition to CO and H2, CO2, H2O, solid particulates, and optionally H2S. In GR1 , FA(i) and / or FA(ii) can further be introduced. In GR2, FB can be further introduced as well. It is in any case required that at least one of the feedstock A (FA(i) and / or FA(ii)) and the feedstock B (FB) be used in the process. FA(i) is obtained after shredding and / or cutting in SCU(i) the textile waste material (TWM). FA(ii) is obtained after sorting in S(ii) the pieces of textile waste material comprised in FA(i), this is the reject stream, while F(R) comprises recyclable polymers such as PA6, PET and / or cellulose-material. FB is obtained after the recycling of F(R) in CRP(jj), which produces P(R) comprising one or more oligomers and / or monomers from the recyclable polymers such as caprolactam, glucose, TPA and / or DMT. The stream S2 is then subjected to a purification stage (PS(b)) to remove the solid particulates, water, carbon dioxide and hydrogen sulphide if present. The purified gas stream S3, comprisingCO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, is obtained and subjected to a separation stage SS(d) for obtaining a stream SI1 comprising CO and a stream SI2 comprising H2. Prior to be separated in SS(d), the CO to H2 molar ratio in the purified gas stream S3 can be adjusted according to the industrial need. The streams SI1 and / or SI2 or a portion of SI1 and / or SI2 can then be subjected to a chemical conversion or sequence of chemical conversions in CCU(e)) for obtaining one or more chemical products that can be used for textile production in TPU. The obtained textiles eventually will become textile waste material together with the scraps and so on from the textile industry. Hence, the process according to the present invention permits to optimize the loop in order to render the textile industry more sustainable in view of the use of all the textile waste material, and not only the valuable recyclable polymers, but also the rejects and residue fractions, in order to produce new polymers and new textile materials.Cited literatureWO 2023 / 28014 A1EP 0 575 860 A1EP 0 568 882 A 1WO 96 / 8614 A1WO 96 / 18612 A1WO 2023 / 187045 A1WO 2023 / 187049 A1 WO 2023 / 187036 A1 WO2023 / 187043 A1 Elaine Barnard et aL, Chemolytic depolymerisation of PET: a review, Green Chem., 2021 , 23, 3765Ademola Bolanle Raheem et aL, Current developments in chemical recycling of post-consumer polyethylene terephthalate wastes for new materials production: A review, Journal of Cleaner Production 225 (2019) 1052-1064Daniel Paszum et aL, Chemical Recycling of Poly(ethylene terephthalate), Ind. Eng. Chem. Res. 1997, 36, 1373Fabien Hammerer et aL, Solvent-Free Enzyme Activity: Quick, High-Yielding Mechano- enzymatic Hydrolysis of Cellulose into Glucose, Angew. Chem. Int. Ed. 2018, 57, 2621- 2624 and Angew. Chem. 2018, 130, 2651-2654 WO 2023 / 161302 A1Wei-Hsin Chen, et aL, “Water gas shift reaction for hydrogen production and carbon dioxide capture”, Applied energy 258 (2020) 114078, https: / / d0i.0rg / l 0.1016 / j.apen- ergy.2019.114078E.Rezaei, S. Dzuryk "Techno-economic comparison of reverse water gas shift reaction to steam and dry methane reforming reactions for syngas production", Chemical Engineering Research and Design, Vol 144 (2019), S. 354-369 EP 2 1759 86 CN 103183346US 8,946,308Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2001 Wiley-VCH Verlag GmbH & Co.KGaA, Carbon Monoxide, Chapter 4.3.2, p.685-686Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2012 Wiley-VCH Verlag GmbH & Co.KGaA, Methanol, Ch. 5Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2016 Wiley-VCH Verlag GmbH & Co.KGaA, Formaldehyde, Ch. 4.1 and 4.2Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2019 Wiley-VCH Verlag GmbH & Co.KGaA, Butanediols, Butenediol and ButynediolUllmann’s Encyclopedia of Industrial Chemistry, Ed. 2012 Wiley-VCH Verlag GmbH & Co.KGaA, Tetrahydrofuran, Chapter 4.1 , p.48Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2000 Wiley-VCH Verlag GmbH & Co.KGaA, Polyoxyalkylenes, Ch. 3Ullmann’s Encyclopedia of Industrial Chemistry, Ed. 2000 Wiley-VCH Verlag GmbH & Co.KGaA, Polyamides, Ch. 5.5, p. 22-25Ullmann’s Encyclopedia of industrial chemistry, Chapter „Phosgene“ 5thEd., Vol. A 19, p413 ff., VCH Verlagsgesellschaft mbH, Weinheim, 1991C. Ryan et.al. "Phosgene and related carbonyl halides", Elsevier Science, 1996, ISBN 978-0-08-053880-8

Claims

Claims1 . A process for preparing carbon monoxide (CO) and molecular hydrogen (H2) from a textile material, the process comprising: a) subjecting at least a refuse derived fuel (RDF) and one or more of a feedstock A and a feedstock B to a partial oxidation, obtaining a raw synthesis gas stream S2 comprising CO and H2, and additionally comprising CO2, H2O, solid particulates, and optionally H2S, the partial oxidation comprising a-1 ) feeding the RDF, optionally the feedstock A, and optionally at least one feedstock C into a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion; a-2) feeding oxygen and steam into the first gasification reactor at the bottom portion or middle portion of said reactor; a-3) bringing in contact the RDF, optionally the feedstock A and optionally the at least one feedstock C fed into the first gasification reactor according to a-1 ), together with oxygen and steam, fed into the first gasification reactor according to a-2), at a temperature in the range of from 350 to 1000 °C and at a pressure in the range of from 1 to 200 bar(abs) in said reactor, obtaining an intermediate gas stream S1 comprising CO, H2, CO2, solid particulates, hydrocarbons, and optionally H2S; a-4) withdrawing S1 obtained according to a-3) from the first gasification reactor at its top portion, and transferring S1 to a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion, via a transfer means linking the top portion of the first gasification reactor to the top portion of the second gasification reactor, wherein the temperature of the gaseous stream S1 during the transfer via the transfer means is in a range of from 500 to 900 °C; a-5) feeding oxygen into the second gasification reactor at the top portion of said reactor; a-6) optionally feeding the feedstock B and optionally at least one feedstock D into the second gasification reactor; a-7) bringing in contact S1 transferred to the second gasification reactor according to a-4) with oxygen fed into the reactor according to a-5), optionally the feedstock B and optionally the at least one feedstock D fed into the reactor according to a-6), at a temperature in the range of from 1000 to 1700 °C and at a pressure in the range of from 1 to 200 bar(abs), obtaining the raw synthesis gas stream S2; a-8) withdrawing the raw synthesis gas stream S2 obtained according to a-7) from the second gasification reactor at the bottom portion of said reactor; wherein, if the feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is optionally fed into the second gasification reactor according to a- 6), and if no feedstock A is fed into the first gasification reactor according to a-1 ), the feedstock B is fed into the second gasification reactor according to a-6);b) subjecting the raw synthesis gas stream S2 obtained according to a) to a purification stage, obtaining a purified gas stream S3 comprising CO and H2, S3 being depleted in CO2, H2O, solid particulates and H2S, if present in S2, compared to S2, the purification stage comprising b-1 ) a washing step to remove the particulate solid; b-2) a drying step to remove water; b-3) an acid gas removal step to remove CO2 and H2S, if present; c) optionally adjusting the CO to H2 molar ratio in the purified gas stream S3 obtained according to b), obtaining a modified gas stream S3’ comprising CO and H2 having a CO to H2 molar ratio different to the CO to H2 molar ratio in S3; d) subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2; e) optionally subjecting at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) to a chemical conversion or sequence of chemical conversions, obtaining one or more chemical products; wherein the feedstock A comprises one or more rejects textile fractions, one or more pieces of textile material, or a mixture thereof, wherein the one or more pieces of the textile material are obtainable or obtained by a process comprising (i) and wherein the one or more rejects textile fractions are obtainable or obtained by a process comprising (i) and (ii) as follows:(i) shredding and / or cutting a textile waste material, obtaining pieces of the textile material;(ii) sorting the pieces of the textile material obtained according to (i) by chemical composition, obtaining one or more textile fractions each with an enriched amount of a specific recyclable polymer and further obtaining the one or more rejects textile fractions; wherein the feedstock B comprises one or more residue fractions, wherein the one or more residue fractions are obtainable or obtained by a process comprising (j) and (jj) as follows:(j) providing one or more recyclable polymer-enriched textile fractions;(jj) subjecting the one or more recyclable polymer-enriched textile fractions provided according to (j) to a chemical recycling process, obtaining one or more of oligomers and / or monomers each derived from the respective recyclable polymer, and further obtaining the one or more residue fractions; wherein the recyclable polymer is one or more of polyamide 6 (PA6), polyethylene terephthalate (PET) and cellulose-based material.

2. The process of claim 1 , wherein sorting according to (ii) comprises, more preferably is an optical sorting, more preferably a hyperspectral or infrared sorting, more preferably a near-infrared sorting or a mid-infrared sorting, more preferably a near-infrared sorting.

3. The process of claim 1 or 2, wherein providing the one or more recyclable polymer-en- riched textile fractions according to (j) comprises (i) and (ii).

4. The process of any one of claims 1 to 3, wherein the chemical recycling process according to (jj) comprises, more preferably is one or more of a hydrolytic depolymerisation, an alkaline depolymerisation, an acidic depolymerisation, a methanolysis, a glycolysis, an ammonolysis, an aminolysis, and an enzymatic depolymerisation.

5. The process of any one of claims 1 to 4, wherein the purification stage according to b) comprises b-1 ) subjecting the stream S2 obtained according to a) to a washing step in a washing unit, obtaining a stream S21 depleted in particulate solid compared to S2 and comprising CO, H2, CO2, H2O, and optionally H2S; b-2) subjecting the stream S21 obtained according to b-1 ) to a drying step in a drying unit, obtaining a stream S22 depleted in H2O compared to S21 and S2; b-3) subjecting the stream S22 obtained according to b-2) to an acid gas removal step in a CO2 / H2S adsorption unit, obtaining the stream S3.

6. The process of any one of claims 1 to 5, wherein c) comprises c-1 ) passing and contacting water with the purified gas stream S3 obtained according to b) into a reaction unit RU(1 ) for a water gas shift reaction, obtaining a stream S3’(1 ) depleted in CO compared to S2 and comprising CO, H2, and CO2; or c-2) passing and contacting CO2 with the purified gas stream S3 obtained according to b) into a reaction unit RU(2) for a reverse water gas shift reaction, obtaining a stream S3’(2) enriched in CO compared to S2 and comprising CO and H2; or c-3) adding H2 to the purified gas stream S3 obtained according to b), obtaining a stream S3’(3) enriched in H2 compared to S2 and comprising CO and H2.

7. The process of claim 6, wherein, if c-1 ) is performed, the process further comprises passing S3’(1 ) in an acid gas removal unit, obtaining a stream S3’(11 ) depleted in CO2 compared to S3’(1) and comprising CO and H2..

8. The process of any one of claims 1 to 7, wherein d) comprises subjecting the purified gas stream S3 obtained according to b), or the modified gas stream S3’ obtained according to c), to a separation stage, preferably comprising introducing S3 or S3’ in a cold box, obtaining CO in a gas stream SI1 and H2 in a gas stream SI2.

9. The process of any one of claims 1 to 8, wherein e) comprises e-1 ) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2obtained according to d) is / are used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) are used for this mixture; e-2) subjecting at least a portion of the methanol according to e-1) to a partial oxidation reaction, obtaining formaldehyde; e-3) subjecting at least a portion of the formaldehyde obtained according to e-2) to a chemical conversion, being a Reppe reaction, with acetylene, obtaining 1 ,4-butyn- diol; e-4) subjecting at least a portion of the 1 ,4-butyndiole obtained according to e-3) to hydrogenation, more preferably using H2 obtained according to d), obtaining 1 ,4-bu- tanediol; e-5) subjecting at least a portion of the 1 ,4-butanediol obtained according to e-4) to cyclization in presence of a catalyst, obtaining tetra hydrofuran (THF) as a chemical product.

10. The process of claim 9, wherein e) further comprises e-6) subjecting the tetrahydrofuran obtained according to e-5) to polymerization, obtaining poly(tetrahydrofuran) as a chemical product.11 . The process of any one of claims 1 to 8, wherein e) comprises e-1 ’) subjecting benzene to catalytic hydrogenation with at least a portion of SI2 comprising H2 obtained according to d) in the presence of a nickel-, palladium-, or platinum containing catalyst, preferably a nickel-containing catalyst, obtaining cyclohexane; e-2’) subjecting the cyclohexane obtained according to e-1 ’) to oxidation in presence of a catalyst, preferably a metal salt catalyst, obtaining cyclohexanone; e-3’) subjecting the cyclohexanone obtained according to e-2’) to ammoximation reaction in presence of a hydroxylamine, obtaining cyclohexanone oxime; e-4‘) subjecting the cyclohexanone oxime obtained according to e-3‘) to a Beckmann rearrangement, obtaining e-caprolactam; e-5’) subjecting the e-caprolactam obtained according to e-4’) to polymerization in presence of water, obtaining polyamide 6.

12. The process of any one of claims 1 to 8, wherein e) comprises e-1 ”) subjecting a mixture of CO and H2 to a chemical conversion in the presence of a heterogeneous catalyst, obtaining methanol, wherein at least a portion of SI1 comprising CO obtained according to d) and / or at least a portion of SI2 comprising H2 obtained according to d) is used for this mixture, more preferably at least a portion of SI1 obtained according to d) and at least a portion of SI2 obtained according to d) is used for this mixture; e-2”) subjecting at least a portion of the methanol according to e-1 ”) to a partial oxidation reaction, obtaining formaldehyde; e-3”) subjecting aniline and the formaldehyde obtained according to e-2”) to condensation in presence of a catalyst, obtaining methylenedianiline (MDA);e-4”) reacting the methylenedianiline obtained according to e-3”) with phosgene in a reactor unit, obtaining methylene diphenyl diisocyanate (MDI) as the chemical product, wherein the phosgene used according to e-4”) is obtainable or obtained by a process comprising reacting Ch with CO, preferably obtained according to d), in presence of a catalyst, preferably an activated carbon catalyst.

13. A process for preparing a polyurethane, comprising using methylene diphenyl diisocyanate and poly(tetrahydrofuran), wherein the methylene diphenyl diisocyanate is obtained according to e-4”) of the process of claim 12 and / or the poly(tetrahydrofuran) is obtained according to e-6) of the process of claim 10; and / or a process for preparing a textile material, comprising using polyamide 6 and / or a polyurethane, wherein the polyamide 6 is obtained according to e-3’) of the process of claim 11 and / or the polyurethane is obtained according to the said process for preparing a polyurethane.

14. A recycling unit for carrying out the process for preparing CO and H2 from a textile material according to any one of claims 1 to 12, the unit comprising a first gasification reactor being a fluidized bed reactor, the fluidized bed reactor having a bottom portion, a top portion and a middle portion an inlet means for feeding the RDF into the first gasification reactor; optionally an inlet means for feeding the feedstock A into the first gasification reactor; optionally at least one inlet means for feeding the at least one feedstock C into the first gasification reactor; an inlet means for feeding oxygen and steam into the first gasification reactor at the bottom, or middle, portion of said reactor; an outlet means for removing S1 from the first gasification reactor; a second gasification reactor being an entrained flow reactor, having a bottom portion, a top portion and a middle portion; a transfer means for transferring S1 from the first gasification reactor to the second gasification reactor; an inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor; an inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor; optionally an inlet means for feeding the feedstock B into the second gasification reactor; optionally at least one inlet means for feeding the at least one feedstock D into the second gasification reactor; an outlet means for removing S2 from the second gasification reactor at the bottom portion of the reactor; one or more means for operating the purification stage; optionally a means for adjusting the CO to H2 molar ratio in S3;one or more means for operating the separation stage; optionally a means for operating the chemical conversion or the sequence of chemical conversions of SI1 and / or SI2; wherein the inlet means for feeding the RDF into the first gasification reactor, optionally the inlet means for feeding the feedstock A into the first gasification reactor, and optionally the at least one inlet means for feeding the at least one feedstock C into the first gasification reactor preferably comprise a hopper system, and wherein the inlet means for feeding S1 into the second gasification reactor at the top portion of said reactor, the inlet means for feeding oxygen into the second gasification reactor at the top portion of said reactor and optionally the inlet means for feeding the feedstock B and the at least one feedstock D into the second gasification reactor are one single unit, more preferably a nozzle or an atomizer, wherein the nozzle is preferably a three-fluid nozzle and the atomizer is preferably a mixing twin-fluid atomizer.

15. A process, preferably according to any one of claims 1 to 12, comprising the step of converting a chemical material obtainable or obtained by the process according to any one of claims 1 to 12 to obtain a product Q; and / or a process comprising using the recycling unit according to claim 14 to obtain a chemical material; and preferably converting at least a part of the chemical material to obtain a product Q.

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