Process for manufacture of synthesis gas from waste streams

Abstract

The present invention relates to a process for manufacturing synthesis gas from a feedstock wherein said feedstock is a sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR such as automotive shredder residue (ASR), said non-sorted shredder residue NSR comprising metal fragments and / or non-metallic inorganic fragments, and fragments of at least one polymer. The size of the metal fragments and / or non-metallic inorganic fragments, and fragments of at least one polymer is reduced followed by a separation of the metal fragments and inorganic fragments to obtain the sorted shredder residue SSR. The sorted shredder residue SSR is then subjected to a gasification reaction in at least one plasma gasifier. Thereby, the sorted shredder residue SSR is converted into synthesis gas whereby less CO2 is produced in comparison to state-of-the-art processes.

Description

Process for manufacture of synthesis gas from waste streamsField of the inventionThe present invention relates to a process for manufacture of synthesis gas from waste streams such as automotive shredder residue by gasification. of the inventionWaste streams comprising shredder residues are widely produced and usually incinerated for production of thermal energy and the like. The demand of more sustainable utilizations of such shredder residue, particularly for automotive shredder residue (ASR) is growing.Plasma gasification using at least one plasma torch is a technology suited to convert such shredder residue, particularly automotive shredder residue, into synthesis gas. CO and H2 comprised in said synthesis gas are for example suited as reactants in the manufacture of polymers and other materials comprised in cars and other vehicles. The at least one plasma torch comprised in a plasma gasifier has a lower operational boundary (“Mindestlast” in German). Hence, a minimum amount of electrical power and a minimum amount of at least one (preferably) gaseous plasma source are required to operate said at least one plasma torch and thereby convert a shredder residue into synthesis gas. An undesired high amount of the at least one plasma source is expelled from the plasma gasifier together with CO and H2 in the reaction product synthesis gas in case said at least one plasma torch is operated below its operational boundary. This is the case when not enough shredder residue is available and / or fed into said plasma gasifier. Said undesired high amount of the at least one plasma source must then be separated from the synthesis gas by energy consuming methods utilizing expensive equipment to obtain CO and H2 in a purity required for downstream processes. A higher amount of the at least one plasma source to be separated from the synthesis gas may even prevent the whole process from being sustainable.It is an objective of the present invention to provide a process for converting waste streams comprising shredder residues such as automotive shredder residue into synthesis gas wherein said process has a reduced product carbon footprint and / or reduced CO2 emissions compared to state-of-the-art processes.It is a further objective to provide a process for manufacturing synthesis gas from shredder residues which does not result in an increasing amount of undesired plasma sources in the synthesis gas, in case the amount of said shredder residue fed into a plasma gasifier is below the operational boundary of the at least one plasma torch inside said plasma gasifier.Summary of the inventionThese problems are solved by a process for manufacturing synthesis gas from a feedstock, said process comprising the steps(i) providing a first feedstock F1 wherein said first feedstock F1 comprises a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR, wherein said non-sorted shredder residue NSR comprises metal fragments and / or non-metallic inorganic fragments, and fragments of at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins, wherein said non-sorted shredder residue NSR is presorted to form the sorted shredder residue SSR, 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 sorted shredder residue SSR is depleted in metal fragments and / or in non-metallic inorganic fragments by step b),(ii) providing at least one further feedstock F2,(ill) converting said first feedstock F1 provided in step (I), together with at least one further feedstock F2 provided in step (ii), in at least one plasma gasifier PG into a gas stream GS1 , said gas stream GS1 comprising synthesis gas wherein said synthesis gas comprises H2, CO and CO2 and wherein said at least one plasma gasifier PG comprises at least one plasma torch, said at least one plasma torch operated with electricity, wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS, and(iv) removing at least a portion of CO2 from the gas stream GS1 formed in step (ill) in a synthesis gas upgrading unit SUP and thereby forming a gas stream GS2.These problems are solved by a use of plasma gasification in at least one plasma gasifier PG to convert a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR, wherein said non-sorted shredder residue NSR comprises metal fragments and / or glass fragments, wherein said non-sorted shredder residue NSR is presorted to form the sorted shredder residue SSR, 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 glass fragments from said non-sorted shredder residue NSR, wherein said sorted shredder residue SSR comprises at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins into synthesis gas.These problems are further solved by providing at least one second feedstock F2 and converting said at least one second feedstock F2 together with said first feedstock F1 comprising a sorted shredder residue SSR in a plasma gasifier comprising at least one plasma torch wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS. Thereby, undesired high amounts of the at least one plasma source PS in the synthesis gas are prevented.Further aspects of the present invention will become apparent to the person skilled in the art directly from the foregoing and following description and the examples.Detailed description of the inventionDefinitions: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."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).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.The process according to the present invention is described in detail below.In step I) of the process according to the present invention, a first feedstock F1 is provided. Said first feedstock F1 comprises a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR. Said non-sorted shredder residue NSR comprises metal fragments and / or glass fragments, and fragments of at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.The non-sorted shredder residue NSR is or comprises for example automotive shredder residue (ASR), shredded electric and electronic equipment devices (WEEE - waste electric and electronic equipment) and other types ofwaste 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.Said non-sorted shredder residue NSR is sorted to form the sorted shredder residue SSR, 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.The non-sorted shredder residue NSR and the sorted shredder residue SSR preferably comprises fractions of end- of-life vehicles and / or shredded waste electric and electronic equipment. A particularly preferred first feedstock F1 comprising fractions of end-of-life vehicles is 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 a sorted shredder residue SSR 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 a vertical 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 weight.The 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 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 nonsorted shredder residue NSR 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 canbe 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 sink / 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 a vibrating 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 separated.The automotive shredder residue comprises fragments of various polymeric vehicle parts comprising at least one polymer selected from polyamides, polyisocyanate polyaddition products, rubber 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.The automotive shredder residue preferably comprises at least 30 wt.-%, more preferably at least 40 wt.-%, and most preferably at least 50 wt.-% of the fragments of the polymeric vehicle parts which are referred herein to as "fragments comprising at least one polymer” wherein said at least one polymer is selected from group consisting of polyamides, polyisocyanate polyaddition products, rubber and polyolefins. Such fragments comprising at least one polymer are particularly suited for a conversion into synthesis gas in step (ill) in the at least one plasma gasifier PG.Epoxy resins are typically comprised in shredded waste electric and electronic equipment and may also be comprised in automotive shredder residue.Polyamides which can be comprised in the sorted shredder residue SSR are 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 sorted shredder residue SSR are 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 sorted shredder residue SSR are 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 sorted shredder residue SSR are 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 sorted shredder residue SSR 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 (ill) because they can be converted onto synthesis gas.The non-sorted shredder residue NSR and / or the sorted shredder residue SSR are / is preferably dried before step (ill).At least one further feedstock F2 is provided in step (II) and subjected to the gasification process in step (ill) wherein said gasification process comprises at least one plasma gasifier PG and whereby said further feedstock F2 is inserted into the at least one plasma gasifier PG "together” with the sorted shredder residue SSR provided in step (I). The meaning of "together” depends on the kind of at least one further feedstock F2 and the type of plasma gasifier PG employed in step (ill) and is explained in detail below.Preferably, the at least one further feedstock F2 provided in step (II) is selected from the group comprising or 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, 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), coal, tar oils, natural gas, contaminated vehicle components and mixtures thereof.The term "biomass” includes but is not limited to wood, wood pellets, wood chips, straw, lignocellulosic biomass, energy crops, algae, bio-based oils, and bio-based fats (preferably hydrated).Biomass is preferably torrefied or converted by pyrolysis into a pyrolysis oil before used in step (ill) as a at least one further feedstock F2. Municipal solid waste (MSW) is optionally pre-treated by methods such as drying, shredding, sorting, inert removal and preferably used in step (ill) in form of refuse-derived fuel (RDF). Torrefied biomass is preferably pre-heated to a temperature such as 200 °C before fed into said at least one plasma gasifier PG as a at least one further feedstock F2 in step (ill)."Contaminated vehicle components” suited as further feedstock F2. 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 vehicle before shredding of the vehicle. The shredded parts of the vehicle are defined as automotive shredder residue (ASR) which is a first feedstock F1 in the process according to the present invention. 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 robots.The at least one further feedstock F2 optionally provided in step (II) is preferably selected from the group comprising or 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), coal, contaminated vehicle components and mixtures thereof.The at least one further feedstock F2 is preferably pre-treated before step (II) by a method selected from the group comprising or consisting of sorting, sieving, milling, grinding, pyrolysis, torrefaction, metal sorting and combinations thereof.The weight ratio "first feedstock F1 : further feedstock F2” preferably ranges from 10 : 1 to 1 : 10, more preferably from 1 : 2 to 1 : 10 and most preferably from 1 : 5 to 1 : 10. Preferably, "further feedstock F2” means all further feedstocks F2 combined, in case more than one further feedstock F2 is employed.Liquid further feedstocks F2 such as bio-based oils and pyrolysis oils are preferably pre-heated and / or pressurized to > 1 bar(abs.), more preferably to > 2 bar(abs.) and most preferably to about 4 bar(abs.) before fed into the at least one plasma gasifier PG. Suitable means for pre-heating and / or pressurizing liquid feedstocks for feeding into said at least one plasma gasifier PG are known in the art, comprise for example flaps and locks butalso annual gaps, pressure nozzles and pressure atomizers, and can be adapted to a given further feedstock F2 by the skilled person. The at least one plasma gasifier PG is most preferably a fixed-bed plasma gasifier PG.An overview of plasma gasifiers PG 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 at least one plasma gasifier PG has at least one inlet through which the first feedstock F1 and the at least one further feedstock F2 are fed into said at least one plasma gasifier PG and at least one outlet through which the synthesis gas is purged from said at least one plasma gasifier PG. Preferably, the at least one plasma gasifier PG has more than one inlet. Thereby, at least one further feedstock F2 can be fed separately from the first feedstock F1 into the at least one plasma gasifier PG through a separate inlet. The term "inlet” comprises openings in the at least one plasma gasifier PG such as flaps and locks but also annual gaps as part of a burner such as in twin fluid atomizers, pressure nozzles and pressure atomizers. The plasma is formed by a at least one plasma torch and at least one plasma source PS.Plasma gasifiers PG are preferred for first feedstocks F1 because said feedstock type which has a varying calorific value and availability, can be better balanced in such plasma gasifiers PG for a consistent synthesis gas production (e.g., yield, molar ratio H2 : CO) together with at least one further feedstock F2. Furthermore, less CO2 is produced from gasification of first feedstocks F1 in plasma gasifiers PG, particularly if steam is used as plasma source PS and if electrical power from a renewable source is used to operate the at least one plasma torch. Thereby, less CO2 is formed compared to all gasifier types relying on heat generation by (partial) oxidation.Plasma gasification is a high-temperature waste treatment process that uses plasma, a gas composed of highly charged particles, to break down organic matter into a gas. In this process, the first feedstock F1 and at least one further feedstock F2 are fed into the plasma gasifier PG, preferably, the first feedstock F1 and at least one further feedstock F2 are fed into the plasma gasifier PG, where they are exposed to at least one plasma torch, which ionizes the first feedstock F1 and the at least one further feedstock F2 and creates a plasma. The plasma is generated by means of at least one plasma torch, more preferably, the plasma is generated by means of at least two plasma torches. Most preferably, the plasma gasifier comprises three or more plasma torches. Preferably at least one plasma torch is installed in the part of the plasma gasifier PG where the first feedstock F1 and / or the at least one further feedstock F2 are / is fed onto the plasma gasifier PG and one or two plasma torches in the part of the plasma gasifier PG where the synthesis gas leaves the plasma gasifier PG (most preferably in arrangement which forces the synthesis gas to pass said one or two plasma torches). The high temperatures inside the plasma gasifier PG, which can reach up to about 10000 K, cause the first feedstock F1 and the at least one further feedstock F2 to vaporize and break down into the constituent components, including hydrogen, carbon monoxide, and methane.Most preferably, the at least one plasma gasifier PG is a fixed-bed plasma gasifier. Fixed-bed plasma gasifiers PG are better suited to first feedstocks F1 because the non-metallic inorganic fragments comprised therein cause less plugging and related undesired effects than in other types of plasma gasifiers PG such as fluidized-bed plasma gasifiers PG and entrained-flow plasma gasifiers PG.Preferably, the electricity used for operating the at least one plasma torch of the at least one plasma gasifier PG is generated from a renewable source. More preferably, the electricity used for operating the at least one plasma torch of the at least one plasma gasifier PG is generated from at least one source selected from the group consisting of solar energy, wind energy, tidal energy, nuclear energy, geothermal energy, and combinations thereof.The plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS selected from the group comprising or consisting of steam, oxygen, CO2, air, and combinations thereof. Steam as plasma source PS is most preferred in case a synthesis gas having a molar ratio H2 : CO > 1 is desired. The synthesis gas leaving the plasma gasifier PG also comprises the at least one plasma source PS or portions thereof.The at least one plasma source is co-fed into the at least one plasma gasifier PG in step (iii). Most preferably, steam is co-fed into the at least one plasma gasifier PG in step (iii). The weight ratio "(first feedstock F1 and optional further feedstock F2 combined) : steam” preferably ranges from 1 : 1 to 10 : 1, more preferably from 2 : 1 to 10 : 1 and most preferably from 5 : 1 to 10 : 1 or higher.Preferably, the ratio "electrical power applied to the plasma torch(es) : mass of gas stream GS1 produced” preferably ranges from 0.1 to 15 kW / h : kg, more preferably from 0.5 to 10 kW / h : kg and most preferably from 1 to 8 kW / h : kg. Such a ratio is preferred to maintain the desired process conditions inside the at least one plasma gasifier PG when using a first feedstock F1.The first feedstock F1 and the at least one further feedstock F2 is / are preferably compressed up to 4 bar(abs.) before fed into the at least one plasma gasifier PG.The temperature of the gas leaving the plasma gasifier PG is preferably in the range of 1100 to 1400 °C, most preferably around 1300 °C. The pressure of the synthesis gas leaving the plasma gasifier PG is preferably at least 0.7 bar(abs.) and more preferably at least 1 bar(abs.). The residence time of the reactants inside the plasma gasifier PG is at least 2 to 3 s. The plasma is preferably generated from a gas (plasma source PS) selected from the group comprising CO2, steam, O2, air and mixtures thereof. More preferably, the plasma is generated from a CO2, steam or a mixture of CO2 and steam.The first feedstock F1 is preferably fed into the plasma gasifier PG through an opening separate of the opening through which the at least one further feedstock F2 is fed. Steam is preferably fed to the plasma gasifier through still another opening.A gas stream GS1 then leaves the at least one plasma gasifier PG. Said gas stream GS1 comprises CO and H2 ("synthesis gas”), byproducts of the gasification reaction such as CO2, CH4 and ash, and the at least one plasma source PS or portions thereof. The synthesis gas formed in step (ill) preferably comprises < 15 Vol.-% CO2, more preferably < 10 Vol.-% CO2 and most preferably < 8 Vol.-% CO2.The process comprises a further step (iv) in which impurities and other undesired components such as the at least one plasma source PS or portions thereof are removed from the gas stream GS1 formed in step (ill) in a gas treatment unit GTU. Thereby, a gas stream GS2 having a first molar ratio H2 : CO is obtained.Typical impurities in the gas stream GS1 comprise chlorides, sulfur-containing organic compounds such as sulfur dioxide, trace heavy metals (e.g., as respective salts), tars / condensable hydrocarbons, particulate residues and the at least one plasma source PS or portions thereof. Various chemical and / or physical methods for removal of such impurities from said gas stream GS1 such as filtration, scrubbing, condensation and ab- / adsorption are known and can be chosen and adapted according to the type and respective concentration of the impurities in said gas stream GS1 and the tolerance to such impurities in a further process FP1. Some selected methods for removal of impurities from said gas stream GS1 will be discussed in more detail. One or more of said methods can also be implemented into the gas treatment unit GTU. However, this selection of methods is not limiting the scope of the present invention.Other gaseous substances such as HOI and H2S are formed and / or separated from the gas stream GS1 in the gas treatment unit GTU. The impurities are removed from the gas stream GS1 and a gas stream GS2 having a first molar ratio H2 : CO is obtained.Particulate impurities can be removed from the gas stream GS1 by a cyclone and / or filters, chlorides by wet scrubbing, trace heavy metals, catalytic hydrolysis for converting sulfur-containing organic compounds to H2S and acid gas removal for extracting sulfur-containing gases such as H2S. Bulky and (fine) particles such as dust in the gas stream GS1 may also be removed with a quench in a soot water washing unit.Particulate impurities can be optionally removed from the gas stream GS1 directly by a cyclone and / or filters after the gas stream GS1 leaves the gasifier. Hence, the removal of particles from the gas stream GS1 can be part of a gasifier and / or part of the gas treatment unit GTU which is fluidically connected to the at least one plasma gasifier PG.Fine particles can be optionally removed from the raw synthesis gas directly with filters after the gas stream GS1 leaves the at least one plasma gasifier PG. Hence, the removal of fine particles from the gas stream GS1 can be partof the at least one plasma gasifier PG and / or part of the gas treatment unit GTU which is fluidically connected to the at least one plasma gasifier PG.The optional gas treatment unit GTU preferably comprises a unit for removing at least a portion of CO2 from the gas stream GS1 in step (iv) by a method selected from the group comprising or consisting of absorption, adsorption, membrane separation, cryogenic separation, and combinations thereof. Most preferably, said unit is a washing unit such as an "amine wash” or a "methanol” wash which uses one or more amine compounds such as alkanolamines or methanol to absorb CO2. Such units are known in the art and can be adapted for removal of at least a portion of the CO2 from a gaseous stream GS1 by the skilled person.CO and / or H2 are optionally separated from the gas stream GS1. CO can be separated from the gas stream GS1 in a synthesis gas separation unit which is, optionally, downstream of and fluidically connected to the at least one gasifier G. CO can be separated from gas stream GS1 by cryogenic separation methods, commonly referred to as a "cold box” which makes use of the different boiling points of CO and H2. H2 can be separated using ^-selective membranes thorough which H2 permeates and is thereby separated from the GS1 stream.The gas stream GS1 has a first molar ratio H2 : CO. Optionally, the gas stream GS1 is then preferably subjected to a water-gas shift reaction in a water-gas shift unit. Thereby, the H2 content in the gas stream GS1 is increased by reacting a portion of the CO of the gas stream GS1 with water to form additional H2 and CO2 and thereby gas stream GS2 having a second molar ratio H2 : CO is formed and leaves the water-gas shift unit. The H2 content in said gas stream GS2 leaving the water-gas shift unit and having a second molar ratio H2 : CO is higher than in said gas stream GS1 leaving the at least one gasifier having a first molar ratio H2 : CO. The hydrogen content in gas stream GS1 can for example also be increased by adding hydrogen provided by another source such as hydrogen formed by electrolysis of water, preferably using electrical energy from a renewable source such as solar and / or wind energy.The water-gas shift reaction will operate with a variety of catalysts (such as copper-zinc-aluminum catalysts and chromium or copper promoted iron-based catalysts) in the temperature range between about 200 °C and about 480 °C.The gas stream GS2 is optionally compressed to a pressure in the range 1.5 to 4 bar(abs.).Optionally, at least of the portion of said CO2 separated from the gas stream GS1 in step (iv) is co-fed together with the first feedstock F1 and the optional further feedstock F2 into the at least plasma gasifier PG and thereby converted into synthesis gas. Such CO2 is not considered a further feedstock F2. The weight ratio CO2 : feedstocks F1 and F2 combined” fed into the at least one plasma gasifier ranges from 0 to 2, preferably from 0 to 1 .5 and more preferably from 0 to 1 . Thereby, undesired CO2 formed during a gasification process of a first feedstock F1 and the at leastone further feedstock F2 or provided as plasma source PS can be utilized as an additional feedstock for the manufacturing of synthesis gas.Further CO2 from other sources such as other chemical processes can optionally also be co-fed with the first feedstock F1 and the at least one further feedstock F2 into the at least plasma gasifier PG and thereby converted into synthesis gas. Thereby, undesired CO2 from other sources can be utilized as an additional feedstock for the manufacturing of synthesis gas.Optionally, the gas stream GS2 is then subjected to a further process FP1 selected from the group comprising methanization, alcohol synthesis (preferably methanol synthesis) and Fischer-Tropsch synthesis whereby at least one first product stream PS1 is formed. The gas stream GS2 can also be used as a fuel gas Said optional further processes FP1 are briefly described below:Optionally, the gas stream gas stream GS2 can be converted into methane by a methanation reaction. The methana- tion reaction is described by chemical reaction schemes (1) and (2):CO + 3H2-> CH4+ H2O (1)CO2+ 4H2-> CH4+ 2H2O (2)The methanation reaction and suitable methanation units are for example described in S. Rdnsch, J. Schneider, S. Matthischke, M. Schluter, M. Gdtz, J. Lefebvre, P. Prabhakaran, S. Bajohr: Review on methanation - From fundamentals to current projects; Fuel 166 (2016) 276-296 and can be selected and adapted by the skilled person.The methanation reaction is for example a catalytic reaction using nickel on alumina catalysts, preferably a honeycomb shape catalyst, at 1 to 70 bar and 200 to 700 °C, preferably 5 to 60 bar, more preferably 10 to 45 bar and preferably 200 to 550 °C, more preferably 10 to 45 bar.Alcohols such as methanol are another chemical product which can be manufactured from the gas stream GS2 by an optional further process FP1. The most preferred, methanol, is produced from synthesis gas by a catalytic gas phase reaction at about 5 to 10 MPa and a temperature of about 200 °C to about 300 °C using a catalyst in a low-pressure methanol process in e.g., adiabatic reactors or quasi-isothermal reactors. The catalyst is for example a mixture of copper and zinc oxides, supported on alumina. The methanol synthesis and various options thereof suitable to be combined with the production system according to the present invention are disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter "Methanol”, p. 3 to 12.The gas stream GS2 can also optionally be converted into hydrocarbons such as light synthetic crude oil in an optional Fischer-Tropsch (FT) reaction unit by the FT process. Such hydrocarbons are also denoted "Fischer-Tropschhydrocarbons”. The light synthetic oil can be further converted by hydrocracking and / or isomerization to naphtha, light olefins, or diesel fuel. For production of gasoline and light olefins, the FT process is operated in a temperature range of about 330 °C to about 350 °C and a pressure of about 2.5 MPa (high-temperature FT-process), for production of waxes and / or diesel fuel, in a temperature range of about 220 °C to about 250 °C and a pressure of about 2.5 MPa to about 4.4 MPa (low-temperature FT-process). Suitable reactors for low-temperature FT-processes comprise tubular fixed-bed reactors and slurry bed reactors. Suitable reactors for high-temperature FT-processes comprise circulating fluidized-bed reactors and SAS (Sasol advanced synthol) reactors. Iron- and / or cobalt-based catalysts are used for the FT-process. The Fischer-Tropsch synthesis and various options thereof suitable to be combined with the production system according to the present invention are disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter "Coal Liquefaction”, p. 20 to 33.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 method 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 method 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.1. Process for manufacturing synthesis gas from a feedstock, said process comprising the steps(I) providing a first feedstock F1 wherein said first feedstock F1 comprises a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR, wherein said non-sorted shredder residue NSR comprises metal fragments and / or non-metallic inorganic fragments, and fragments of at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins, wherein said non-sorted shredder residue NSR is presorted to form the sorted shredder residue SSR, 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 sorted shredder residue SSR is depleted in metal fragments and / or in non-metallic inorganic fragments by step b),(ii) providing at least one further feedstock F2,(ill) converting said first feedstock F1 provided in step (I), together with at least one further feedstock F2 provided in step (ii), in at least one plasma gasifier PG into a gas stream GS1, said gas stream GS1 comprising synthesis gas wherein said synthesis gas comprises H2, CO and CO2 and wherein said at least one plasma gasifier PG comprises at least one plasma torch, said at least one plasma torch op-erated with electricity, wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS, and(iv) removing at least a portion of CO2 from the gas stream GS1 formed in step (ill) in a synthesis gas upgrading unit SUP and thereby forming a gas stream GS2.2. Process according to embodiment 1 wherein the non-sorted shredder residue NSR and the sorted shredder residue SSR comprise fractions of end-of-life vehicles.3. Process according to embodiment 1 or 2 wherein the fragments of at least one polymer are selected from at least one member selected from the group consisting 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, and charge air cooler valves.4. Process according to any one of embodiments 1 to 3 wherein step a) is selected from the group comprising or consisting of shredding, grinding, milling, sieving, classifying and combinations thereof.5. Process according to any one of embodiments 1 to 4 wherein 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.6. Process according to any one of embodiments 1 to 5 wherein step b) comprises at least removing metal fragments and / or non-metallic inorganic fragments from said non-sorted shredder residue NSR.7. Process according to any one of embodiments 1 to 6 wherein step b) is selected from the group comprising or consisting of magnetic separation, separation by eddy current, density separation, manual sorting and combinations thereof.8. Process according to embodiment 7 wherein the density separation is a method selected from the group comprising or preferably consisting of cyclone separation, jigging, air separation, sink-float separation and combinations thereof.9. Process according to any one of embodiments 1 to 8 wherein the non-sorted shredder residue NSR preferably comprises up to 15 wt.-%, more preferably up to 10 wt.-%, and most preferably to 5 wt.-% of metal fragments, and / or preferably up to 15 wt.-%, more preferably up to 10 wt.-%, and most preferably to 5 wt.-% of glass fragments.10. Process according to any one of embodiments 1 to 9 wherein the non-sorted shredder residue NSR and / or the sorted shredder residue SSR are / is dried before step (ill).11. Process according to any one of embodiments 1 to 10 wherein the polyamides are selected from the group consisting of PA 6, PA 66 and mixtures thereof.12. Process according to any one of embodiments 1 to 11 wherein the polyisocyanate polyaddition products are selected from the group consisting of polyurethane (PU), thermoplastic polyurethane (TPU), polyurea, polyi- socyanurate (PIR) and mixtures thereof.13. Process according to any one of embodiments 1 to 12 wherein the rubber is selected from the group comprising natural rubber, styrene-butadiene rubber, butyl rubber, ethylene propylene diene monomer rubber, neoprene, nitrile rubber and silicone rubber.14. Process according to any one of embodiments 1 to 13 wherein the polyolefins are selected from the group consisting of low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP) and mixtures thereof.15. Process according to any one of embodiments 1 to 14 wherein the sorted shredder residue SSR comprises at least two different polymers of the group consisting of polyamides, polyisocyanate polyaddition products and polyolefins.16. Process according to any one of embodiments 1 to 15 wherein at least one feedstock F2 is provided in step (II), said at least one further feedstock F2 selected from the group comprising or 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, 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), coal, tar oils, natural gas, contaminated vehicle components and mixtures thereof.17. Process according to any one of embodiments 1 to 16 wherein the at least one further feedstock F2 optionally provided in step (ii) is selected from the group comprising or 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), coal, , contaminated vehicle components and mixtures thereof.18. Process according to any of embodiments 1 to 17 wherein the optional at least one further feedstock F2 is pre-treated before step (II) by a method selected from the group comprising or consisting of sorting, sieving, milling, grinding, pyrolysis, torrefaction, metal sorting and combinations thereof.19. Process according to any one of embodiments 1 to 18 wherein the weight ratio "first feedstock F1 : further feedstock F2” preferably ranges from 10 : 1 to 1 : 10, more preferably from 1 : 2 to 1 : 10 and most preferably from 1 : 5 to 1 : 10.20. Process according to any one of embodiments 1 to 19 wherein the at least one plasma gasifier PG comprises at least 3 plasma torches.21. Process according to any one of embodiments 1 to 20 wherein the electricity used for operating the at least one plasma torch of the at least one plasma gasifier PG is generated from a renewable source.22. Process according to any one of embodiments 1 to 21 wherein the electricity used for operating the at least one plasma torch of the at least one plasma gasifier PG is generated from at least one source selected from the group consisting of solar energy, wind energy, tidal energy, nuclear energy, geothermal energy, and combinations thereof.23. Process according to any one of embodiments 1 to 22 wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS selected from the group comprising or consisting of steam, oxygen, CO2, air, and combinations thereof.24. Process according to any one of embodiments 1 to 23 wherein the ratio "electrical power applied to the plasma torch(es) : mass of gas stream GS1 produced” preferably ranges from 0.1 to 15 kW / h : kg, more preferably from 0.5 to 10 kW / h : kg and most preferably from 1 to 8 kW / h : kg.25. Process according to any of embodiments 1 to 24 wherein the at least one plasma gasifier PG is a fixed-bed plasma gasifier.26. Process according to any one of embodiments 1 to 25 wherein steam is co-fed into the at least one plasma gasifier PG in step (ill).27. Process according to any one of embodiments 1 to 26 wherein steam is co-fed into the at least one plasma gasifier PG in step (ill) and wherein the weight ratio "(first feedstock F1 and optional further feedstock F2 combined) : steam” preferably ranges from 1 : 1 to 10 : 1, more preferably from 2 : 1 to 10 : 1 and most preferably from 5 : 1 to 10 : 1 or higher.28. Process according to any one of embodiments 1 to 27 wherein the synthesis gas formed in step (ill) preferably comprises < 15 Vol.-% CO2, more preferably < 10 Vol.-% CO2 and most preferably < 8 Vol.-% CO2.29. Process according to any of embodiments 1 to 28 wherein at least a portion of the CO2 is removed in step (iv) by a method selected from the group comprising or consisting of absorption, adsorption, membrane separation, cryogenic separation, and combinations thereof.30. Process according to any of embodiments 1 to 29 wherein the weight ratio "CO2 : feedstocks F1 and F2 combined” fed into the at least one plasma gasifier in step (v) ranges from 0 to 2, preferably from 0 to 1 .5 and more preferably from 0 to 1 .31 . Process according to any one of embodiments 1 to 30 wherein the process comprises a further step (v), said further step (v) selected from the group comprising or consisting of separating H2 and CO in the gas stream GS2 from each other, compressing said gas stream GS2 and / or said H2 and / or said CO, combinations of the aforementioned, subjecting the gas stream GS2 to a Fischer-Tropsch process, subjecting gas stream GS2 to a methanization and subjecting gas stream GS2 to a methanol synthesis.32. Process according to any one of embodiments 1 to 31 wherein monomers of at least one polymer are manufactured from the synthesis gas formed in step (ill), said at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins.33. Process, according to any one of embodiments 1 to 32, comprising the step: converting the gas stream GS2 or CO or H2 obtainable by or obtained by the process according to any one of embodiments 1 to 33 or a chemical material obtainable by or obtained by the process according to any one of embodiments 1 to 33 to obtain a product.34. Process according to embodiment 33, wherein the product is selected from: a) building block or monomer; orb) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or c) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or d) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or e) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or f) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or g) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or h) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.35. Use of plasma gasification in at least one plasma gasifier PG to convert a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR, wherein said non-sorted shredder residue NSR comprises metal fragments and / or non-metallic inorganic fragments, wherein said non-sorted shredder residue NSR is presorted to form the sorted shredder residue SSR, preferably in this order, by a) reducing the size of said non-sorted shredder residue NSR and b) sorting out metal fragments and / or glass fragments from said non-sorted shredder residue NSR, wherein said sorted shredder residue SSR comprises at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins into synthesis gas.36. Use according to embodiment 35 wherein the at least one plasma gasifier PG comprises at least one plasma torch.37. Use according to embodiment 35 or 36 wherein the at least one plasma gasifier PG is a fixed bed plasma gasifier.It is explicitly noted that the above set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and thus, suitably supports, but does not represent the claims of the present invention.The present invention further relates to a process according to any one of embodiments 33 or 34, wherein the content of the gas stream GS2 formed in step (iv) or CO or H2 formed therefrom in the product is 1 wt.-% or more, preferably 2 wt.-% or more, more preferably 5 wt.-% or more, more preferably 15 wt.-% or more, more preferably 30 wt.- % or more, more preferably 40 wt.-% or more, more preferably 60 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more, more preferably 95 wt.-% or more; and / or wherein the content of the gas stream GS2 formed in step (iv) or CO or H2 formed therefrom in the product is 100 wt.-% or less, preferably 95 wt.-% or less, more preferably 90 wt.-% or less, more preferably 50 wt.-% or less, more preferably 25 wt.-% or less, more preferably 10 wt.-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

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

[1000] to

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

[1000] to

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

[1000] to

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

[2001] to

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

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

[2009] and

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

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

[3035] to

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

[3008] to

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

[3001] to

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

[3006] to

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

[3045] to

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

[3056] to

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

[6006] entitled "Binders for paper coating” section

[6007] entitled "Binders for fiber bonding” section

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

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

[8000] to

[8005] of Reference RF1.The invention will be further explained by the following non-limiting examples.ExamplesFor the examples a fixed-bed plasma gasifier PG is compared with a solid feed conventional gasifier combination of fluidized bed and entrained flow gasifier. As a main feed, an automotive shredder residue as sorted first feedstock F1 is used with 50 wt.-% carbon, 6 wt.-% hydrogen, 10 wt.-% oxygen, 1 wt.-% nitrogen, 3 wt.-% sulfur, 30 wt.-% ash ("inerts”).Example 1 (invention)The plasma fixed bed gasifier is fed with a mass ratio (kg : kg) "first feedstock F1 : first gas stream GS1 produced” = 1.01. The first feedstock F1 was sorted automotive shredder residue as sorted shredder residue SSR. The plasma is generated from steam, for the desired amount of plasma, a mass ratio (kg : kg) "steam : gas stream GS1 produced” = 0.25 was used. The steam had a pressure of 5.4 bar and a temperature of 180 °C. The ratio (kW / h : kg) "electrical power applied to the plasma torches : mass of gas stream GS1 produced” = 3.91 to reach the desired gas phase temperature of 1350 °C at the outlet of the fixed-bed plasma gasifier PG. The fixed-bed plasma gasifier PG was operated at atmospheric pressure conditions. The complete produced CO2 in the gas stream GS1 was separated therefrom in the gas treatment unit GTU in step (iv) and fed into the fixed-bed plasma gasifier PG. Accordingly, no CO2 is emitted from the process. The molar ratio H2 : CO in the gas streams GS1 and GS2 was 2.07.Example 2 (comparative)For comparison a conventional solid feed gasifier combination of 1. a fluidized-bed gasifier and 2. an entrained-flow gasifier was simulated (the fluidized-bed gasifier produces a raw first gas stream GS1 r from the first feedstock F1which is then converted into a gas stream GS1 comprising synthesis gas in the entrained-flow gasifier). The fl uidized- bed gasifier was fed with mass ratio (kg : kg) "first feedstock F1 : first gas stream GS1r produced” = 0.98 kg. Additionally, oxygen was fed with a ratio of 0.53 kg per kg synthesis gas comprised in the first gas stream GS1 produced, and steam was fed for fluidization with a mass ratio (kg : kg) "steam : raw gas stream GS1 produced” =0.49 kg per kg raw synthesis gas produced. The steam had a pressure of 5.4 bar and a temperature of 180 °C. The raw first gas stream GS1r leaving the fluidized-bed gasifier had a temperature of 850 °C and a pressure of 4 bar. In the secondary reformer (entrained flow reactor) the raw gas stream GS1r is heated up in the second gasifier (entrained-flow gasifier) by introduction of additional oxygen with a mass ratio (kg : kg) "oxygen : first gas stream GS1 produced” = 0.14 kg. At the entrained-flow gasifier exit a temperature of 1350 °C was reached. In step (iv), CO2 of a CO2 ratio 0.39 kg per / kg synthesis gas comprised in the gas stream GS2 produced is separated and afterwards emitted. The molar ratio H2 : CO in the gas streams GS1 and GS2 was 0.94.

Claims

Claims1. Process for manufacturing synthesis gas from a feedstock, said process comprising the steps(i) providing a first feedstock F1 wherein said first feedstock F1 comprises a sorted shredder residue SSR, said sorted shredder residue SSR formed by sorting from a non-sorted shredder residue NSR, wherein said non-sorted shredder residue NSR comprises metal fragments and / or non-metallic inorganic fragments, and fragments of at least one polymer selected from the group consisting of polyamides, polyisocyanate polyaddition products, rubber, epoxy resins and polyolefins, wherein said non-sorted shredder residue NSR is presorted to form the sorted shredder residue SSR, 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 sorted shredder residue SSR is depleted in metal fragments and / or in non-metallic inorganic fragments by step b),(ii) providing at least one further feedstock F2,(ill) converting said first feedstock F1 provided in step (I), together with at least one further feedstock F2 provided in step (ii), in at least one plasma gasifier PG into a gas stream GS1 , said gas stream GS1 comprising synthesis gas wherein said synthesis gas comprises H2, CO and CO2 and wherein said at least one plasma gasifier PG comprises at least one plasma torch, said at least one plasma torch operated with electricity, wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS, and(iv) removing at least a portion of CO2 from the gas stream GS1 formed in step (ill) in a synthesis gas upgrading unit SUP and thereby forming a gas stream GS2.

2. Process according to claiml wherein the non-sorted shredder residue NSR and the sorted shredder residue SSR comprise fractions of end-of-life vehicles.

3. Process according claim 1 or 2 wherein the fragments of at least one polymer are selected from of at least one member selected from the group consisting 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, and charge air cooler valves.

4. Process according to any one of claims 1 to 3 wherein the step a) is selected from the group comprising or consisting of shredding, grinding, milling, sieving, classifying and combinations thereof.

5. Process according to any one of claims 1 to 4 wherein step b) is selected from the group comprising or consisting of magnetic separation, separation by eddy current, density separation, manual sorting and combinations thereof.

6. Process according to any one of claims 1 to 5 wherein at least one feedstock F2 is provided in step (ii), said at least one further feedstock F2 selected from the group comprising or 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, 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), coal, tar oil, natural gas, CO2, contaminated vehicle components and mixtures thereof.

7. Process according to any one of claims 1 to 6 wherein the at least one plasma gasifier PG comprises at least 3 plasma torches.

8. Process according to any one of claims 1 to 7 wherein the electricity used for operating the at least one plasma torch of the at least one plasma gasifier PG is generated from a renewable source.

9. Process according to any one of claims 1 to 8 wherein the plasma in the at least one plasma gasifier PG is generated from at least one plasma source PS selected from the group comprising or consisting of steam, oxygen, CO2, air, and combinations thereof.

10. Process according to any one of claims 1 to 9 wherein the ratio "electrical power applied to the plasma torch(es) : mass of gas stream GS1 produced” preferably ranges from 0.1 to 15 kW / h : kg, more preferably from 0.5 to 10 kW / h : kg and most preferably from 1 to 8 kW / h : kg.11 . Process according to any one of claims 1 to 10 wherein steam is co-fed into the at least one plasma gasifier PG in step (ill) and wherein the weight ratio "(first feedstock F1 and further feedstock F2 combined) : steam” preferably ranges from 1 : 1 to 10 : 1, more preferably from 2 : 1 to 10 : 1 and most preferably from 5 : 1 to 10 : 1 or higher.

12. Process according to any of claims 1 to 11 wherein at least a portion of the CO2 is removed in step (iv) by a method selected from the group comprising or consisting of absorption, adsorption, membrane separation, cryogenic separation, and combinations thereof.

13. Process according to any of claims 1 to 12 wherein the weight ratio "CO2 : feedstocks F1 and F2 combined” fed into the at least one plasma gasifier in step (v) ranges from 0 to 2, preferably from 0 to 1 .5 and more preferably from 0 to 1 .

14. Process, according to any one of claims 1 to 13, comprising the step: converting the synthesis gas or CO or H2 obtainable by or obtained by the process according to any one of claims 1 to 12 or a chemical material obtainable by or obtained by the process according to claim 13 to obtain a product.

15. Process according to claim 14, wherein the product is selected from: a) building block or monomer; or b) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or c) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or d) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or e) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or f) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or g) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or h) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.