Process for manufacturing c6−c8 aromatic hydrocarbons from end-of-life vehicles

Abstract

The present invention concerns a process for manufacture of C6−C8 aromatic hydrocarbons from pre-sorted fractions of end-of-life vehicles (first feedstock) using at least one gasifier. Said first feedstock F1 and a second feedstock are converted in at least one gasifier into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6−C8 aromatic hydrocarbons. Next, said C6−C8 aromatic hydrocarbons are removed from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed. Next, an aromatic stream AS and a second liquid stream LR2 are removed from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6−C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6−C8 aromatic hydrocarbons.

Description

Process for manufacturing C6-C8 aromatic hydrocarbons from end-of-life vehiclesTechnical fieldThe process of the present invention relates to the manufacture of C6-C8 aromatic hydrocarbons by gasification of pre-sorted fractions from end-of-life vehicles.Background of the inventionThe requirement to provide base chemicals, monomers and polymers having a recycling content is growing in the chemical industry. In specific sectors such as the automotive market, specific levels of recycling content for polymers are in discussion and will be implemented as regulations sooner or later.Accordingly, there is a need to provide processes in which plastic waste is converted into important base chemicals such as benzene, toluene and xylene isomers having a recycling content. Even more pressing is the need to provide such processes for which feedstocks can be utilized which comprise at least a portion of plastic waste from end-of life vehicles such as plastic waste comprised in automotive shredder residue (ASR). Said base chemicals then serve as a raw material for synthesis of monomers and such monomers as building blocks in polymers of relevance for the automotive market. Several polymer types of relevance for the automotive market comprise monomers which are based on C6-C8 aromatic hydrocarbons. Furthermore, such processes must be tolerant to the high concentration of (mostly) inorganic fillers comprised in plastic waste from end-of-life vehicles. In addition, such process must be scalable and economic because the demand of polymers having a recycling content for use in new vehicles will be high in near future.A method for producing olefins and aromatic compounds from a feedstock is disclosed in US 2014 / 0228606 A1. A hydrocarbon feedstock is converted in the presence of a catalyst composition at a reactor temperature of 420 to 730 °C in a reactor to products of at least one of olefins and aromatic compounds within the reactor, at least some of the products being contained in a liquid product stream. The catalytic composition comprises a fluidized bed catalytic cracking (FCC) catalyst and a ZSM-5 zeolite catalyst. The conversion of said hydrocarbon feedstock can be accomplished within a low residence time on the order of seconds up to 3 min or less. Accordingly, the method disclosed in US 2014 / 0228606 A1 is a fluidized catalytic cracking process which is different form gasification methods in several aspects such as the reaction temperature range and residence time and the presence of specific zeolite catalyst which results in a specific product composition. As described in paragraph

[0108] of said document, the main products produced by saif fluid catalytic cracking process are light gas olefins, aromatics, gasoline or naphtha, diesel, a heavier stream and coke whereas a typical gasification process produces as main products CO, H2, CO2, methane and tar.It is an objective of the present invention to provide a process for manufacturing and separating C6-C8 aromatic hydrocarbons from pre-sorted fractions from end-of-life vehicles.It is a further objective of the present invention to provide monomers M manufactured from said C6-C8 aromatic hydrocarbons.It is a further objective of the present invention to provide polymers P manufactured from said monomers.It is a further objective of the present invention to provide polymers P manufactured from pre-sorted fractions from end-of-life vehicles for new vehicles.It is a further objective to provide a process for recycling of plastic waste comprised in end-of-life vehicles which is applicable to plastic waste having a high filler content in said plastic waste.Summary of the inventionThese objectives are solved by a process for manufacturing a monomer M from pre-sorted fractions of end-of-life vehicles, the process comprising the steps:(a) providing a C6-C8 aromatic hydrocarbon,(b) converting said C6-C8 aromatic hydrocarbon into a monomer M wherein the C6-C8 aromatic hydrocarbon is manufactured by or obtained by the steps(i) providing at least one pre-sorted fraction PSE of end-of-life vehicles as first feedstock F1, wherein said at least one pre-sorted fraction PSE comprises at least one polymer which forms at least one C6-C8 aromatic hydrocarbon in step (ii), providing a second feedstock F2 and optionally a third feedstock F3, wherein at least 10 wt.-%, more preferably at least 15 wt.-% and most preferably at least 20 wt.-% of all feedstocks provided in step (i) are second feedstock F2,(ii) converting said first feedstock F1 and said second feedstock F2 provided in step (I) and said third feedstock F3 optionally provided in step (I) in a first gasifier G1 into a first raw synthesis gas RSG1 , wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6-C8 aromatic hydrocarbons,(ill) removing said C6-C8 aromatic hydrocarbons from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed, wherein said first liquid residue LR1 is enriched in C6-C8 aromatic hydrocarbons and wherein said clean first synthesis gas CSG1 is depleted in C6-C8 aromatic hydrocarbons, and(iv) separating an aromatic stream AS and a second liquid stream LR2 from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6-C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6-C8 aromatic hydrocarbons and wherein said aromatic stream AS is optionally further separated into an aromatic stream ASa, an aromatic stream ASb and an aromatic stream ASc in said aromatic hydrocarbon extraction unit AEU.These objectives are further solved by a chemical plant for manufacture of C6-C8 aromatic hydrocarbons from presorted fractions of end-of-life vehicles, the chemical plant comprisinga. a first gasifier G1, b. optionally a second gasifier, said optional second gasifier downstream of and fluidically connected to said first gasifier G1 , c a gas cleaning unit GCU, said gas cleaning unit GCU downstream of and fluidically connected to said first gasifier G1 and said optional second gasifier G2, and d an aromatic hydrocarbon extraction unit AEU, said aromatic hydrocarbon extraction unit AEU downstream of and fluidically connected to said gas cleaning unit GCU, wherein said first gasifier G1 is a fixed bed gasifier and wherein said optional second gasifier G2 is an entrained flow gasifier.Preferably, said second feedstock F2 is a particulate feedstock having a particle size PS and is selected from the group comprising or more preferably consisting of coal, bio char, wood and combinations thereof.Preferably, no catalyst composition such as a FCC catalyst and hydrogen are purposedly added into the first gasifier G1 before or during step (ii).The process and the chemical plant according to the present invention is suited to fulfil recent requirements concerning the utilization and recycling targets set for end-of-life vehicles and new vehicles. At least a portion of the polymers comprised in end-of-life vehicles, e.g., in the form of automotive shredder residue (ASR) which is utilized as “first feedstock FT are converted by this process into C6-C8 aromatic hydrocarbons which can then be further converted into monomers M and optionally further converted into polymers P. Accordingly, typical polymers comprised in end-of-life vehicles such as poly(azepan-2-one) (polyamide-6, PA6), poly [imino(1 ,6- dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66), (T)PUs, polyisocyanurates, polyureas, poly(ethylene terephthalate) (PET), poly(oxy-1,4-butanediyloxycarbonyl-1 ,4-phenylenecarbonyl) (PBT), other polyesters comprising monomer M benzene-1,4-dicarboxylic acid and polmyers P comprising monomer M styrene can be used in the process according to the present invention as first feedstock F1 for a gasification from which C6-C8 aromatic hydrocarbons having a recycling content are obtained. Said C6-C8 aromatic hydrocarbons having a recycling content can then be converted into monomer M such as azepan-2-one, hexanedioic acid, benzene-1,4- dicarboxylic acid, 1,T-methylenebis(4-isocyanatobenzene), 2-isocyanato-1 -methylbenzene, 3-isocyanato-1- methylbenzene, 4-isocyanato-1 -methylbenzene, 2,4-diisocyanato-1-methylbenzene, 2,6-diisocyanato-1- methylbenzene and styrene, from which alone or in combinations with further monomers M' polymers P such as poly(azepan-2-one) (polyamide-6, PA6), poly[imino(1 ,6-dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66), (T)PUs, polyisocyanurates, polyureas, polyethylene terephthalate) (PET), poly(oxy-1 ,4- butanediyloxycarbonyl-1,4-phenylenecarbonyl) (PBT), other polyesters comprising monomer M benzene-1,4- dicarboxylic acid and polymers P comprising monomer M styrene having a recycling content are obtained. Said polymers P having a recycling content can then be used in new vehicles. Thereby recent and future requirements concerning the utilization and recycling targets set for end-of-life vehicles and new vehicles can be fulfilled.Figure 1 shows the process and chemical plant according to the present invention utilizing a first gasifier G1.Figure 2 shows the process and chemical plant according to the present invention utilizing a first gasifier G1 and a washing liquid WL.Figure 3 shows the process and chemical plant according to the present invention utilizing a first gasifier G1 and a second Gasifier G2.Figure 4 shows the process and chemical plant according to the present invention utilizing a first gasifier G1, a second gasifier G2 and a washing liquid WL.Detailed description of the inventionThe present invention is further described below with reference to the embodiments, but the present invention is not limited to these embodiments, and any modifications of these embodiments, combinations of these embodiments or substitutions within the basic spirit of the present invention are still within the scope of the present invention as claimed.Definitions:In the context of the present description and the accompanying claims, the term "about” preferably means a deviation of the thus described value of ±10 %. In the context of the present invention, the term “combinations thereof is inclusive of one or more of the recited elements. In the context of the present invention, the term “mixture thereof” is inclusive of one or more of the recited elements.The term “downstream of” is defined herein in respect to a succession of unit operations as located next to on the side which is in the flow direction of fluids passing said succession of unit operations.The term “fluidically connected to” in respect to two or more units is defined herein that a fluid such as a particulate solid, liquids, gases, and mixtures thereof can flow from one of such unit to the other such unit and flow through and / or along such an analytical unit. Two units “fluidically connected to” each other are for example connected by one or more pipes which each other or by screw conveyors or by extruders or by solids pumps.“Directly" in respect to “fluidically connected” is defined as fluidically connected by a suitable means such as a pipe. Accordingly, the respective outlet of a first unit is fluidically connected by a suitable means such as a pipe with the respective inlet of a second unit wherein said second unit is downstream of said first unit.“Indirectly" in respect to “fluidically connected” is defined as interrupted by e.g., an additional unit, storage tank(s), transporting a stream by for example by truck or train or in a pipeline.“C6-C8 aromatic hydrocarbons" means benzene, toluene, 1,2-xylene, 1,3-xylene, 1,4-xylene, ethylbenzene, and styrene, "06-08 aromatic hydrocarbons” preferably means toluene, 1 ,2-xylene, 1,3-xylene, 1,4-xylene, and ethylbenzene.“Refuse-derived fuel” (RDF) is defined herein as a fuel produced form various types of waste such as municipal solid waste (MSW), industrial waste or commercial waste. RDF consists largely of combustible components of such waste, as non-recyclable plastics (not including PVC), paper cardboard, labels, and other corrugated materials. These fractions are separated by different processing steps, such as screening, air classification, ballistic separation, separation of ferrous and non-ferrous materials, glass, stones, and other foreign materials and shredding into a uniform grain size, or also pelletized to produce a homogeneous material which can be used as a feedstock for gasification processes (Y. Yang et al., Gasification of refuse-derived fuel from municipal solid waste for energy production: a review, Environmental Chemistry Letters (2021) 19, 2127-2140 (https: / / doi.org / 10.1007 / s10311-020- 01177-5).In step (i) of the process according to the present invention, at least one pre-sorted fraction PSE from end-of-life vehicles is provided as first feedstock F1 , wherein said at least one pre-sorted fraction PSE comprises at least one organic polymer.Said first feedstock F1 comprises at least one pre-sorted fraction PSE of end-of-life vehicles, said pre-sorted fraction PSE of end-of-life vehicles formed by sorting from a non-sorted shredder residue NSR of end-of-life vehicles. Said non-sorted shredder residue NSR comprises metal fragments and / or non-metallic inorganic fragments (such as glass fragments), and fragments of at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.Said first feedstock F1 comprises plastic waste previously comprised in end-of-life vehicles, such as in the plastic waste comprised in automotive shredder residue (ASR) which has been taken from end-of-life vehicles and then presorted to increase the amount of at least one polymer therein and reduce the amount of metals and / or non-metallic inorganic fragments comprised in end-of-life vehicles. Preferably, the first feedstock F1 comprises 1 to 50 wt.-% plastic waste from end-of-life vehicles, most preferably, the first feedstock F1 comprises 5 to 30 wt.-% plastic waste from end-of-life vehicles Plastic waste comprised in end-of-life vehicles is preferably selected from the group comprising polyolefins, polyamides, polyurethanes, polyesters, and mixtures thereof. Most preferably, the plastic waste from end-of-life vehicles comprised in the first feedstock F1 is automotive shredder residue (ASR).The non-sorted shredder residue NSR may further comprise shredded electric and electronic equipment devices (WEEE - waste electric and electronic equipment) and other types of waste which are shredded. Shredded electric and electronic equipment devices (WEEE - waste electric and electronic equipment) preferably comprises epoxy resins originating from printed circuit boards and the like comprised therein. Such WEEE optionally also have been part of the end-of-life vehicles.Said non-sorted shredder residue NSR is sorted to form the pre-sorted fraction PSE of end-of-life vehicles, preferably in this order, by a) optionally further reducing the size of said non-sorted shredder residue NSR and b) sorting out metal fragments and / or non-metallic inorganic fragments from said non-sorted shredder residue NSR.A particularly preferred first feedstock F1 comprising pre-sorted fractions of end-of-life vehicles is pre-sorted automotive shredder residue (ASR) which is described in more detail below:Automotive shredder residue is obtainable, preferably is obtained, by shredding vehicles. Preferably, the automotive shredder residue is obtainable by depollution of the vehicles, dismantling the vehicles, shredding the vehicles, and separating metal particles from the shredded vehicles.The methods described for a) optionally further reducing the size of said metal fragments and / or non-metallic inorganic fragments and fragments of at least one polymer and b) sorting out said metal fragments and / or said non- metallic inorganic fragments in respect to automotive shredder residue (ASR) described below can also be applied to other non-sorted shredder residue NSR provided in step (i) to form at least one pre-sorted fraction PSE of end-of-life vehicles which is depleted in metal fragments and / or in non-metallic inorganic fragments by step b) compared to the non-sorted shredder residue NSR. Non-metallic inorganic fragments are for example glass fragments.The vehicles in automotive shredder residue (ASR) are typically end-of-life vehicles (also called “ELV”), which are typically at least 15 years old. The vehicles can be passenger cars, light-duty or heavy-duty trucks, motorbikes, a utility vehicle, an agricultural vehicle, or recreational vehicles. The vehicle can be an electric vehicle, such as a fully electric vehicle or a hybrid electric vehicle.In depollution of vehicles hazardous liquids such as fuel, lubricating oil, coolants, brake fluids and batteries can be removed from the vehicles prior to shredding.The dismantling of vehicles may comprise selective removal of parts, such as engines, gearboxes, tires, glass, and plastics, for being reused as spare parts for the second-hand market. The dismantling may also comprise the removal of larger plastic components, such as bumpers, dashboard, fluid containers for recycling the plastics separately.The ASR may comprise further waste from other sources. For examples, garbage from the last owners may remain in the trunk or interior of the vehicles. The advantage of the present process is that it can handle broadly varying compositions of the ASR.The shredding can be made with a vehicle shredder machine. Vehicle shredder machines are manufactured in different sizes. Typically, a vehicle shredder machine comprises a heavy fast-turning rotor, which may revolve in avertical or a horizontal plane and is often equipped with swinging hammers. The vehicle shredder machine tears and shreds the car hulk until its parts are reduced to fragments. Then the fragments may pass through grids and leave the rotor housing. The automotive shredder residue represents preferably 10 to 40 wt.-%, more preferably from 15 to 35 wt.-%, and most preferably from 20 to 30 wt -% of the original vehicle weightThe fragments are optionally further reduced in size in step a) to obtain the preferred fragment size of at least 90 wt.- % of the shredder residue fragments formed in step a) are smaller than 5 cm, preferably at least 95 wt.-% smaller than 5 cm and more preferably at least 95 wt.-% are smaller than 3 cm. Optional step a) is preferably omitted in case the non-sorted shredder residue NSR has already the preferred fragment size of at least 90 wt.-% of the shredder residue fragments formed in step a) are smaller than 5 cm, preferably at least 95 wt.-% smaller than 5 cm and more preferably at least 95 wt.-% are smaller than 3 cm.The method employed in optional step a) is selected from the group comprising or consisting of shredding, grinding, milling, sieving, classifying and combinations thereof. Optional step a) may further comprise optical and / or manual sorting to remove fragments too large. Such methods are known to the skilled person and can be adapted to a given non-sorted shredder residue NSR to form at least one pre-sorted fraction PSE of end-of-life vehicles which is then provided in step (i).After shredding and further size reduction in optional step a), the metal fragments such as ferrous and non-ferrous metal fragments and non-metallic inorganics (“inerts”) such as glass or sand can be separated from the shredded vehicles in step b). Step b) comprises at least removing metal fragments and / or glass fragments from said nonsorted shredder residue NSR. Metal fragments usually but not always comprise ferrous metal fragments and nonferrous metal fragments.The ferrous metal fragments can be removed by magnetic separators. The magnetic separators utilize typically the magnetic properties of ferrous metals to attract and separate them from non-magnetic materials. Usually, the material is fed onto a conveyor belt or a vibrating feeder, and as the material moves along the conveyor belt, a powerful magnetic field is generated by the magnetic separator (e.g., the magnetic field is created by passing an electric current through a coil, which produces a magnetic force). When the material passes through the magnetic field, the ferrous metals, being magnetic, can be attracted to the magnetic separator. Once the ferrous metals are attracted to the magnetic separator, they can be separated from the rest of the waste material and collected separately. This can be done using a separate chute or conveyor belt to direct the separated ferrous metals to a designated collection area.The non-ferrous metal fragments can be separated from the shredded vehicles by eddy current separators, by density separation methods (e.g., heavy media si nk / float units), by manual sorting and combinations thereof. Suitable eddy current separators exploit the principle of electromagnetic induction to create eddy currents, which in turn generate a magnetic field that repels non-ferrous metals. Usually, the material is fed onto a conveyor belt or avibrating feeder, and as the material moves along the conveyor belt, an alternating magnetic field is generated by the eddy current separator. When the alternating magnetic field interacts with the conductive non-ferrous metals, such as aluminum or copper, it can induce eddy currents within them due to electromagnetic induction. These eddy currents generate typically their own magnetic fields which create a repulsive force that acts against the magnetic field of the eddy current separator. This repulsion may cause the non-ferrous metals to be propelled away from the separator, diverting them from the rest of the material.The automotive shredder residue preferably comprises up to 15 wt.-%, more preferably up to 10 wt -%, and most preferably up to 5 wt.-% of metal fragments, such as ferrous and non-ferrous metal particles. Typically, 60 to 90 wt.- % of the vehicle weight is metal, which can be separated from the shredded vehicle.Non-metallic inorganics ("inerts”) such as glass or sand are preferably separated by density separation. Suitable methods for density separation are cyclone separation, jigging, air separation, or sink-float separation. The automotive shredder residue may comprise preferably up to 15 wt.-%, more preferably up to 10 wt.-%, and most preferably up to 5 wt-% of glass fragments, e.g., broken window glass fragments.The cyclone separation is usually a method used to separate materials based on their density and size using a device called a cyclone. A cyclone typically consists of a cylindrical body with a conical base and an inlet and outlet at the top. The inlet may be tangentially connected to the body, which creates a swirling motion inside the cyclone. As the material spins inside the cyclone, centrifugal force can be generated which may cause the denser and larger particles to move towards the outer wall of the cyclone, while the lighter and smaller particles tend to stay closer to the center.The jigging separation is a method usually used to separate materials based on their density using a device called a jig, which typically consists of a rectangular or circular container with a screen or mesh on the bottom. The container can be mounted on a frame with a mechanism that causes it to move up and down. The jig can be filled with water, and a pulsating flow of water is introduced from the bottom of the container. The pulsation may cause the material to move up and down in the container. The denser particles may tend to settle faster and move towards the bottom of the container, while the lighter particles tend to stay near the top.The air separation is often based a stream of air, e g., in an air classifier structure which typically consists of a vertical chamber with an inlet at the bottom and an outlet at the top. The chamber may contain a series of vanes or blades that create a centrifugal force that separates the materials. A stream of air is usually introduced from the bottom of the chamber and the air flow causes the material to move upwards and separates it based on its density. The denser particles often tend to move towards the outer wall of the chamber, while the lighter particles tend to stay closer to the center. The separated materials can be collected at different points of the air classifier.The sink-float separation is usually based on the principle that materials with different densities will behave differently when placed in a fluid medium: Dense materials often sink while less dense materials float. The fluid medium can be a heavy liquid, such as water or a specialized solution, or a finely ground powdered material. The liquid is usually chosen to have a density that is between the densities of the materials to be separatedThe automotive shredder residue comprises fragments of various polymeric vehicle parts comprising at least one polymer selected from polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins. Said fragments selected from fragments of bumpers, interior panels, dashboard, cable insulation, electrical insulation, flexible foam seating, foam insulation panels, automotive suspension bushings, electrical potting compounds, car body parts, pillar coverings, spoilers polymer parts coated with automotive paint, wheel covers, gears, bushes, cams, bearings, weatherproof coatings, interior and exterior trims, fuel systems, gear housings, headlamp retainer, engine cover, connector housings, door handles, carburetor components, exterior mirror components, windscreen wiper components, windscreen wiper protective housings, decorative grilles, cover strips, roof rails, window frames, sliding roof frames, antenna cladding covers, front and rear lights, radiator grill and body exterior parts, engine covers, cylinder head covers, intake pipes, cylinder head covers, engine covers, housings for charge air coolers, charge air cooler valves of which preferably at least one member is comprised in the sorted shredder residue SSR.“Contaminated vehicle components” are also suited as first feedstock F1. Such contaminated vehicle components are made from plastic materials and were contaminated by contaminants such as gasoline or diesel because of the yearlong physical and chemical contact between said vehicle parts and the respective contaminants. Contaminated vehicle components are for example gas tanks (made from plastic material such as polyethylene) contaminated with gasoline or diesel (= contaminants). Contaminated vehicle components are preferably dismantled from the respective end-of-life vehicle before shredding of said end-of-life vehicle. The shredded parts of the end-of-life vehicle are defined as automotive shredder residue (ASR), the conversion of ASR into at least one pre-sorted fraction PSE of end-of-life vehicles suited a first feedstock F1 in the process according to the present invention is described above. Accordingly, such contaminated vehicle parts are preferably not comprised in automotive shredder residue (ASR). Dismantling of contaminated vehicle parts can be made by manually by humans and / or automated by robotsIn one aspect of the present invention, contaminated vehicle components are combined with at least one pre-sorted fraction PSE of end-of-life vehicles to form the first feedstock F1 provided in step (i) In another aspect of the present invention contaminated vehicle components are combined with at least one pre-sorted fraction PSE of end-of-life vehicles and shredded waste electric and electronic equipment to form the first feedstock F1 provided in step (i).Polyamides which can be comprised in the at least one pre-sorted fraction PSE of end-of-life vehicles are preferably selected from the group consisting of polyamide 6 (PA6), polyamide 66 (PA66) and mixtures thereof. Such polyamides may comprise fillers.Polyisocyanate polyaddition products which can be comprised in the at least one pre-sorted fraction PSE of end-of- life vehicles are preferably selected from the group consisting of polyurethane (PU), thermoplastic polyurethane (TPU), polyurea, polyisocyanurate (PIR) and mixtures thereof. Such polyisocyanate polyaddition products may comprise fillers.Rubbers which can be comprised in the at least one pre-sorted fraction PSE of end-of-life vehicles are preferably selected from the group comprising natural rubber, styrene-butadiene rubber, butyl rubber, ethylene propylene diene monomer rubber, neoprene, nitrile rubber and silicone rubber.Polyolefins which can be comprised in the at least one pre-sorted fraction PSE of end-of-life vehicles are preferably selected from the group consisting of low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP) and mixtures thereof. Such polyolefins may comprise fillers.The at least one pre-sorted fraction PSE of end-of-life vehicles more preferably comprises at least two different polymers of the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.The automotive shredder residue may comprise up to preferably 15 wt.-%, more preferably up to 10 wt.-%, and most preferably up to 5 wt.-% of wood and cardboard. Such components can remain in the first feedstock F1 for the gasification process in step (iii) because they can also be converted into raw synthesis gas RSG1 comprising C6-C8 aromatic hydrocarbons.The non-sorted shredder residue NSR and / or the at least one pre-sorted fraction PSE of end-of-life vehicles are / is optionally dried before step (I). The first feedstock F1 is preferably pelletized before provided in step (I). More preferably, the first feedstock F1 is preferably pelletized before provided in step (I) to pellets having a particle size PS of at least 3 mm (determined by sieving with sieves having defined mesh sizes) and up to about 50 mm.A second feedstock F2 is also provided in step (i) and fed into the first gasifier G1 in step (ii) together with the first feedstock F1 provided in step (i).Said second feedstock F2 is a particulate feedstock having a particle size PS and is preferably selected from the group comprising and more preferably consisting of coal, bio char, wood and combinations thereof.Said particle size PS of said second feedstock F2 is at least 3 mm (determined by sieving with sieves having defined mesh sizes). Such a minimum size of the second feedstock F2 is required for a stable operation of the first gasifier G1 which is preferably a fixed bed gasifier. Preferably, the upper particle size PS is about 50 mm (determined by sieving with sieves having defined mesh sizes).A second feedstock F2 selected from the group comprising or preferably consisting of coal, bio char, wood and combinations thereof, and having a particle size PS of at least 3 mm (determined by sieving with sieves having defined mesh sizes) is more preferred for a stable operation fixed bed gasifier as first gasifier G1.Preferably, at least 10 wt.-%, more preferably at least 15 wt.-% and most preferably at least 20 wt.-% of all feedstocks provided in step (i) is said second feedstock F2. Thereby, a stable operation of a fixed bed gasifier as first gasifier G1 is archived, particularly in case said second feedstock F2 is a particulate feedstock having a particle size PS and is selected from the group comprising or preferably consisting of coal, bio char, wood and combinations thereof:In case the first gasifier G1 is a fixed bed gasifier, said content of said second feedstock F2 improves the permeability ("macro-porosity”) of the fixed bed comprising or consisting of said mixture of feedstocks F1 and F2 (or, optionally of F1 , F2 and F3). Thereby, gases such as the synthesis gas formed can better flow through said fixed bed.In case the first gasifier G1 is a fluidized bed gasifier, said content of said second feedstock F2 improves the homogeneity of said mixture of feedstocks F1 and F2 (or, optionally of F1 , F2 and F3).Preferably, also the first feedstock F1 has a particle size of at least 3 mm (determined by sieving with sieves having defined mesh sizes). Such a minimum size of the first feedstock F1 is preferred for a stable operation of the first gasifier G1 which is preferably a fixed bed gasifier. Preferably, the upper particle size of the first feedstock F1 is about 50 mm (determined by sieving with sieves having defined mesh sizes). Thereby, a stable operation of a fixed bed gasifier as first gasifier G1 is further improved.Coal is preferably selected from the group comprising or preferably consisting of meta-anthracite, anthracite, semianthracite, low volatile bituminous coal, medium volatile bituminous coal, high volatile A bituminous coal, high volatile B bituminous coal, high volatile C bituminous coal, subbituminous A coal, subbituminous B coal, subbituminous C coal, lignite A, lignite B and mixtures thereof. More preferably, the coal is selected from the group consisting of low volatile bituminous coal, medium volatile bituminous coal, high volatile A bituminous coal, high volatile B bituminous coal, high volatile C bituminous coal, subbituminous A coal, subbituminous B coal, subbituminous C coal, lignite A, lignite B and mixtures thereof. Said terms are in accordance with the respective definition disclosed in ASTM D388-23. Accordingly, bituminous, and anthracitic coals are summarized in ASTM D388-23 in “meta-terms" as "high rank coal", and lignitic and subbituminous coals as "low rank coals". Because real coal feedstocks used for gasification can be composed of more than one of said coal types according to ASTM D388-23, the "meta-terms” "high rank coals” and “low rank coals” are used in the examples section.Coal is optionally pretreated before provided in step (i). Preferably, the coal is pretreated by a method selected from the group comprising or preferably consisting of milling, grinding, classification, drying, pelletizing and combinations thereof, whereby optionally coal dust as a side product is formed. Such pre-treatment methods are known to the skilled person and can be selected and applied for a given type of coal feedstock. Said coal dust can be alsosubjected to the gasification process in the first gasifier G1 as an optional third feedstock F3 and / or the optional second gasifier G2 as an optional fourth feedstock F4 and thereby further increase the yield of C6-C8 aromatic hydrocarbons comprised in the raw synthesis gas RSG1 and / or the second raw synthesis gas RSG2.Biochar is a type of charcoal that is produced through a process called pyrolysis. Pyrolysis involves heating biomass in the absence of oxygen. Biochar is the solid residue that remains after the pyrolysis process. The production of biochar involves heating the biomass to temperatures ranging from 350 to 700 °C in a pyrolysis reactor. During the pyrolysis process, the absence of oxygen prevents the biomass from burning completely and instead promotes the formation of stable carbon compounds, which make up the biochar. The heating process also drives off volatile organic compounds.Biochar suitable as second feedstock F2 can be made from various types of biomass (including wood), agricultural waste, crop residues, forestry waste, animal manure, and sewage sludge.Wood is preferably provided in form of chips and / or pellets as second feedstock F2.Said optional third feedstock F3 is selected from the group comprising or consisting of biomass, refuse-derived fuel (RDF), textiles, dried sewage sludge, pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), tar oils, natural gas, CO2, and mixtures thereof.Preferably, said optional third feedstock F3 is selected from the group consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, municipal solid waste (MSW), CO2, and mixtures thereof.The optional at least one third feedstock F3 is optionally pre-treated before step (i) by a method selected from the group comprising or consisting of sorting, sieving, milling, grinding, pyrolysis, torrefaction, metal sorting and combinations thereof.More preferably, said first feedstock F1 is converted in step (ii) together with a second feedstock F2 which is a particulate feedstock having a particle size PS and is selected from the group comprising or preferably consisting of coal, bio char and wood wherein said particle size PS of said second feedstock F2 is at least 3 mm (determined by sieving with sieves having defined mesh sizes), most preferably the first feedstock F1 is converted in step (ii) together with a second feedstock F2 which is a particulate feedstock having a particle size PS and is selected from the group comprising or preferably consisting of coal, bio char and wood wherein said particle size PS of said second feedstock F2 is at least 3 mm (determined by sieving with sieves having defined mesh sizes) and a third feedstockF3 which comprises most preferably RDF. The yield of C6-C8 aromatic hydrocarbons separated from said first liquid residue LR1 in step (iv) is increasing, when converting said first feedstock F1 together with the second feedstock F2 or together with the second feedstock F2 and the third feedstock F3 in step (ii). Furthermore, a steadier production of raw synthesis gas RSG1 is archived by such feedstock combinations (preferably F1 + F2, more preferably F1 + F2 + F3) because fluctuating amounts and / or calorific value of the first feedstock F1 can be balanced by such feedstock combinations.Preferably, at least 10 wt.-% of all feedstocks provided in step (ii) are second feedstock F2 More preferably, at least 15 wt.-% of all feedstocks provided in step (ii) are second feedstock F2. Most preferably, at least 20 wt.-% of all feedstocks provided in step (ii) are second feedstock F2. The remaining portion are the first feedstock F1 and optionally also the third feedstock F3.In step (ii) of the process according to the present invention, said first feedstock F1 comprising at least one presorted fraction PSE provided in step (i) and the second feedstock F2 are converted in a first gasifier G1 into a first raw synthesis gas RSG1 , wherein said first raw synthesis gas RSG1 comprises CO, H2, C6-C8 aromatic hydrocarbons.Optionally, said first feedstock F1 and said second feedstock F2 and a third feedstock F3 are provided in step (i) and converted in step (ii) in a first gasifier G1 into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, C6-C8 aromatic hydrocarbons.The first feedstock F1 and the second feedstock F2 can be fed into the first gasifier G1 separately or together and thereby converted into a first raw synthesis gas RSG1 , wherein said first raw synthesis gas RSG1 comprises CO, H2, C6-C8 aromatic hydrocarbons. Together includes a) feeding the first feedstock F1 and the second feedstock F2 at the same time into the first Gasifier G1 without pre-mixing the first feedstock F1 and the second feedstock F2 or premixing the first feedstock F1 and the second feedstock F2 before feeding said feedstocks into the first gasifier G1 .In case the first feedstock F1 and the second feedstock F2 are converted in step (ii) together with a third feedstock F3, all three feedstocks can be fed into the first gasifier G1 separately or together (F1 + F2 together and F3 separately or F1 + F3 together and F2 separately or F2 + F3 and F1 separately, or F1 + F2 + F3 together, “feedstock combinations”) and thereby converted into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, C6-C8 aromatic hydrocarbons. Together includes a) feeding said feedstock combinations at the same time into the first Gasifier G1 without pre-mixing or pre-mixing said feedstock combinations before feeding said feedstocks into the first gasifier G1.The first gasifier G1 is preferably a fixed bed gasifier which is best suited for converting at least one pre-sorted fraction PSE from end-of-life vehicles comprised in the first feedstock F1 and the second feedstock F2 by gasification into C6-C8 aromatic hydrocarbons (comprised in the raw synthesis gas RSG1). More preferably, the fixed bed firstgasifier G1 is a fixed bed dry bottom gasifier or a slagging gasifier. Said gasifier types are even more suited for converting at least one pre-sorted fraction PSE from end-of-life vehicles and the second feedstock F2 by gasification into C6-C8 aromatic hydrocarbons. Slagging gasifiers such as the British Gas / Lurgi gasifier (also known as “BGL” gasifier) require less steam to be fed into the gasifier than other types of fixed bed gasifiers. Thereby, a higher temperature is achieved in the combustion zone of the gasifier and the conversion of the at least one pre-sorted fraction PSE from end-of-life vehicles is further increased. Furthermore, a fixed bed dry bottom gasifier G1 or a slagging gasifier G1 enables a higher throughput of pre-sorted fraction PSE from end-of-life vehicles comprised in the first feedstock F1 because drag out of slag which is formed therefrom during the gasification is simpler than in other types of fixed bed gasifiers G1. Thereby, the yield of desired C6-C8 aromatic hydrocarbons is increased.The content of methane comprised in the raw synthesis gas RSG1 formed in the first gasifier G1 may be higher than desired. Furthermore, side products, referred herein as "condensates” and comprising tar, particularly tar oil may also be produced in said first gasifier G1. Accordingly, in a preferred aspect of the present invention, said condensates, particularly tar oil TO, produced as a side product in the first gasifier G1 are / is then used as a feedstock for a second gasifier G2 which is preferably an entrained flow gasifier. Said condensates, particularly tar oil TO, are / is converted in the second gasifier G2 by a gasification process into a raw synthesis gas RSG2 which preferably comprises methane at a higher concentration than in the raw synthesis gas RSG1. When both raw synthesis gas streams RSG1 and RSG2 are combined, the resulting combined raw synthesis gas RSG12 has a lower methane concentration than the raw synthesis gas RSG1 , which is a desired effect. Furthermore, the yield of 06-08 aromatic hydrocarbons formed by gasification of the first feedstock F1 comprising at least one pre-sorted fraction PSE provided in step (i) is further increased thereby, which is a particularly desired effect.In one aspect of the present invention, "condensates” are formed as a side product during step (ii) in said first gasifier G1 from which condensates preferably tar oil TO is separated in an optional condensate separation unit CSU. Said condensates, preferably said tar oil TO is separated from said condensates are / is then fed as a feedstock into an optional second gasifier G2 which is preferably an entrained-flow gasifier and converted onside said optional second gasifier G2 into a second raw synthesis gas RSG2. Said second raw synthesis gas RSG2 can be combined with the first raw synthesis gas RSG1 before cleaning said first raw synthesis gas RSG1 and said second raw synthesis gas RSG2 in step (iii). Thereby, the yield of C6-C8 aromatic hydrocarbons comprised in the resulting raw synthesis gas streams RSG1 and RSG2 and the clean synthesis gas stream CSG is increased. Furthermore, a higher portion of the at least one pre-sorted fraction PSE from end-of-life vehicles comprised in the first feedstock F1 and provided in step (i) is converted into the desired C6-C8 aromatic hydrocarbons then comprised in the first liquid residue LR1.An overview of gasifiers G, especially entrained flow gasifiers G and plasma gasifiers G is for example provided in James G. Speight, Handbook of Gasification Technology, Scrivener Publishing and Wiley, 2020, chapter 8.4.2, pages 259 to 262.The temperature inside the optional entrained flow gasifier G2 preferably ranges from 1000 to 1500 °C, more preferably from 1100 to 1450 °C and most preferably from 1200 to 1400 °C. The pressure inside said optional entrained flow gasifier preferably ranges from 1 to 55 bar(abs.), more preferably from 5 to 50 bar(abs.) and most preferably from 20 to 45 bar(abs.)Optionally, a fourth feedstock F4 is converted in said optional second gasifier G2 together with said condensates, preferably said tar oil TO separated from said condensates, into raw synthesis gas RSG2. Said optional fourth feedstock F4 is a feedstock which is preferably liquid or gaseous at room temperature or at an elevated temperature such as 80 °C.Said optional fourth feedstock F4 is more preferably selected from the group comprising or preferably consisting of pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, tar oils from other sources than the first gasifier G1 , natural gas, coal dust, CO2, and mixtures thereof.Optional fourth feedstocks F4 such as bio-based oils and pyrolysis oils are preferably pre-heated and / or pressurized before fed into the optional second gasifier G2. The optional fourth feedstock F4 is preferably pressurized to > 10 bar(abs.), more preferably > 20 bar(abs.) and most preferably > 40 bar(abs.) before fed into the optional second gasifier G2. Suitable means for pre-heating and / or pressurizing the optional forth feedstock F4 for feeding into the optional second gasifier G2 are known in the art, comprise for example flaps and locks but also annual gaps as part of a burner such as in twin fluid atomizers, pressure nozzles and pressure atomizers, and can be adapted to a given fourth feedstock F4 and / or second gasifier G2 type by the skilled person.Optional addition of a fourth feedstock F4 is preferred because thereby the desired constant operation conditions in said entrained flow gasifier G2 can be better maintained and the desired C6-C8 aromatic hydrocarbons and raw synthesis gas RSG2 having the desired molar ratio CO : H2 is formed.Preferably, the tar oil TO and the optional fourth feedstock F4 are fed into the entrained flow gasifier G2 via at least one burner whereby said at least one burner comprises one annular gap for the tar oil TO and a separate annular gap through which the optional fourth feedstock F4 is fed. Steam, preferably mixed with oxygen is co-fed into the entrained flow gasifier G2 through a separate annular gap in said at least one burner.A fourth feedstock F4 is preferred for a stable operation of the optional second gasifier G2 in case the amount of tar oil TO provided as a side product of the first gasifier G1 falls below a critical value. Preferably, said optional fourth feedstock F4 is co-fed into the optional second gasifier in case the minimum feedstock load (about 25 to 30 % of the optimum feedstock load of a given second gasifier G2) is reached or be lower because of insufficient tar oil TOsupply from the first gasifier G1. Said minimum feedstock load is required for a stable operation of and synthesis gas production in said optional second gasifier G2.In step (ill) of the process according to the present invention, said C6-C8 aromatic hydrocarbons comprised in the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2 in case an optional second gasifier G2 is also used, are removed from said first raw synthesis gas RSG1 and / or said raw synthesis gas RSG2.In principle, C6-C8 aromatic hydrocarbons can be removed from the raw synthesis gas RSG1 and / or RSG2 by different gas cleaning process such as condensation, absorption (chemical absorption and / or physical separation), adsorption, filtration (e.g., membrane filtration). The skilled person can select from such processes and adapt the selected process to a specific raw synthesis gas composition and other parameters.C6-C8 aromatic hydrocarbons can be condensed from raw synthesis gas by cooling down said raw synthesis gas below the boiling point of the individual components of said C6-C8 aromatic hydrocarbons. Thereby, the C6-C8 aromatic hydrocarbons become liquid and the remaining portions of the raw synthesis gas, (CO, H2 and other gases) stay in the gas phase. Thereby, C6-C8 aromatic hydrocarbons can be separated from raw synthesis gas.Adsorption methods such as solid bed adsorption involve the use of specialized adsorbents, such as activated carbon, zeolites, or molecular sieves, to remove 06-08 aromatic hydrocarbons from raw synthesis. The raw synthesis gas is passed through a bed of adsorbent material, which selectively adsorbs 06-08 aromatic hydrocarbons while allowing the clean synthesis gas to pass through. The adsorbent is preferably periodically regenerated by heating or purging with an inert gas to release the captured acid gases. The selection of the appropriate adsorbent (e.g., activated carbon, zeolites, or molecular sieves) for the removal of 06-08 aromatic hydrocarbons depends on factors such as the specific composition of the raw synthesis gas RSG1 and / or RSG2, the required purity levels, and the economics of the process. The regeneration of the adsorbent material is also an important consideration, as it affects the overall cost and environmental impact of the process.Membrane separation is a technology that utilizes selective permeable membranes to separate C6-C8 aromatic hydrocarbons from raw synthesis based on size, solubility, or diffusivity For example, gases such as CO, H2, being smaller molecules, can be selectively permeated through the membrane, while the C6-C8 aromatic hydrocarbons are retained This method offers advantages such as simplicity, compactness, and low energy requirements.Preferably, said C6-C8 aromatic hydrocarbons comprised in the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2 in case an optional second gasifier G2 is also used, are separated from said first raw synthesis gas RSG1 and / or said raw synthesis gas RSG2 by a gas cleaning process GC in a gas cleaning unit GCU, wherein said first raw synthesis gas RSG1 and / or said raw synthesis gas RSG2 is contacted with at least one washing liquid WL, whereby a clean first synthesis gas CSG and a first liquid residue LR1 are formed, wherein said first liquid residue LR1 comprises C6-C8 aromatic hydrocarbons.The at least one washing liquid WL separates CO2 and C6-C8 aromatic hydrocarbons comprised in the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2 therefrom, whereby C6-C8 aromatic hydrocarbons are absorbed (chemically and / or physically absorbed) by the at least one washing liquid WL. Optionally further components other than CO and H2 such as sulfur oxides which may be comprised in the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2 are / is separated therefrom.Preferred gas cleaning process GO with at least one washing liquid WL in the gas cleaning unit GCU comprise amine scrubbing. Amine scrubbing, also known as amine gas treating or gas sweetening, is a suitable gas cleaning process GO for acid gas removal and separation of C6-C8 aromatic hydrocarbons from raw synthesis gas RSG1 and / or RSG2. In this process, raw synthesis gas is brought into contact with a solution of amines and / or alkanolamines, such as monoethanolamine (MEA) or diethanolamine (DEA). The amine and / or alkanolamine solution reacts with the acid gases, selectively absorbing and removing them from the raw synthesis gas. Furthermore, C6-C8 aromatic hydrocarbons comprised in the raw synthesis gas are condensed from said raw synthesis gas and thereby separated therefrom. The loaded amine and / or alkanolamine solution is then regenerated by heating, releasing the captured acid gases for further processing or disposal. Furthermore, the unipolar C6-C8 aromatic hydrocarbons are separated as a liquid phase LP1 from the more polar at least one washing liquid WL forming a liquid phase LP2 and can then be separated by standard methods for separating immiscible liquid phases from each other, e.g., by gravitation in a settler unit. Such separation methods are known to the skilled person and can applied accordingly to a given separation problem.Preferred gas cleaning process GC with at least one washing liquid WL in the gas cleaning unit GCU further comprise physical solvent absorption methods such as the Selexol™ which utilizes a mixture of dimethylethers of polyethyleneglycol as washing liquid WL and the Rectisol® process which utilizes methanol as washing liquid WL. In general, such alcohols and / or ethers are suited as washing liquid WL in such physical solvent absorption methods. Such washing liquids WL have a high affinity for C6-C8 aromatic hydrocarbons and can selectively absorb them from the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2.In another preferred gas cleaning process GC with at least one washing liquid WL in the gas cleaning unit GCU is disclosed in WO 2018 / 208144 A1. In said, the first raw synthesis gas RSG1 and / or the raw synthesis gas RSG2 is contacted with a washing liquid WL in step (a), at a temperature of 15-250 °C, to obtain a clean first synthesis gas CSG, which is depleted in C6-C8 aromatic hydrocarbons, and a first liquid residue LR1 wherein the C6-C8 aromatic hydrocarbons are dissolved. The first liquid residue LR1 is preferably stripped in step (b) with a stripping gas comprising at least 50 Vol.-% steam, to obtain a stripped washing liquid WL which is advantageously reused in step (a) and a loaded stripping gas comprising the aromatic compounds. The aromatic compounds are separated from the loaded stripping gas in an aromatic hydrocarbon extraction unit AEU for example by condensation of the steam and / or the aromatic compounds comprised in the loaded stripping gas to obtain an immiscible composition andisolating the C6-C8 aromatic hydrocarbons therefrom. The washing liquid WL comprises or consists of organic polysiloxanes, preferably organic polysiloxanes comprising aryl groups.Preferably, the at least one washing liquid WL is selected from the group comprising amines, alkanolamines, alcohols, ethers, organic polysiloxanes, and mixtures thereof. More preferably, the at least one washing liquid is selected from the group consisting of amines, alkanolamines, alcohols, ethers, organic polysiloxanes, and mixtures thereof. Most preferably, the at least one washing liquid is selected from the group consisting of monoethanolamine, diethanolamine, methanol, dimethylethers of polyethyleneglycol, organic polysiloxanes comprising aryl groups, and mixtures thereof.In step (iv) of the process according to the present invention, said C6-C8 aromatic hydrocarbons are separated from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU which is downstream of the gas cleaning unit GCU and in which a C6-C8 aromatic hydrocarbon-rich stream AS is separated from said first liquid residue LR1. The remaining portion of said first liquid residue LR1 leaves said aromatic hydrocarbon extraction unit AEU and is depleted in C6-C8 aromatic hydrocarbons.Preferably, C6-C8 aromatic hydrocarbons comprised in stream AS are preferably further separated in said aromatic hydrocarbon extraction unit AEU into a stream ASa which is enriched in benzene, a stream ASb which is enriched in toluene, a stream ASc which is enriched in C8 aromatic hydrocarbons (ethylbenzene, 1 ,2-xylene, 1 ,3-xylene, 1 ,4- xylene) and said second liquid residue LR2 which is depleted in C6-C8 aromatic hydrocarbons. 1 ,4-Xylene can then be separated from stream ASc by standard methods knwon in the art such as distillation.The aromatic hydrocarbon extraction unit AEU can be any unit operation suitable to separate C6-C8 aromatic hydrocarbons comprised in the first liquid residue LR1 into a stream AS and a second liquid residue LR2 and / or a stream ASa, a stream ASb, a stream ASc and said second liquid residue LR2. For example, the aromatic hydrocarbon extraction unit AEU can comprise at least one selective adsorption unit operation, at least one selective absorption unit operation, at least one extractive distillation unit operation, at least one solvent extraction followed by distillation and combinations thereof. Suitable solvents for extraction comprise solvents having a higher boiling point than C6-C8 aromatic hydrocarbons such as N-methylpyrrolidone and morpholine.Suitable aromatic hydrocarbon extraction units AEU are commercially available, for example the Morphylane® extractive distillation process by Uhde, Sulfolan® process by Shell-UOP (using tetrahydrothiophene dioxide as extraction solvent), Arosolvan® process by Lurgi (using N-methylpyrrolidone as solvent), Morphylex® process by Krupp-Koppers (using N-formylmorpholine as solvent), Formex® process by Snamprogetti (using N-formylmorpholine as solvent), IFP process by IFP (using dimethyl sulfoxide as solvent) and Mofex® process by Leunawerke (using methylformamide as solvent).The stream ASa preferably comprises at least 90 wt.-% benzene, more preferably at least 95 wt.-% benzene and most preferably at least 99 wt.-% benzene. The stream ASb preferably comprises at least 90 wt.-% 1- methylbenzene, more preferably at least 95 wt.-% 1 -methylbenzene and most preferably at least 99 wt.-% 1- methylbenzene. The stream ASc preferably comprises at least 90 wt.-% of xylene isomers, more preferably at least 93 wt.-% of xylene isomers. “Xylene isomers” comprise 1,2-xylene, 1,3-xylene and 1,4-xylene.The C6-C8 aromatic hydrocarbons comprised in the first liquid residue LR1 can also be separated therefrom in an aromatic hydrocarbon extraction unit AEU by the following steps: a) contacting the first liquid residue LR1 with a stripping gas SG, said stripping gas, preferably comprising at least 50 Vol.-% steam, to obtain a loaded stripping gas LGS, said loaded stripping gas LGS comprising C6-C8 aromatic hydrocarbons separated from said first liquid residue LR1 and a stripped washing liquid WL previously comprised in said first liquid residue LR1 and b) separating the C6-C8 aromatic hydrocarbons from the loaded stripping gas LSG formed in step a) by condensation of the C6-C8 aromatic hydrocarbons comprised in the loaded stripping gas LSG therefrom.Optionally, the one or both streams ASb and / or ASc are then fed into a hydroalkylation unit HAU whereby toluene and / or xylene isomers and / or ethylbenzene are converted into benzene. Accordingly, the benzene yield can be increased thereby. Hydroalkylation of alkyl-substituted benzene-derivatives into benzene and corresponding hydroalkylation units HAU are known in the art and are for example described in Ullmann's Encyclopedia of Industrial Chemistry, Vol. 5, Chapter “Benzene” by H. O. Folkins, pages 246-251, 2012 and in Industrielle organische Chemie, 3rdEd., K. Weissermel, H.-J. Arpe, pages 351 -352, 1988 which are both incorporated by reference herein.Next, the C6-C8 aromatic hydrocarbons separated from the first liquid residue LR1 are provided in step (a) and converted into at least on monomer M in step (b). Said monomer M is preferably selected from the group comprising or preferably consisting of azepan-2-one, hexanedioic acid, benzene-1 ,4-dicarboxylic acid, 1 ,1 '-methylenebis(4- isocyanatobenzene), 2-isocyanato-1 -methylbenzene, 3-isocyanato-1-methylbenzene, 4-isocyanato-1- methylbenzene, 2,4-diisocyanato-1-methylbenzene, 2,6-diisocyanato-1-methylbenzene and styrene.Benzene separated in step (iv) is preferably converted in step (b) into a monomer M selected from the group comprising or preferably consisting of azepan-2-one, hexanedioic acid, and 1 ,1 '-methylenebis(4- isocyanatobenzene).1 -Methylbenzene separated in step (iv) is preferably converted in step (b) into a monomer M selected from the group comprising or preferably consisting of 2-isocyanato-1 -methylbenzene, 3-isocyanato-1 -methylbenzene, 4-isocyanato- 1 -methylbenzene, 2,4-diisocyanato-1-methylbenzene, 2,6-diisocyanato-1-methylbenzene and styrene.1 ,4-Xylene separated in step (iv) as stream ASc or from stream ASc in a further step (e.g., by distillation) is preferably converted in step (b) into the monomer M benzene-1 ,4-dicarboxylic acid.Ethylbenzene optionally separated in step (iv) is preferably converted in step (b) into monomer M styrene by methods known in the art.Benzene can be converted into azepan-2-one or hexanedioic acid in step (b) of the process according to the present invention by the following method: First, benzene separated in step (iv) from the first liquid residue LR1 (e.g., from stream ASa) is provided in step (a) and reacted with hydrogen. Hydrogen from standard sources used in chemical plants can be used. Preferably, the hydrogen or at least a portion thereof is “green hydrogen”, generated for example by electrolysis of water using electricity generated from renewable energy sources (e.g., solar energy, wind energy, tidal energy, and nuclear energy) and / or low-carbon energy sources and / or a methane pyrolysis, preferably a methane pyrolysis using at least partially methane from a renewable source. Methane from a renewable source comprises biomethane. Next, the benzene provided in step (a) and hydrogen are contacted with each other in the presence of a first heterogeneous catalyst whereby cyclohexane is formed. Cyclohexane can be manufactured by a hydrogenation reaction from said benzene by a catalytic hydrogenation reaction in the presence of hydrogen. Suitable catalysts comprise nickel, platinum, or palladium on a support such as alumina, or a Raney nickel catalyst. The process temperature is about 300 °C or less at a pressure of about 20 to about 30 MPa. Further details are for example disclosed in M. L. Campbell, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 11 , Chapter “Cyclohexane”, pages 44 to 46, 2011 and the references cited therein.Next, the cyclohexane is oxidized in the presence of oxygen and, optionally, a second heterogeneous catalyst, whereby cyclohexanone is formed. Cyclohexanone can be manufactured from cyclohexane for example by liquidphase oxidation in the presence of air in an uncatalyzed or catalyzed reaction (e.g., cobalt catalyst as second heterogeneous catalyst) at a temperature in the range of about 140 to about 180 °C and a pressure in the range of 0.8 to about 2 MPa. Cyclohexanone can also be manufactured from cyclohexane in the presence of anhydrous (meta-)boric acid. Cyclohexanol is produced by such processes as a side product. Such mixtures comprising cyclohexanone and cyclohexanol are also known as “KA oil” (“ketone-alcohol oil”) and “AnoIon”. Suitable manufacturing processes for cyclohexanone from cyclohexane such as the above discussed ones are for example disclosed in M T. Musser, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 11, Chapter “Cyclohexanol and Cyclohexanone”, pages 51 to 54, 2011 and the references cited therein.Azepan-2-one is then formed from cyclohexanone by converting cyclohexanone to cyclohexanone oxime and then converting the cyclohexanone oxime into azepan-2-one. Azepan-2-one (caprolactam) is manufactured from cyclohexanone via cyclohexanone oxime as an intermediate. Next, cyclohexanone oxime is subjected to a Beckmann rearrangement by which azepan-2-one is formed. Cyclohexanone oxime can be for example formed from cyclohexanone in the presence of ammonium hydroxylammonium sulfate or by an ammoximation of cyclohexanone in the presence of ammonia and hydrogen peroxide. Azepan-2-one can be formed from cyclohexanone oxime by a Beckmann rearrangement. The Beckmann rearrangement reaction can be performed in the presence of a catalyst either in liquid phase or gas phase. For example, fuming sulfuric acid or oleum is used as a catalyst in liquid phaseBeckmann rearrangement followed by a neutralization reaction and separation of the azepan-2-one which is then purified in further process steps. Such manufacturing methods for azepan-2-one from cyclohexanone are for example disclosed in J. Tinge, M. Groothaert, H. o. h. Veld, J. Ritz, H. Fuchs, H. Kieczka, W. C. Moran, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Caprolactam", pages 4 to 16, 2018 and the references cited therein.Hexanedioic acid can be manufactured from cyclohexanone by oxidation in the presence of nitric acid, for example at temperature between about 60 to 80 °C and a pressure of about 0 1 to about 0.4 MPa in the presence of a coppervanadium catalyst Optionally, a second reactor operating at a temperature from about 110 to about 120 °C is added to the process. Next, nitrogen oxides are removed with air and nitric acid is recovered from such mixtures.Hexanedioic acid can then be separated by crystallization and purified by recrystallization. Suitable manufacturing processes for hexanedioic acid cyclohexanone are for example described in M.T. Musser, Ullmann’s Encyclopedia of Industrial Chemistry, Vol. 11, Chapter “Adipic Acid”, pages 2 to 5, 2005 and the references cited therein.Isocyanate derivatives of benzene and 1 -methylbenzene which are suitable as monomers M for the manufacture of polymers P can be manufactured in step (b) from benzene and 1 -methylbenzene separated in step (iv) from the first liquid residue LR1 (e.g., from stream ASb) as follows:In step (b) of the process according to the present invention, benzene or 1 -methylbenzene is contacted with the mixture of nitric acid and sulfuric acid whereby nitrobenzene or a nitro-derivative of 1 -methylbenzene is formed, wherein the nitro-derivative of 1 -methylbenzene is preferably selected from the group consisting of 2-nitro-1- methylbenzene, 3-nitro1 -methylbenzene, 4-nitro1-methylbenzene, 2,4-dinitro1 -methylbenzene, 2,6-dinitro1- methylbenzene and mixtures thereof. Benzene or 1 -methylbenzene are converted to nitrobenzene or (di)nitro derivatives of 1 -methylbenzene by direct nitration in liquid phase using a mixture of nitric acid and sulfuric acid (“nitrating acid"). The nitration reaction can be made by an isothermal reaction at a temperature of about 50 to about 100 °C and ambient pressure in a cascade of reactors (stirred cylindrical or tubular) or by an adiabatic reaction in a cascade of stirred reactors or a jet impingement reactor at a temperature in the range of about 90 to about 190 °C and ambient pressure or increased pressure such as 1.5 bar, 2 bar or even higher pressure such as 5 bar or 10 bar.Next, the nitrobenzene or nitro-derivative of benzene or 1 -methylbenzene, preferably the mono-nitro-derivatives of the aforementioned, is hydrogenated in the presence of hydrogen and, optionally, a catalyst, whereby aniline or an amino-derivative of 1 -methylbenzene is formed, wherein the amino-derivative of 1 -methylbenzene is preferably selected from the group consisting of 2-amino-1 -methylbenzene, 3-amino-1 -methylbenzene, 4-amino-1- methylbenzene, 2, 4-amino-1 -methylbenzene, 2,6-amino-1-methylbenzene and mixtures thereof. Aniline is manufactured from benzene via nitrobenzene, (di)amino-derivatives of 1 -methylebenzene are manufactured via (di)nitro-l -methylbenzene derivatives manufactured from 1 -methylbenzene. Hydrogen used can be in principle hydrogen generated from any known source and by any known method. Preferably, said hydrogen is preferably “blue hydrogen" (formed by steam reforming and / or autothermal reforming of natural gas whereby the CO2 formed during said reactions is captured and stored or otherwise used), more preferably “green hydrogen” which is generated forexample by electrolysis of water using electricity generated from renewable energy sources (e.g., solar energy, wind energy, tidal energy, and nuclear energy) and / or low-carbon energy sources and / or formed by a methane pyrolysis, preferably a methane pyrolysis using at least partially methane from a renewable source. Methane from a renewable source comprises biomethane. Hydrogen can also be provided as a side product of pyrolysis of plastic waste such as mixed plastic waste and / or end-of-life tires. Nitrobenzene or the (di)nitro derivative of 1 -methylbenzene is catalytically hydrogenated to aniline or to a (di)amino derivative of 1 -methyl benzene in vapor phase or liquid phase Fixed-bed or fluidized-bed reactors can be used for the gas-phase hydrogenation of nitrobenzene to aniline and of (di)nitro derivatives of 1 -methylbenzene to (di)amino derivatives of 1 -methylbenzene in the presence of at least one catalyst. The at least one catalyst is preferably a copper and / or palladium catalyst on a support (e.g., activated carbon or oxide(s) such as alumina or silica) and optionally further comprises elements such as lead, vanadium, phosphorous, chromium as modifiers or promoters. One particular gas-phase process uses a copper catalyst on a silica support promoted with chromium, zinc and barium. In case of a catalytic gas-phase hydrogenation, nitrobenzene, or a (di)nitro derivative of 1 -methylbenzene is preferably hydrogenated in the presence of hydrogen and of at least one catalyst in a fluidized bed, preferably at a temperature of about 250 to about 300 °C. The pressure preferably ranges from about 400 to about 1000 kPa. The product gas stream is then cooled down and aniline or the (di)amino derivative of 1 -methylbenzene which is then separated, preferably in a liquid-gas separator, from the product stream. Liquid-phase hydrogenation of nitrobenzene to aniline or a (di)nitro derivative of 1 -methylbenzene to the respective (di)amino derivative of 1 -methylbenzene can be for example operated in a temperature range of about 90 to about 200 °C. Preferably, the pressure ranges from about 100 to about 600 kPa. For example, slurry- or fluidized-bed reactors can be used for the liquid-phase hydrogenation of nitrobenzene in the presence of hydrogen and at least one catalyst. Suitable catalysts comprise nickel on a support such as for example kieselguhr. Further details of the manufacture of aniline from benzene are for example disclosed in G. Booth, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 24, Chapter "Nitro Compounds, Aromatic”, pages 305 to 309, 2012 and the references cited therein and T. Kahl, K.-W. Schroder, F. R. Lawrence, W. J. Marshall, H. Hoke, R. Jackh, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 3, Chapter "Aniline”, pages 467 to 470, 2012 and the references cited therein. Further details of the manufacture of (di)amino derivatives of 1-methylbenzene from 1 -methylebenzene by catalytic hydrogenation are for example disclosed in G. Booth, Ullmann's Encyclopedia of Industrial Chemistry, Vol 24, Chapter “Nitro Compounds, Aromatic”, pages 309 to 313, 2012 and the references cited therein and P. F Vogt, J J Gerulis, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 2, Chapter “Amines, Aromatic", pages 707 to 710, 2012 and the references cited therein.The monomer M 1,T-Methylenebis(4-isocyanatobenzene) can be manufactured from aniline via the diamine precursor 1,1 '-methylenebis(4-aminobenzene). First, two equivalents of aniline are condensed with formaldehyde, preferably in the presence of hydrochloric acid as a catalyst, to form the diamine precursor 1 ,1 '-methylenebis(4- ami nobenzene). Next, 1 ,1 '-methylenebis(4-aminobenzene) is phosgenated with phosgene to form different isomers of 1,1 '-methylenebis(isocyanatobenzene). The phosgenation of 1,r-methylenebis(4-aminobenzene) can be for example made in liquid phase using an aromatic solvent in a batch process or a continuous process. The desired 1, 1 '-methylenebis(4-isocyanatobenzene) is then separated from the phosgenation reaction products by a continuousthin-film distillation and / or by crystallization. Both processes are known as "splitting" (or, respectively, the equipment known as "splitters"). In addition to 1,1 '-methylenebis(isocyanatobenzene) also condensation products thereof can be formed thereby which are poly-isocyanate derivatives of benzene. The residual crude product which comprises or consists of oligomeric 1,1 '-methylenebis(4-isocyanatobenzene) can be for example used for manufacture of rigid polyurethane or polyisocyanurate foams. The residual crude product is for example marketed as polymeric 1, 1 '- methylenebis(4-isocyanatobenzene) (“PMDI”, poly-isocyanate derivatives of benzene) and contains, next to a residual level of monomers, oligomers and polymers of 1, 1 '-methylenebis(4-isocyanatobenzene) with a broader distribution of chain lengths. Different PMDI grades vary by viscosity, functionality, and the like. PMDI also has various applications, such as polyisocyanurate rigid insulation foams from high viscous PMDI or such as polyurethane rigid insulation foams, woodbinders (e.g., particle board, OSB, MDF), appliances (fridges, freezers, cold chain in general), pipe insulation, transportation from low viscous PMDI. The preparation of such diamine precursors from aniline and their phosgenation to 1,1 '-methylenebis(4-isocyanatobenzene) is for example described in C. Six, F. Richter, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 20, Chapter "Isocyanates, Organic", pages 70 to 76, 2012 and the references cited therein.Di- and poly-isocyanate derivatives of benzene, 1 -methylbenzene are manufactured from (di)amino derivatives of 1- methylbenzene by phosgenation with phosgene. The phosgenation of (di)amino derivatives of benzene and 1- methylbenzene can be for example made in liquid phase using an aromatic solvent in a batch process or a continuous process. The desired di- and / or poly-isocyanate derivative of benzene and 1 -methylbenzene is then for example separated from the phosgenation reaction products by a continuous thin-film distillation and / or by crystallization. Both processes are known as "splitting" (or, respectively, the equipment known as "splitters"). The manufacture of di- and poly-isocyanate derivatives of benzene and 1 -methylbenzene from benzene or 1- methylbenzene including the phosgenation of (di)amino derivatives of benzene and 1 -methylbenzene to di- and polyisocyanate derivatives of 1 -methylbenzene is for example described in C. Six, F. Richter, Ullmann's Encyclopedia of Industrial Chemistry, Vol. 20, Chapter "Isocyanates, Organic”, pages 70 to 76, 2012 and the references cited therein. The amino derivative of benzene is aniline, and most preferably, aniline is converted into 1 , 1 '-methylenebis(4- aminobenzene) which can be then utilized as starting materials for manufacture of 1 ,1 '-methylenebis(4- isocyanatobenzene) therefrom. The (di)amino derivatives of 1 -methylbenzene are preferably selected from the group consisting of 2-amino-1-methylbenzene, 3-amino-1-methylbenzene, 4-amino-1 -methylbenzene, 2,4-diamino-1- methylbenzene, 2,6-diamino-1-methylbenzene, and mixtures thereof. Most preferably, the (di)amino derivatives of 1- methylbenzene is 2, 4-diamino-1 -methylbenzene The di-isocyanate derivatives of 1 -methylbenzene are preferably selected from the group consisting of 2-isocyanato-1-methylbenzene, 3-isocyanato-1 -methylbenzene, 4-isocyanato- 1 -methylbenzene, 2, 4-diisocyanato-1 -methylbenzene and 2, 6-diisocyanato-1 -methylbenzene and mixtures thereof. Most preferably, the (di)isocyanate derivative of 1 -methylbenzene is 2, 4-diisocyanato-1 -methylbenzene.Benzene-1,4-dicarboxylic acid is manufactured by conversion of 1 ,4-xylene which is separated from the first liquid residue LR1 in step (iv) (e.g., by distillation from stream ASc) and provided in step (a). Several methods such as the Amoco process (chapters 3.2 and 3.3), multistage oxidation (chapter 3.4) and the Dynamit Nobel (Witten) process(chapter 3.5) are described in Ullmann’s Encyclopedia of Industrial Chemistry, chapter "Terephthalic Acid, Dimethyl Terephthalate, and Isophthalic Acid”, R. A. F. Tomas, J. C. M. Bordado, J. F. P. Gomes, R. J. Sheehan, Wiley-VCH GmbH Weinheim, 2024, pages 3 to 13 (DOI: 10.1002 / 14356007.a26_193.pub3).Optionally, at least a portion of the monomer M formed in step (b) is converted into a polymer P in optional step (c): azepan-2-one formed as monomer M in step (b) from benzene separated in step (iv) from the first liquid residue LR1 is preferably converted in optional step (c) into poly(azepan-2-one) (polyamide-6, PA6) as polymer P. Hexanedioic acid formed as monomer M in step (b) from benzene separated in step (iv) from the first liquid residue LR1 is preferably converted together with 1,6-hexamethylenediamine in optional step (c) into poly[imino(1 ,6- dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66) as polymer P. Iso-cyanate derivatives benzene and 1-methylbenzene formed as monomers M in step (b) from benzene and 1 -methyl benzen separated in step (iv) from the first liquid residue LR1 is / are preferably converted in optional step (c) together with additional monomers / building blocks into (T)PUs, polyisocyanurates, and polyureas. Benzene-1 ,4-dicarboxylic acid formed as monomer M in step (b) from 1 ,4-xylene separated in step (iv) from the first liquid residue LR1 is preferably converted in optional step (c) together with ethane-1 ,2-diol into polyethylene terephthalate) (PET) or together with butane-1 ,4- diol into poly(oxy-1 ,4-butanediyloxycarbonyl-1,4-phenylenecarbonyl) (PBT) or other polyesters comprising benzene- 1 ,4-dicarboxylic acid as monomer M.Azepan-2-one manufactured on step (b) from benzene separated in step (iv) from the first liquid residue LR1 can be for example converted in optional step (c) into poly-(azepan-2-one) by a hydrolytic polymerization of molten azepan- 2-one in the presence of water. Such hydrolytic polymerization can be for example operated as a continuous process in so-called “VK tube” reactors. Methods for manufacturing poly-(azepan-2-one) from azepan-2-one are for example described in B. Herzog, M. I. Kohan, S. A. Mestemacher, R. U. Pagilagan, K. Redmond, R. Sarbandi, Ullmann's Encyclopedia of Industrial Chemistry, Chapter "Polyamides”, pages 22 to 28, 2020 and the references cited therein. A portion of azepan-2-one provided in step (c) for the conversion in polymer P can be manufactured by another method and from another feedstock than azepan-2-one manufactured by step (b) from the benzene separated in step (iv) from the first liquid residue LR1. For example, said portion of azepan-2-one can be manufactured from benzene of fossil origin using the methods disclosed in J. Tinge, M. Groothaert, H. o. h. Veld, J. Ritz, H. Fuchs, H Kieczka, W. C. Moran, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Caprolactam", pages 4 to 16, 2018 and the references cited therein. Said portion of azepan-2-one can also be manufactured by a depolymerization process using plastic waste comprising poly-(azepan-2-one) Such methods are for example disclosed in WO 96 / 18612 A1, EP 568882 A1 , and EP 1975156 A1. Said portion may also comprises azepan-2-one from both foregoing sources.Hexanedioic acid manufactured on step (b) from benzene separated in step (iv) from the first liquid residue LR1 can then be used as a monomer M for manufacturing poly[imino(1,6-dioxohexamethylene) iminohexamethylene) in optional step (c). First, an aqueous solution comprising stochiometric amounts of hexanedioic acid and hexane-1,6- diamine is provided. This aqueous solution is optionally subjected to decolorization method using e.g., char coal priorto further use. Poly[imino(1,6-dioxohexamethylene) iminohexamethylene) can either prepared by batch processes or continuous processes from such aqueous solutions. Batch processes can be conducted in autoclaves at elevated temperatures. Continuous processes can be conducted by controlled evaporation in devices known as “separators” and “flashers" and in a final manufacturing step in “finisher” devices. Suitable methods for manufacturing poly[imino(1,6-dioxohexamethylene) iminohexamethylene) from hexanedioic acid and hexane-1,6-diamine are for example described in B. Herzog, M. I. Kohan, S. A Mestemacher, R. U. Pagilagan, K. Redmond, R. Sarbandi, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Polyamides”, pages 19 to 21 , 2020 and the references cited therein.Polymers derived from isocyanate precursors such as polyurethanes (PUs), thermoplastic polyurethanes (TPUs), polyisocyanurates, and polyureas, which for example based on 1,1 '-methylenebis(4-isocyanatobenzene) or 2,4- diisocyanato-1 -methylbenzene, or poly-isocyanates (e.g., oligomers of di-isocyanato derivatives of benzene and 1- methylbenzene) (“building block”), can be for example manufactured in a continuous processes, solvent-based processes or solvent-free process in the presence of at least one further compound (“building block”) selected from the group comprising or consisting of polyesterpolyoles, polyetherpolyoles, polycarbonatepolyoles, polyetheresterpolyoles, polyacrylatepolyoles, polyesterpolyacrylatepolyoles, diols, polycaprolactane polyols, polytetramethylene glycol, diamines, amino-terminated polyethers and mixtures thereof. Catalysts and additives used to support the desired reactions of the above-mentioned building blocks comprise Lewis-bases, Lewis-acids, and insertion catalysts. Optionally, also chemical, or physical blowing agents are added in case foams are produced (for example: cyclopentane, pentane, hydrofluoro-olefins (“HFOs”), HCOs, water).The manufacture of polyurethanes (PUs), thermoplastic polyurethanes (TPUs), polyisocyanurates, and polyureas using 1 ,1 '-methylenebis(4-isocyanatobenzene) or a (di)isocyanate derivative of 1-methylbenzene such as 2,4- diisocyanato-1 -methylbenzene as a starting material is for example described in G. Brereton et al., Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Polyurethanes”, pages 4 to 27, 2019 and the references cited therein. The manufacture of polyurethanes (PUs), thermoplastic polyurethanes (TPUs), polyisocyanurates, and polyureas using 1, 1 '-methylenebis(4-isocyanatobenzene) or di- and poly-isocyanate derivatives of 1-methylbenzene such as 2,4-diisocyanato-1-methylbenzene as a starting material is for example described in T. Ouhadi, S. Abou-Sabet, H -G. Wussow, L. M. Ryan, L. Plummer, F. E. Baumann, J. Lohmar, H. F. Vermeire, F. L. G Malet, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Thermoplastic Elastomers”, pages 13 to 15, 2013 and the references cited therein.The polyurethanes (PUs), thermoplastic polyurethanes (TPUs), polyisocyanurates, and polyureas comprising di- or multi-isocyanate building blocks which are manufactured from aniline and (di)amino derivatives of 1-methylbenzene by the process according to the present invention can be used for different applications and markets which comprise: Insulation in appliance applications (such as in refrigerators, freezers, boilers, water heaters, cold storage), diverse applications in the automotive market (such as seating carpet backing, acoustics, steering wheels, panel skins, panel foams, headliner foam, headliner adhesive, coating adhesives, sealants, jounce bumpers, suspension mounts, ABScables, ESP cables, interior skins), construction market (such as sandwich panels, spray foam, insulated doors, roller profiles, pipe insulation, wood binders, composite binders, laminate insulation boards, canned foam), footwear (casual shoes, safety shoes, sport shoes, synthetic leather, adhesives, soles for sport shoes, soles for safety shoes), furniture, upholstery and mattrassesThe conversion of benzene-1, 4-dicarboxylic acid as monomer M into polyesters in optional step (c) comprising said monomer M, preferably the conversion of benzene-1 , 4-dicarboxylic acid together with ethane-1 ,2-diol into polyethylene terephthalate) (PET) or together with butane-1,4-diol into poly(oxy-1 ,4-butanediyloxycarbonyl-1,4- phenylenecarbonyl) (PBT) and other polyesters comprising benzene-1, 4-dicarboxylic acid as monomer M is described in Ullmann's Encyclopedia of Industrial Chemistry, chapter “Polyesters” (E. Gubbels et al., Wiley-VCH GmbH Weinheim, 2018, pages 7 to 10 (10.1002 / 14356007. a21_227.pub2).Polymers P comprising styrene as a monomer M comprise polystyrene (PS), poly-acrylonitrile-butadiene-styrene (ABS), styrene-butadiene rubber (SBR) and poly-styrene-acrylonitrile (SAN) which can be manufactured by method described in textbooks.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any 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 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 the claims of the present invention.1 . Process for manufacturing a monomer M from pre-sorted fractions of end-of-life vehicles, the process comprising the steps:(a) providing a C6-C8 aromatic hydrocarbon,(b) converting said C6-C8 aromatic hydrocarbon into a monomer M wherein the C6-C8 aromatic hydrocarbon is manufactured by or obtained by the steps(i) providing at least one pre-sorted fraction PSE of end-of-life vehicles as first feedstock F1, wherein said at least one pre-sorted fraction PSE comprises at least one polymer which forms at least one C6-C8 aromatic hydrocarbon in step (ii), providing a second feedstock F2 and optionally a third feedstock F3, wherein at least 10 wt.-%, more preferably at least 15 wt.-% and most preferably at least 20 wt.-% of all feedstocks provided in step (i) are second feedstock F2,(ii) converting said first feedstock F1 and said second feedstock F2 provided in step (i) and said third feedstock F3 optionally provided in step (i) in a first gasifier G1 into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6-C8 aromatic hydrocarbons,(iii) removing said C6-C8 aromatic hydrocarbons from said first raw synthesis gas RSG1 by a gas cleaning process GO in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed, wherein said first liquid residue LR1 is enriched in C6-C8 aromatic hydrocarbons and wherein said clean first synthesis gas CSG1 is depleted in C6-C8 aromatic hydrocarbons, and(iv) separating an aromatic stream AS and a second liquid stream LR2 from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6-C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6-C8 aromatic hydrocarbons and wherein said aromatic stream AS is optionally further separated into an aromatic stream ASa, an aromatic stream ASb and an aromatic stream ASc in said aromatic hydrocarbon extraction unit AEU. Process according to embodiment 1 further comprising step(c) converting said at least one monomer M into at least one polymer P. Process according to embodiment 1 or 2 wherein a C6-C8 aromatic hydrocarbon is separated from the aromatic stream AS separated in step (iv) and provided in step (a), wherein said C6-C8 aromatic hydrocarbon is selected from the group consisting of benzene, 1-methylbenzene, 1 ,2-diemthylbenzene, 1,3- dimethylbenzene, 1,4-dimethylbenzene and ethylbenzene. Process according to any one of embodiments 1 to 3 wherein the monomer M formed in step (b) is selected from the group comprising or preferably consisting of azepan-2-one, hexanedioic acid, benzene-1 ,4- dicarboxylic acid, 1 ,1 '-methylenebis(4-isocyanatobenzene), 2-isocyanato-1 -methylbenzene, 3-isocyanato-1- methylbenzene, 4-isocyanato-1 -methylbenzene, 2, 4-d iisocy an ato- 1 -methylbenzene, 2, 6-d i isocy anato- 1 - methylbenzene and styrene. Process according to any one of embodiments 1 to 4 wherein the monomer M formed in step (b) is selected from the group consisting of azepan-2-one, hexanedioic acid, benzene-1,4-dicarboxylic acid, 1,1 '- methylenebis(4-isocyanatobenzene), and 2, 4-d i I socy an ato-1 -methylbenzene. Process according to any one of embodiments 2 to 5 wherein the polymer P formed in step (c) is selected from the group comprising or preferably consisting of poly(azepan-2-one) (polyamide-6, PA6), poly [imino(1 ,6- dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66), (T)PUs, polyisocyanurates, polyureas, polyethylene terephthalate) (PET), poly(oxy-1,4-butanediyloxycarbonyl-1 ,4-phenylenecarbonyl) (PBT), other polyesters comprising monomer M benzene-1 ,4-dicarboxylic acid, polystyrene (PS) and other polymers comprising monomer M styrene.7. Process according to any one of embodiments 2 to 6 wherein the polymer P formed in step (c) is selected from the group consisting of poly(azepan-2-one) (polyamide-6, PA6), poly[imino(1,6-dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66), and (T)PUs.8 Process according to any one of embodiments 1 to 7 wherein the at least one polymer which forms at least one C6-C8 aromatic hydrocarbon in step (ii) and is comprised in the at least one pre-sorted fraction PSE of end-of-life vehicles as first feedstock F1 provided in step (i) is selected from the group comprising or consisting of polyolefins, polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.9. Process according to any one of embodiments 1 to 8 wherein said at least one pre-sorted fraction PSE is formed by the steps i. providing an end-of-life vehicle, said end-of-life vehicle comprising at least one polymer, metal fragments and / or non-metallic inorganic fragments, ii. shredding said end-of-life vehicle and thereby forming a non-sorted shredder residue NSR, ill. pre-sorting said non-sorted shredder residue NSR to form said pre-sorted shredder residue NSR, preferably in this order, by a) optionally further reducing the size of said metal fragments and / or non-metallic inorganic fragments and fragments of at least one polymer and b) sorting out said metal fragments and / or said non-metallic inorganic fragments, whereby said pre-sorted shredder residue NSR is depleted in metal fragments and / or in non-metallic inorganic fragments by step b).10. Process according to any one of embodiments 1 to 9 wherein step ii. is selected from the group comprising or consisting of shredding, grinding, milling, sieving, classifying and combinations thereof.11. Process according to any one of embodiments 1 to 10 wherein step ill. is selected from the group comprising or consisting of magnetic separation, separation by eddy current, density separation, manual sorting, and combinations thereof.12. Process according to any one of embodiments 1 to 11 wherein said second feedstock F2 is a particulate feedstock having a particle size PS and is selected from the group comprising or preferably consisting of coal, bio char, wood and combinations thereof.13. Process according to any one of embodiments 1 to 12 wherein said particle size PS of said second feedstock F2 is at least 3 mm (determined by sieving with sieves having defined mesh sizes).14. Process according to any one of embodiments 1 to 13 wherein the second feedstock F2 is selected from the group comprising or preferably consisting of meta-anthracite, anthracite, semianthracite, low volatile bituminous coal, medium volatile bituminous coal, high volatile A bituminous coal, high volatile B bituminous coal, high volatile C bituminous coal, subbituminous A coal, subbituminous B coal, subbituminous C coal, lignite A, lignite B and mixtures thereof15. Process according to any one of embodiments 1 to 14 wherein the second feedstock F2 is selected from the group consisting of low volatile bituminous coal, medium volatile bituminous coal, high volatile A bituminous coal, high volatile B bituminous coal, high volatile C bituminous coal, subbituminous A coal, subbituminous B coal, subbituminous C coal, lignite A, lignite B and mixtures thereof.16. Process according to any one of embodiments 1 to 15 wherein a third feedstock F3 is provided in step (i) and wherein said third feedstock F3 is selected from the group comprising or consisting of biomass, refuse-derived fuel (RDF), textiles, dried sewage sludge, pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, 05 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), tar oils, natural gas, CO2, and mixtures thereof.17. Process according to embodiment 16 wherein the third feedstock is selected from the group consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of- life tires, pyrolysis oils made from biomass, municipal solid waste (MSW), CO2, and mixtures thereof.18. Process according to any one of embodiments 1 to 17 wherein said first gasifier G1 is a fixed-bed gasifier.19. Process according to any one of embodiments 1 to 18 wherein said first gasifier G1 is a fixed bed dry bottom gasifier or a slagging gasifier.20. Process according to any one of embodiments 1 to 19 wherein also tar oil TO is formed in said in a first gasifier G1 and wherein said tar oil TO is converted in a second gasifier G2 into a second raw synthesis gasRSG2.21. Process according to embodiment 20 wherein said second gasifier G2 is an entrained flow gasifier.22. Process according to embodiment 20 or 21 wherein a fourth feedstock F4 is provided and converted in said second gasifier G2 together with tar oil TO into said second raw synthesis gas RSG2.23. Process according to embodiment 22 wherein said fourth feedstock F4 is selected from the group comprising or preferably consisting of pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, tar oils from other sources than said first gasifier G1 , natural gas, coal dust, CO2, and mixtures thereof.24. Process according to any one of embodiments 1 to 23 wherein said 06-08 aromatic hydrocarbons comprised in the first raw synthesis gas RSG1 or the raw synthesis gas RSG12 are separated from said first raw synthesis gas RSG1 or said raw synthesis gas RSG12 in step (iii) by contacting said first raw synthesis gas RSG1 or said raw synthesis gas RSW12 with at least one washing liquid WL.25. Process according to embodiment 24 wherein said at least one washing liquid WL is selected from the group comprising or preferably consisting of alcohols, ethers, amines, alkanolamines, organic polysiloxanes, and mixtures thereof.26. Process according to embodiment 24 or 25 wherein said at least one washing liquid WL is selected from the group consisting of methanol, methylethers of polyethyleneglycol, monoethanolamine, diethanolamine, organic polysiloxanes comprising aryl groups, and mixtures thereof.27. Process according to any one of embodiments 1 to 26 wherein said clean first synthesis gas CSG1 comprises CO and H2 and is depleted in C6-C8 aromatic hydrocarbons compared to said first raw synthesis gas RSG1.28. Process according to any one of embodiments 1 to 27 wherein said C6-C8 aromatic hydrocarbons are separated from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU.29. Process according to any one of embodiments 1 to 28 wherein said C6-C8 aromatic hydrocarbons are separated from said first liquid residue LR1 by a process selected from the group comprising or preferably consisting of adsorption, selective absorption, extractive distillation, solvent extraction followed by distillation, and combinations thereof.30. Process according to any one of embodiments 1 to 29 wherein the C6-C8 aromatic hydrocarbons are selected from the group consisting of benzene, 1 -methylbenzene, 1 ,2-xylene, 1 ,3-xylene, 1 ,4-xylene and ethylbenzene.31. Process according to any one of embodiments 1 to 30 wherein said aromatic stream AS is further separated into an aromatic stream ASa, an aromatic stream ASb and an aromatic stream ASc and wherein said aromatic stream ASa preferably comprises at least 90 wt,-% benzene, more preferably at least 95 wt.-% benzene and most preferably at least 99 wt.-% benzene, wherein said aromatic stream ASb preferably comprises at least 90 wt.-% 1 -methyl benzene, more preferably at least 95 wt.-% 1 -methylbenzene and most preferably at least 99 wt.-% 1-methylbenzene, and wherein said aromatic stream ASc preferably comprises at least 90 wt.-% of xylene isomers, more preferably at least 93 wt.-% of xylene isomers.32. Chemical plant for manufacture of C6-C8 aromatic hydrocarbons from pre-sorted fractions of end-of-life vehicles, the chemical plant comprising a. a first gasifier G1, b. optionally a second gasifier, said optional second gasifier downstream of and fluidically connected to said first gasifier G1, c. a gas cleaning unit GCU, said gas cleaning unit GCU downstream of and fluidically connected to said first gasifier G1 and said optional second gasifier G2, and d. an aromatic hydrocarbon extraction unit AEU, said aromatic hydrocarbon extraction unit AEU downstream of and fluidically connected to said gas cleaning unit GCU, wherein said first gasifier G1 is a fixed bed gasifier and wherein said optional second gasifier G2 is an entrained flow gasifier.33. Use of a chemical plant according to embodiment 32 for a process according to any one of embodiments 1 to 31.The invention will be further explained by the following non-limiting example.A feedstock composition consisting of 50 wt.-% first feedstock F1 (pre-sorted fraction PSE of end-of-life vehicles, pelletized), 20 wt.-% second feedstock F2 (coal) and 30 wt.-% of feedstock F3 (RDF) are provided in step (i). Next, the feedstock composition is converted in a first gasifier G1 (fixed-bed gasifier) into a first raw synthesis gas RSG1 , wherein said first raw synthesis gas RSG1 comprises 14 Vol.-% CO, 30 Vol.-% H2, and 26 g C6-C8 aromatic hydrocarbons per m3of first raw synthesis gas RSG1. Next, C6-C8 aromatic hydrocarbons are removed from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU with a washing liquid WL (methanol), whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed. The first liquid residue LR1, after a liquid phase comprising methanol was separated therefrom, comprises 86.2 wt.-% benzene. Next, C6-C8 aromatic hydrocarbons comprised in the first liquid residue LR1 are separated by extractive distillation in an aromatic hydrocarbon extraction unit AEU by which a stream ASa which is enriched in benzene is obtained. Next, azepan-2-one (as monomer M) is synthesized from said benzene.

Claims

Claims1. Process for manufacturing a monomer M from pre-sorted fractions of end-of-life vehicles, the process comprising the steps:(a) providing a C6-C8 aromatic hydrocarbon,(b) converting said C6-C8 aromatic hydrocarbon into a monomer M wherein the C6-C8 aromatic hydrocarbon is manufactured by or obtained by the steps(i) providing at least one pre-sorted fraction PSE of end-of-life vehicles as first feedstock F1, wherein said at least one pre-sorted fraction PSE comprises at least one polymer which forms at least one C6-C8 aromatic hydrocarbon in step (ii), providing a second feedstock F2 and optionally a third feedstock F3, wherein at least 10 wt,-%, more preferably at least 15 wt.-% and most preferably at least 20 wt.-% of all feedstocks provided in step (i) are second feedstock F2,(ii) converting said first feedstock F1 and said second feedstock F2 provided in step (i) and said third feedstock F3 optionally provided in step (i) in a first gasifier G1 into a first raw synthesis gas RSG1, wherein said first raw synthesis gas RSG1 comprises CO, H2, and C6-C8 aromatic hydrocarbons,(iii) removing said C6-C8 aromatic hydrocarbons from said first raw synthesis gas RSG1 by a gas cleaning process GC in a gas cleaning unit GCU, whereby a clean first synthesis gas CSG1 and a first liquid residue LR1 are formed, wherein said first liquid residue LR1 is enriched in C6-C8 aromatic hydrocarbons and wherein said clean first synthesis gas CSG1 is depleted in C6-C8 aromatic hydrocarbons, and(iv) separating an aromatic stream AS and a second liquid stream LR2 from said first liquid residue LR1 in an aromatic hydrocarbon extraction unit AEU, wherein said aromatic stream AS is enriched in C6-C8 aromatic hydrocarbons and wherein said second liquid stream LR2 is depleted in C6-C8 aromatic hydrocarbons and wherein said aromatic stream AS is optionally further separated into an aromatic stream ASa, an aromatic stream ASb and an aromatic stream ASc in said aromatic hydrocarbon extraction unit AEU.2 Process according to claim 1 further comprising step(c) converting said at least one monomer M into at least one polymer P3 Process according to claim 1 or 2 wherein a C6-C8 aromatic hydrocarbon is separated from the aromatic stream AS separated in step (iv) and provided in step (a), wherein said C6-C8 aromatic hydrocarbon is selected from the group consisting of benzene, 1-methylbenzene, 1,2-diemthylbenzene, 1,3-dimethylbenzene, 1,4-dimethylbenzene and ethylbenzene.

4. Process according to any one of claims 1 to 3 wherein the monomer M formed in step (b) is selected from the group comprising or preferably consisting of azepan-2-one, hexanedioic acid, benzene-1,4-dicarboxylic acid, 1,1 '-methylenebis(4-isocyanatobenzene), 2-isocyanato-1 -methylbenzene, 3-isocyanato-1 -methylbenzene, 4-isocyanato-1 -methylbenzene, 2,4-diisocyanato-1-methylbenzene, 2, 6-diisocyanato-1 -methylbenzene and styrene.

5. Process according to any one of claims 2 to 4 wherein the polymer P formed in step (c) is selected from the group comprising or preferably consisting of poly(azepan-2-one) (polyamide-6, PA6), poly[imino(1 ,6- dioxohexamethylene) iminohexamethylene] (polyamide-66, PA66), (T)PUs, polyisocyanurates, polyureas, polyethylene terephthalate) (PET), poly (oxy- 1,4-butanediyloxycarbony 1-1 ,4-phenylenecarbonyl) (PBT), other polyesters comprising monomer M benzene-1,4-dicarboxylic acid, polystyrene (PS) and other polymers comprising monomer M styrene.

6. Process according to any one of claims 1 to 5 wherein the at least one polymer which forms at least one 06-08 aromatic hydrocarbon in step (ii) and is comprised in the at least one pre-sorted fraction PSE of end- of-life vehicles as first feedstock F1 provided in step (I) is selected from the group comprising or consisting of polyolefins, polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.

7. Process according to any one of claims 1 to 6 wherein said at least one pre-sorted fraction PSE is formed by the steps i. providing an end-of-life vehicle, said end-of-life vehicle comprising at least one polymer, metal fragments and / or non-metallic inorganic fragments, ii. shredding said end-of-life vehicle and thereby forming a non-sorted shredder residue NSR,Hi. pre-sorting said non-sorted shredder residue NSR to form said pre-sorted shredder residue NSR, preferably in this order, by a) optionally further reducing the size of said metal fragments and / or non-metallic inorganic fragments and fragments of at least one polymer and b) sorting out said metal fragments and / or said non-metallic inorganic fragments, whereby said pre-sorted shredder residue NSR is depleted in metal fragments and / or in non-metallic inorganic fragments by step b).

8. Process according to any one of claims 1 to 7 wherein said second feedstock F2 is a particulate feedstock having a particle size PS and is selected from the group comprising or preferably consisting of coal, bio char, wood and combinations thereof.

9. Process according to any one of claims 1 to 8 wherein said particle size PS of said second feedstock F2 is at least 3 mm (determined by sieving with sieves having defined mesh sizes).

10. Process according to any one of claims 1 to 9 wherein a third feedstock F3 is provided in step (i) and wherein said third feedstock F3 is selected from the group comprising or consisting of biomass, refuse-derived fuel (RDF), textiles, dried sewage sludge, pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, 05 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), tar oils, natural gas, CO2, and mixtures thereof.

11. Process according to any one of claims 1 to 10 wherein said first gasifier G1 is a fixed-bed gasifier.

12. Process according to any one of claims 1 to 11 wherein also tar oil TO is formed in said in a first gasifier G1 and wherein said tar oil TO is converted in a second gasifier G2 into a second raw synthesis gas RSG2.

13. Process according to any one of claims 1 to 12 wherein said 06-08 aromatic hydrocarbons comprised in the first raw synthesis gas RSG1 or the raw synthesis gas RSG12 are separated from said first raw synthesis gas RSG1 or said raw synthesis gas RSG12 in step (iii) by contacting said first raw synthesis gas RSG1 or said raw synthesis gas RSW12 with at least one washing liquid WL.

14. Process according to claim 13 wherein said at least one washing liquid WL is selected from the group comprising or preferably consisting of alcohols, ethers, amines, alkanolamines, organic polysiloxanes, and mixtures thereof.

15. Chemical plant for manufacture of C6-C8 aromatic hydrocarbons from pre-sorted fractions of end-of-life vehicles, the chemical plant comprising a. a first gasifier G1 , b. optionally a second gasifier, said optional second gasifier downstream of and fluidically connected to said first gasifier G1, c. a gas cleaning unit GCU, said gas cleaning unit GCU downstream of and fluidically connected to said first gasifier G1 and said optional second gasifier G2, and d. an aromatic hydrocarbon extraction unit AEU, said aromatic hydrocarbon extraction unit AEU downstream of and fluidically connected to said gas cleaning unit GCU, wherein said first gasifier G1 is a fixed bed gasifier and wherein said optional second gasifier G2 is an entrained flow gasifier.

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