Process for synthesis gas production by gasification from biomass

Abstract

The present invention concerns a process for gasification of biomass with reduced fouling of the gasification equipment in which at least one pretreated first feedstock F1 having a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995) and at least one pretreated second feedstock F2 having a deformation temperature of 1100 to 2000 °C are converted in at least one gasifier into synthesis gas. The present invention further concerns a production plant for converting agricultural residues from fast growing plants into synthesis gas which is suited for said process.

Description

Process for synthesis gas production by gasification from biomassTechnical area of the inventionThe present invention relates to a synthesis gas production process from biomass feedstocks in at least one gasifier.Background of the inventionSynthesis gas production from biomass feedstocks by gasification is an emerging technology that offers several advantages over traditional synthesis gas production methods that rely on fossil-based feedstocks. This technology is gaining popularity due to its less damaging impact on the environment. One type of biomass that is of great interest for utilization as a feedstock in the chemical industry is agricultural residues from fast-growing plants like grain and corn. These agricultural residues are abundantly available and cost-effective. Unlike energy crops, which require dedicated resources like soil for cultivation, agricultural residues from regular food crops can be repurposed for synthesis gas production. This dual use of resources makes the process more sustainable.However, when using agricultural residues from fast-growing plants, characterized by a low deformation temperature, as a feedstock for synthesis gas production through gasification, certain challenges may arise. In the gasifiers, particularly in the cold sections with temperatures ranging from 300 to 800 °C, fouling occurs. Such cold sections comprise the synthesis gas outlet of a gasifier and the fluid passage between two sequential gasifiers. Fouling refers to the undesired accumulation of impurities or deposits, which can hinder the efficiency of the gasification process. This fouling can affect various components such as the outlets for the raw synthesis gas or the cold fluid passages between sequential gasifiers if they are used.Moreover, if fluidized bed gasifiers or fixed bed gasifiers are employed, the agricultural residues from fast-growing plants can cause clumping in the fluidized bed or lead to the formation of undesirable melts in the fixed bed at the required gasification process temperatures. These phenomena can disrupt the synthesis gas production process, resulting in a decrease in synthesis gas yield or even rendering the process infeasible.It is important to address these challenges to optimize the synthesis gas production process and maximize the synthesis gas yield. Researchers and engineers are exploring various techniques to mitigate fouling and clumping issues, such as modifying gasifier designs, optimizing operating conditions, and developing catalysts or additives that can enhance the gasification process.It is an objective to reduce fouling of equipment in a synthesis gas production process based on gasification of biomass having a low deformation temperature.It is a further objective of the present invention to provide a synthesis gas production process based on gasification of biomass having a low deformation temperature with an increased synthesis gas yield.Summary of the inventionThese objectives are solved by a process for gasification of biomass comprising the steps(i) providing at least one first feedstock F1, wherein said at least one first feedstock F1 has a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995),(ii) pretreating said at least one first feedstock F1 , the pretreatment comprising comminution and drying,(iii) providing at least one second feedstock F2, wherein said at least one second feedstock F2 has a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995),(iv) pretreating the at least one second feedstock F2, the pretreatment comprising comminution and drying,(v) combining the at least one first feedstock F1 pretreated in step (ii) and the at least one second feedstock F2 pretreated in step (iv), and thereby forming a combined feedstock CF12,(vi) optionally agglomerating said combined feedstock CF12 and thereby forming an agglomerated combined feedstock ACF12,(vii) transferring said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 through a feeding system FS into a first gasifier G1, and(viii) subjecting said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 to a gasification process in a first gasifier G1 whereby a gas stream GS1 is formed and wherein said first gasifier G1 has at least one outlet 01 for said gas stream GS1.These objectives are further solved by a production plant for gasification of biomass comprising(a) at least one first pretreatment unit PU1 for pretreating at least one first feedstock F1, said first pretreatment unit PU1 comprising, preferably in this order, (ia) at least one first means for shredding MS1 , (iia) at least one first means for drying MD1 , and optionally (iiia) at least one first means for milling MM1 ,(b) at least one second pretreatment unit PU2 for pretreating at least one second feedstock F2, said first pretreatment unit PU2 comprising, preferably in this order, (ib) at least one second means for shredding MS2, (iib) at least one second means for drying MD2, and optionally (iiib) at least one second means for milling MM2,(c) a mixing unit MU, the mixing unit downstream of and directly or indirectly fluidically connected to the first pretreatment unit PU1 and downstream of and directly or indirectly fluidically connected to the second pretreatment unit PU2, the mixing unit MU preferably further comprising a dosing system DS,(d) optionally an agglomeration unit AU, the optional agglomeration unit AU downstream of and directly or indirectly fluidically connected to the mixing unit MU, and(e) at least a first gasifier G1 , the at least one gasifier G1 downstream of and directly or indirectly fluidically connected to the mixing unit MU or to the optional agglomeration unit AU.At least on first feedstock F1, comprising or consisting of agricultural residues from fast growing plants, is mixed with at least one second feedstock F2 which has a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995) to form a combined feedstock CF12 which is then converted by gasification in at least one gasifier into synthesis gas. Thereby, less tar is produced and undesired fouling in cold sections of the at least one gasifiersuch as the outlet for raw synthesis gas, or in case two sequential gasifiers are used, in the fluid passage between the raw syngas outlet of the first gasifier and the raw syngas inlet of the second gasifier is reduced and the synthesis gas yield is increased.FiguresFigure 1 schematically shows a first aspect of the process and the production plant according to the present invention.Figure 2 schematically shows a second aspect of the process and the production plant according to the present invention.Figure 3 schematically shows a third aspect of the process and the production plant according to the present invention.Figure 4 schematically shows a fourth aspect of the process and the production plant according to the present invention.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. 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), transportation of a stream, a feedstock, a pretreated feedstock and the like by, for example, truck or train or in a pipeline.“Refuse-derived fuel” (RDF) is defined herein as a fuel produced from 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 (preferably 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 “deformation temperature” of the at least one first feedstock F1 , the at least one second feedstock F2, the combined feedstock CF12, and the combined feedstock CF123 is determined according to ISO 540:1995. The “deformation temperature” can be determined under oxidative of reductive atmosphere. Preferably, the “deformation temperature” is measured under reductive atmosphere (ISO 540:1995, 7.1). The “deformation temperature” is defined as the temperature at which the first signs of rounding, due to melting, of the tip or edges of the test piece occur (ISO 540:1995, 3.1).The “major axis length” of particles is defined as longest distance of an (elongated) particle. The major axis length represents the length of the particle from one end to the other, passing through its center. In geometric terms, the major axis length corresponds to the longest distance between two opposite points on the outer boundary of the particle.The term “at least one” means one or two or three or four or five or six or a higher number. For example, “at least one feedstock” means one feedstock or two feedstocks or three feedstocks or four feedstocks or five feedstocks or six feedstocks and so on.The process for gasification of biomass with reduced fouling of gasification equipment according to the present invention is described below in detail.At least one first feedstock F1 is provided in step (i). Said at least one first feedstock F1 has a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995).Preferably, the at least one first feedstock F1 is selected from the group comprising or preferably consisting of stalks, peels, stems, leaves, husks, shells, cobs, ears, stovers, nuts and combinations thereof, i.e., from plants having a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995).More preferably, the at least one first feedstock F1 is selected from the group comprising or preferably consisting of corn stalks, millet stalks, kenaf stalks, sorghum stalks, sunflower stalks, hemp stalks, rice straw, wheat straw, barley straw, rye straw, oat straw, flax straw, sugarcane bagasse, oil palm empty fruit bunches, bamboo, switchgrass, miscanthus, cassava stems, banana stems, jatropha residues, soybean residues, kenaf residues, moringa residues, wheat bran, maize cobs, pineapple leaves, coffee husks, coconut husks, rice husks, tea waste, peanut shells, sorghum bagasse, other agricultural residues from fast growing plants, and combinations thereof. Such plants and parts of plants have a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995). For example, the first feedstock F1 may comprise rice straw harvested from and / or pretreated at two or more, e.g., three, four, five and so on different locations, or comprise rice straw and corn stalks, or rice straw, rice husks and wheat straw (optionally one or more of said types of first feedstock F1 members harvested and / or pretreated at different locations), and so on. The same options for the “at least one” first feedstock F1 also apply to the other members of the above list.Next, the at least one first feedstock F1 provided in step (i) is pretreated, said pretreatment comprising comminution and drying. The at least one first feedstock F1 may be pretreated at the same location where the first gasifier G1 is installed or at a different location and is then transported to the location where the first gasifier G1 is installed. Optionally, the at least one first feedstock F1 may be comminuted at the same location where the first gasifier G1 is installed or at a different location. Optionally, the at least one first feedstock F1 may be dried at the same location where the first gasifier G1 is installed or at a different location.Preferably, the at least one first feedstock F1 is pretreated in step (ii) by, preferably in this order, (a1) shredding, (b1) drying and (d) milling. The at least one first feedstock F1 may be pretreated at the same location where the first gasifier G1 is installed or at a different location where the first gasifier G1 is installed. Optionally, the at least one first feedstock F1 may be comminuted at the same location where the first gasifier G1 is installed or at a different location. Optionally, the at least one first feedstock F1 may be dried at the same location where the first gasifier G1 is installed or at a different location.The at least one first feedstock F1 is preferably shredded in step (ii) in at least one means for shredding MS1 , said at least one means for shredding MS1 selected from the group comprising or preferably consisting of disc shredders, comprehensive shredders, shear shredders, chipper shredders, tub grinders, bale shredders, flail mowers, rotary cutters, disk harrows, chaff cutters, mulchers, silage cutters, shaft shredders, horizontal grinders, hammer mills, granulators and combinations thereof.The purpose of shredding the at least one first feedstock F1 is to improve the conveyability, transportability, handling, drying and storability.Said at least one means for shredding MS1 can be located where the at least one first feedstock F1 is collected (“location 1 a”) or formed by processing the respective agricultural plant (“location 2a”). Said at least one means for shredding MS1 can also be located where the at least one gasifier G1 is operated (“location 3”). Said at least one means for shredding MS1 can also be located at a location different from where the at least one first feedstock F1 is collected, sourced or formed by processing the respective agricultural residue (“location 4a”). In case two or more means for shredding MS1 are utilized in step (ii), they may be distributed over “location 1 a”, “location 2a”, “location 3”, and “location 4a” in any combination.Chipper Shredders typically have a hopper for feeding the material, which is then shredded using sharp blades or hammers. Chipper shredders are particularly suited for shredding green and dry agricultural residues. Tub grinders work by feeding the material into a tub or drum, where it is shredded and ground by rotating hammers. Tub grinders are particularly suited for shredding large volumes of agricultural residues. Bale shredders typically have a conveyor system that feeds the bales into a shredding chamber, where they are broken down into smaller pieces. Bale shredders are particularly suited for shredding large quantities of baled agricultural residues. Flail mowers typically consist of rotating blades or flails attached to a rotating drum. Flail mowers are particularly suited for shredding crop residues like corn stalks, wheat straw, and rice straw. Rotary cutters are similar to flail mowers, but instead of flails, they have rotating blades that cut the agricultural residues. They are particularly suited for shredding crops like corn, cotton, and soybeans. Disk harrows typically comprise disks which are designed to cut and chop the residues as they pass over them, leaving them evenly distributed on the soil surface. Chaff cutters are simple machines designed to chop agricultural residues into small pieces. They are particularly suited for shredding straw and hay, but they can also be used for shredding other agricultural residues. Mulchers typically comprise a large drum or rotor with cutting teeth that shred the material as it passes through. Mulchers are particularly suited for shredding crop residues like corn stalks, wheat straw, and soybean residues such as soybean stubble. Silage cutters are preferably designed to process crops like corn and sorghum for use as animal feed but can also be used in step (ii) of the process according to the present invention.The major axis length of particles of the at least one first feedstock F1 preferably ranges after shredding from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).The at least one feedstock F1 is preferably dried in step (ii), preferably after shredding, in at least one means for drying MD1 , said at least one means for drying MD1 selected from the group comprising or preferably consisting of rotary dryers, fluidized bed dryers, tray dryers, belt dryers, solar dryers, drum dryers, microwave dryers and combinations thereof.The purpose of drying the at least one feedstock F1 , preferably after shredding, is to reduce the water content, to reduce the weight, to increase the calorific value, to improve the ability for agglomeration and to reduce the adhesiveness.Said at least one means for drying MD1 can be located where the at least one first feedstock F1 is collected (“location 1 a”) or formed by processing the respective agricultural plant (“location 2a”). Said at least one means for drying MD1 can also be located where the at least one gasifier G1 is operated (“location 3”). Said at least one means for drying MD1 can be located at a location different from where the at least one first feedstock F1 is collected, sourced, or formed by processing the respective agricultural residue (“location 4a”) and where the at least one means for shredding MS1 is operated (“location 5a”). In case two or more means for drying MD1 are utilized in step (ii), they may be distributed over “location 1 a”, “location 2a”, “location 3”, “location 4a”, and “location 5a” in any combination.Rotary dryers typically consist of a large cylindrical drum that rotates slowly, allowing the agricultural residues to be contacted with hot air. The hot air passes through the drum and absorbs moisture from the agricultural residues, preferably the shredded agricultural residue, resulting in drying. Fluidized bed dryers typically use hot air to fluidize and suspend the agricultural residues, preferably the shredded agricultural residues, creating a fluidized bed. This promotes efficient heat transfer and drying of the residues. Fluidized bed dryers are known for their high drying rates and uniform drying. Tray dryers typically are simple and cost-effective devices that use a series of trays to hold the agricultural residues. Hot air is passed through the trays, and the moisture is evaporated, drying the (preferably shredded) agricultural residues. Belt dryers typically consist of a conveyor belt that carries the agricultural residues through a drying chamber. Hot air is blown over the residues, drying them as they move along the belt. Belt dryers are particularly suited for continuous drying of large quantities of (preferably shredded) agricultural residues. Solar dryers typically utilize solar energy to dry agricultural residues. They can be passive or active systems, using natural convection or fans to circulate air. Solar dryers are environmentally friendly and may be a cost-effective option in regions with abundant sunlight. Drum dryers are similar to rotary dryers but operate at lower temperatures. They use heated drums to dry the (preferably shredded) agricultural residues. Microwave dryers typically use microwave energy to heat and dry (preferably shredded) agricultural residues. Microwave drying may be faster than conventional drying methods and may be more energy efficient.Preferably, the at least one first feedstock F1 is dried in step (ii) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).The at least one first feedstock F1 is optionally milled in step (ii), preferably after shredding and drying, in at least one means for milling MM1 , said at least one means for milling MM1 selected from the group comprising or preferably consisting of hammer mill, ball mill, roller mill, fluid energy mill, pulverizer, grinder, cryogenic grinder and combinations thereof.The purpose of milling the at least one first feedstock F1, preferably after shredding and drying, is to further reduce the particle size distribution obtained from shredding and / or further improving the ability for agglomeration.Said optional at least one means for milling MM1 can be located where the at least one first feedstock F1 is collected (“location 1 a”) or formed by processing the respective agricultural plant (“location 2a”). Said optional at least one means for milling MM1 can also be located where the at least one gasifier G1 is operated (“location 3”). Said optional at least one means for milling MM1 can be located at a location different from where the at least one first feedstock F1 is collected, sourced, or formed by processing the respective agricultural residue (“location 4a”) and where the at least one means for shredding MS1 and / or the at least one means for drying MD1 is / are operated (“location 5a”). In case two or more optional means for milling MM1 are utilized in step (ii), they may be distributed over “location 1 a”, “location 2a”, “location 3”, “location 4a”, and “location 5a” in any combination.Said means for milling MM1 are designed to crush and grind the, preferably shredded and dried, at least one first feedstock F1 into fine particles, resulting in a powdered form.Hammer Mills consist of a rotating shaft with free-swinging hammers that shred the agricultural residues into small particles. Hammer mills particularly suited for milling (preferably shredded and dried) agricultural residues like corn cobs and rice husks. Ball mills utilize spherical objects such as balls instead of free-swinging hammers. Roller mills utilize cylindrical objects and objects having a related form instead of balls or free-swinging hammers. Fluid energy mills use high-pressure air or gas jets to mill the (preferably shredded and dried) at least one first feedstock F1.Hammer mills can be also used as a means for shredding MS1 in step (ii).The at least one first feedstock F1 is optionally milled in step (ii) after drying to particles having a major axis length of less than 1 cm, preferably less than 0.5 cm and more preferably less than 0.2 cm in case the combined feedstock CF12 is agglomerated in step (vi) whereby an agglomerated combined feedstock ACF12 is formed and wherein said particle size is determined by (determined by sieving with sieves having defined mesh sizes)Next, at least one second feedstock F2 is provided, wherein said at least one second feedstock F2 has a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995).Preferably said at least one second feedstock F2 comprises or consists of wood.More preferably, the at least one second feedstock F2 is selected from the group comprising or preferably consisting of wood chips, sawdust, wood pellets, bark, logging residues, forest thinnings, wood shavings, forest residues, tree trimmings, wood bark mulch, wood residues from woodworking industries, wood pulp and paper byproducts, wood sawdust pellets, tree bark mulch, wood residues from furniture manufacturing, wood shreddings, wood residues fromconstruction and demolition, wood bark chips, wood residues from pulp and paper mills, wood residues from forestry operations, , wood residues from urban tree pruning and removal, other woody biomass, and combinations thereof. Such “woody” feedstocks have a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995). For example, the second feedstock F2 may comprise wood chips collected from and / or pretreated at two or more, e.g., three, four, five and so on different locations, or comprise wood chips and sawdust, or wood chips, sawdust and wood pellets (optionally one or more of said types of second feedstock F2 members collected and / or pretreated at different locations), and so on. The same options for the “at least one” second feedstock F2 also apply to the other members of the above list.Next, the at least one second feedstock F2 provided in step (iii) is pretreated, the pretreatment comprising comminution and drying. The at least one second feedstock F2 may be pretreated at the same location where the first gasifier G1 is located or at a different location and is then transported to the location where the first gasifier G1 is installed. Optionally, the at least one second feedstock F2 may be comminuted at the same location where the first gasifier G1 is located or at a different location. Optionally, the at least one second feedstock F2 may be dried at the same location where the first gasifier G1 is located or at a different location.Preferably, the at least one second feedstock F2 is pretreated in step (iv) by, preferably in this order, (a2) shredding, (b2) drying and optionally (c2) milling. The at least one second feedstock F2 may be pretreated at the same location where the first gasifier G1 is installed or at a different location and is then transported to the location where the first gasifier G1 is installed. Optionally, the at least one second feedstock F2 may be shredded at the same location where the first gasifier G1 is installed or at a different location. Optionally, the at least one second feedstock F2 may be dried at the same location where the first gasifier G1 is installed or at a different location. Optionally, the at least one second feedstock F2 may be milled at the same location where the first gasifier G1 is located or at a different location.The at least one second feedstock F2 is preferably shredded in step (iv) in at least one means for shredding MS2, said at least one means for shredding MS2 selected from the group comprising or preferably consisting of woodchippers, shredder grinders, mulchers, industrial shredders, drum chippers, mobile shredders, handheld shredders and combinations thereof.The purpose of shredding the at least one second feedstock F2 is to improve the conveyability, transportability, handling, drying and storability.Said at least one means for shredding MS2 can be located where the at least one second feedstock F2 is collected (“location 1 b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”). Said at least one means for shredding MS2 can also be located where the at least one gasifier G1 is operated (“location 3”). Said at least one means for shredding MS2 can also be located at a location different from where the at least one second feedstock F2 is collected, sourced or formed (“location 4b”). In case two or more means for shredding MS2 areutilized in step (ii), they may be distributed over “location 1b”, “location 2b”, “location 3”, and “location 4b” in any combination.Woodchippers are typically powerful machines designed specifically for shredding wood into small, uniform pieces called wood chips. Shredder grinders are typically heavy-duty machines that combine the functions of a woodchipper and a grinder. They are capable of handling larger pieces of wood and can produce finer wood chips or mulch. Mulchers are typically used for shredding small to medium-sized branches, leaves. Industrial shredders are typically heavy-duty machines capable of shredding large volumes of wood, including whole trees. Drum chippers, also known as drum-style chippers typically consist of a large drum with cutting blades or knives that chip away at the wood as it passes through. Mobile shredders are suitable for on-site wood shredding. These machines are often mounted on trucks or trailers and can handle various types of wood waste, including branches. Handheld shredders are typically lightweight, portable devices that are designed for shredding branches and small wood pieces. Handheld shredders typically have a cutting mechanism powered by electricity or gasoline, allowing for easy shredding of small quantities of wood waste.The major axis length of particles of the at least one first feedstock F1 preferably ranges after shredding from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).The at least one second feedstock F2 is preferably dried in step (iv), preferably after shredding, in at least one means for drying MD2, said at least one means for drying MD2 selected from the group comprising or preferably consisting of rotary dryers, fluidized bed dryers, tray dryers, belt dryers, solar dryers, drum dryers, microwave dryers, rotary kilns, fluidized bed reactors, fixed bed reactors, drum torrefiers, microwave torrefaction systems, screw pyrolysis reactors, hybrid system torrefiers and combinations thereof.The drying of the at least one second feedstock F2, preferably after shredding, may comprise or consist of a first drying sub-step followed by a torrefaction sub-step.The purpose of drying the at least one feedstock F1 , preferably after drying, is to reduce the water content, to reduce the weight, to increase the calorific value, to improve the ability for agglomeration and to reduce the adhesiveness.Said at least one means for drying MD2 can be located where the at least one second feedstock F2 is collected (“location 1 b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”). Said at least one means for drying MD2 can also be located where the at least one gasifier G1 is operated (“location 3”). Said at least one means for drying MD2 can be located at a location different from where the at least one second feedstock F2 is collected, sourced, or formed by processing the respective at least one second feedstock F2 (“location 4b”) and where the at least one means for shredding MS2 is operated (“location 5b”). In case two or more means for dryingMD2 are utilized in step (ii), they may be distributed over “location 1 b”, “location 2b”, “location 3”, “location 4b”, and “location 5b” in any combination.Furthermore, drying can be separated into e.g., two drying stages such as drying at a lower temperature and then drying at a higher temperature (“torrefaction”). Said two drying stages may also be operated at different locations.Some of the means for drying MD2 are described in more detail further above (MD1). Means for drying MD2 which are particularly suited for high temperature drying, also referred to as “torrefaction” of the at least one second feedstock F2 comprise rotary kilns, fluidized bed reactors, fixed bed reactors, drum torrefiers, microwave torrefaction systems, screw pyrolysis reactors and hybrid systems. Said means for drying MD2 are described further below.Rotary kilns are typically large, cylindrical drums that rotate slowly and expose the at least one second feedstock F2 to high temperatures. They are commonly used for commercial-scale torrefaction due to their high throughput capacity. Fluidized bed reactors suspend the at least one second feedstock F2 in an upward-flowing stream of hot gas. This technology offers excellent heat transfer and uniform temperature distribution, making it suitable for torrefaction. Fixed bed reactors are vertical or horizontal vessels in which the at least one second feedstock F2 is heated in a stationary bed. Drum torrefiers typically consist of a rotating drum in which the at least one second feedstock F2 is heated. Microwave torrefaction typically systems use electromagnetic radiation to heat the at least one second feedstock F2. This technology offers rapid and efficient heating. Screw pyrolysis reactors use a rotating screw to transport and heat the at least one second feedstock F2. This technology offers good control over residence time and temperature, making it suitable for torrefaction. Hybrid system torrefiers typically combine multiple technologies, such as rotary kilns with fluidized bed reactors or fixed bed reactors with microwave heating, to optimize the torrefaction process.Preferably, the at least one second feedstock F2 is dried in step (iv) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).The at least one second feedstock F2 is optionally milled in step (iv), preferably after shredding and drying, in at least one means for milling MM2, said at least one means for milling MM2 selected from the group comprising or preferably consisting of hammer mill, tub grinder, ball mill, roller mill, fluid energy mill, pulverizer, grinder, cryogenic grinder and combinations thereof.Hammer Mills consist of a rotating shaft with free-swinging hammers that shred the agricultural residues into small particles. Hammer mills particularly suited for milling (preferably shredded and dried) agricultural residues like corn cobs and rice husks. Ball mills utilize spherical objects such as balls instead of free-swinging hammers. Roller mills utilize cylindrical objects and objects having a related form instead of balls or free-swinging hammers. Fluid energy mills use high-pressure air or gas jets to mill the (preferably shredded and dried) at least one second feedstock F2.The purpose of optional milling the at least one first feedstock F2, preferably after shredding and drying, is to further reduce the particle size distribution obtained from shredding, further improving the ability for agglomeration.Said optional at least one means for milling MM2 can be located where the at least one second feedstock F2 is collected (“location 1b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”). Said optional at least one means for milling MM2 can also be located where the at least one gasifier G1 is operated (“location 3”). Said optional at least one means for milling MM2 can be located at a location different from where the at least one second feedstock F2 is collected, sourced, or formed by processing the respective at least one second feedstock F2 (“location 4b”) and where the at least one means for shredding MS2 and / or the at least one means for drying MD2 is / are operated (“location 5b”). In case two or more optional means for milling MM2 are utilized in step (ii), they may be distributed over “location 1 b”, “location 2b”, “location 3”, “location 4b”, and “location 5b” in any combination.Said at least one means for milling MM2 is designed to crush and grind the, preferably shredded and dried, at least one second feedstock F2 into fine particles, resulting in a powdered form.Preferably, the at least one second feedstock F2 is milled in step (iv), preferably after shredding and drying, to particles having a major axis length of less than 1 cm, preferably less than 0.5 cm and more preferably less than 0.2 cm in case the combined feedstock CF12 is agglomerated in step (vi) whereby an agglomerated combined feedstock ACF12 is formed and wherein said particle size is determined by (determined by sieving with sieves having defined mesh sizes)Tub grinders are large, horizontal grinders that are commonly used in the forestry and logging industry. They typically consist of a tub-shaped container with a rotating drum or hammermill inside. Wood waste is fed into the tub, and the spinning drum shreds the wood into smaller pieces. Tub grinders are capable of handling large volumes of wood and are often used for processing whole trees, stumps, and other bulky wood materials.Next, the at least one first feedstock F1 pretreated in step (ii) and the at least one second feedstock F2 pretreated in step (iv) are combined in step (v), preferably in a mixing unit MU, and thereby a combined feedstock CF12 is formed.Preferably, weight ratio “first feedstock F1 : second feedstock F2” in the combined feedstock CF12 ranges from 10 : 90 to 90 : 10.Preferably, the amount of the at least one second feedstock F2 combined with the at least one first feedstock F1 in step (v) is sufficient to form a mixed feedstock CF12 having a deformation temperature of at least 850 °C (determined according to ISO 540:1995). Hence, said sufficient amount of the at least one second feedstock can be for example determined by taking a sample of a mixed feedstock CF12, determining the deformation temperature ofsaid combined feedstock CF12 and adding an additional amount of said at least one second feedstock F2 to said combined feedstock CF12 in case the determined deformation temperature of the sample of said mixed feedstock CF12 is below 850 °C. Determination of the deformation temperature and addition of additional amounts of the at least one second feedstock F2 may be repeated until the desired determination temperature (at least 850 °C) of the combined feedstock CF12 is reached. In case the determined deformation temperature of the combined feedstock CF12 is far above 850 °C, a lower amount of the at least one second feedstock F2 may be added to form the combined feedstock CF12. A deformation temperature of at least 850 °C of the combined feedstock CF12 is particularly preferred to prevent undesired fouling in cold sections such as the synthesis gas outlet of a gasifier and the fluid passage between two sequential gasifiers. This first aspect of the present invention is schematically shown in Figure 1.Optionally, at least one third feedstock F3 is provided and combined with the at least one first feedstock F1 pretreated in step (ii) and the at least one second feedstock F2 pretreated in step (iv), whereby a combined feedstock CF123 is formed. The optional at least one third feedstock F3 is preferably combined in the mixing unit MU to form a homogeneous mixture with the pretreated at least one first feedstock F1 and the pretreated at least one second feedstock F2. The deformation temperature of the combined feedstock CF123 is determined according to ISO 540:1995. Said combined feedstock CF123 is then preferably agglomerated whereby an agglomerated combined feedstock ACF123 is formed.The optional at least one third feedstock F3 comprises or preferably consists of plastic waste. Thereby, the calorific value of the combined feedstock CF12 can be increased. The at least one optional feedstock F3 may comprises plastic waste sourced and / or pretreated in one, two, three, four, five, six, and so on, locations. The at least one optional feedstock F3 may comprises plastic waste which comprises one, two, three, four, five, six, and so on, different types of plastic materials. The term “plastic waste” also includes accompanying matter such as fillers, dirt, and other non-plastic material which were not separated from said plastic waste during sorting and / or other pretreatment operations.Preferably, the at least one third feedstock F3 is pretreated by at least one method selected from the group comprising or preferably consisting of shredding, drying, hydrothermal carbonization, torrefaction, milling, sorting and combinations thereof, before combined with the at least one first feedstock F1 and the at least one second feedstock F2 in step (v) and or transferred separately through a feeding system FS into a first gasifier G1. Sorting may comprise sorting by NIR and / or manual sorting. Such pretreatment methods are known and can be applied by the skilled person to a given at least one third feedstock F3 accordingly.Preferably, the optional at least one third feedstock F3 is provided after a pretreatment comprising drying and comminution. More preferably, the optional at least one third feedstock F3 is provided after drying and comminution to particles having a major axis length of less than 1 cm, preferably less than 0.5 cm and mor preferably less than0.2 cm in case the combined feedstock CF123 is agglomerated before subjected to a gasification process in a first gasifier G1.The combination with at least one third feedstock F3 preferably makes the agglomerated combined feedstock ACF123 less sensitive for attrition than the agglomerated combined feedstock ACF12 and results in an agglomerated combined feedstock having a higher impact resistance. This will preferably lower the dust formation when handling and during storage of such agglomerated combined feedstocks as compared to when handling agglomerated combined feedstocks ACF12. Furthermore, the optional at least one third feedstock may also decrease undesired swelling of agglomerated combined feedstocks, e.g., at elevated temperatures. Such undesired swelling has a negative effect when feeding an agglomerated combined feedstock into the at least one first gasifier G1, particularly when said swelling occurs during said feeding.Preferably, optional at least one third feedstock F3 has, when provided, a major axis length of particles of less than 1 cm, more less than 0.5 cm and most preferably less than 0.2 cm in case the combined feedstock CF123 is agglomerated in step (vi) whereby an agglomerated combined feedstock ACF123 is formed and therein said particle size is determined by (determined by sieving with sieves having defined mesh sizes).Preferably, the at least one optional third feedstock F3 is provided and combined in step (v) with the at least one first feedstock F1 and the at least one second feedstock F2 and thereby forming a combined feedstock CF123 and / or is transferred separately through a feeding system FS into a first gasifier G1 .Preferably, the combined feedstock CF12 or the combined feedstock CF123 is agglomerated in optional step (vi) whereby agglomerates of an agglomerated combined feedstock ACF12 or agglomerates of an agglomerated combined feedstock ACF123 is formed and wherein the first gasifier G1 is selected from fixed bed gasifiers, fluidized bed gasifiers, and plasma fixed bed gasifiers. This second aspect of the present invention is schematically shown in Figure 2.Agglomerated combined feedstocks AFC 12 and AFC123 are suited for a gasification process in a first gasifier G1 , wherein said first gasifier G1 is selected from the group consisting of fixed bed gasifiers, fluidized bed gasifiers and plasma fixed bed gasifiers. Said agglomerated combined feedstocks AFC 12 and AFC123 are not preferred for entrained flow gasifiers G1 . Combined feedstocksCF12 or CF123 are preferred for entrained flow gasifiers G1 .Preferably, step (vi) is applied with the proviso that the first gasifier G1 is a fixed bed gasifier, fluidized bed gasifier or plasma fixed bed gasifier and wherein step (vi) is not applied with the proviso that the first gasifier G1 is an entrained flow gasifier.Agglomeration of the combined feedstocks CF12 and CF123 can be for example, achieved by the following procedure (other suitable procedures are known by the skilled person and can be applied to the combined feedstocks CF12 and CF123 accordingly):1. The combined feedstock CF12 or CF123 is fed into a pellet mill. The combined feedstock CF12 or CF123 is preferably fed through a feeding system such as a hopper, which feeds the combined feedstock CF12 or CF123 into the pelletizing chamber comprised in the pellet mill.2. Next, the combined feedstock CF12 or CF123 is compressed, for example, by rollers that rotate against a die. The die has small holes in it, which shape the agglomerated combined feedstock ACF12 or agglomerated combined feedstock ACF123.3. The agglomerated combined feedstock ACF12 or ACF123 is then optionally heated. The heat softens the lignin comprised in the second feedstock F2 comprised in agglomerated combined feedstock ACF12 or the lignin comprised in the second feedstock F2 and the plastic comprised in the third feedstock F3, both comprised in agglomerated combined feedstock ACF123, which acts as a natural binding agent. This helps the respective agglomerated combined feedstock to hold its shape.4. Next, the respective agglomerated feedstock ACF12 or ACF123 is cooled, preferably as it passes through a cooler. This helps to harden the respective agglomerated feedstock and prevent it from breaking.5. The final step is to screen the agglomerated feedstock ACF12 or ACF123 to remove any fines or dust. The fines can be recycled back into the agglomeration process, while the dust can be used otherwise.Steps (v) and / or (vi) may performed at the location where the first gasifier G1 is installed or at a different location.Optionally, agglomerates of an agglomerated combined feedstock ACF12 or ACF123 are formed in a location which is different from the location where the first gasifier G1 is installed.Next, said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 or AFC 123 is transferred through a feeding system FS into a first gasifier G1 in step (vii).The feeding system FS is selected from the group comprising or preferably consisting of hoppers, vibratory feeders, screw feeders, belt feeders, pneumatic feeders and combinations thereof.The feeding system FS is optionally rinsed with an inert gas such as CO2 and / or N2 during feeding the combined feedstock CF12, the combined feedstock CF123, the optional agglomerated feedstock ACF12 or ACF123 into the first gasifier G1 . Thereby, the oxygen content in the first gasifier G1 and the gasification reaction can be better controlled.Next, in step (viii) said combined feedstock CF12 or said combined feedstock CF123 or said agglomerated combined feedstocks ACF12 or ACF123 is subjected to a gasification process in a first gasifier G1 whereby gas stream GS1 isformed and wherein said first gasifier G1 has at least one outlet 01 for said gas stream GS1 . This third aspect of the present invention is schematically shown in Figure 3.Preferably, the size of agglomerates of agglomerated feedstocks ACF12 and ACF123 ranges from 1 to 10 cm in case the first gasifier G1 is a fixed bed gasifier or a plasma fixed bed gasifier or the size of agglomerates of agglomerated feedstocks ACF12 and ACF123 ranges from 0.3 to 5 cm in case the first gasifier G1 is a fluidized bed gasifier, wherein said agglomerate size is determined by sieving with sieves having defined mesh sizes.Preferably, the first gasifier G1 is selected from the group comprising or preferably consisting of fixed bed gasifier, fluidized bed gasifier, entrained flow gasifier, plasma fixed bed gasifier.In case the first gasifier G1 is a fixed bed plasma gasifier said gasifier G1 preferably comprises at least one plasma torch.An overview of 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.Preferably, the temperature in the outlet 01 of the first gasifier G1 ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C. Thereby, undesired formation of deposits which result in fouling is suppressed.Preferably, the gas stream GS1 comprises CO, H2, CO2, methane, tar, tar oils and combinations thereof.Preferably, the gas stream GS1 is further converted in a second gasifier G2. Said second gasifier G2 has at least one inlet (I2), said at least one inlet (I2) is fluidically connected to the at least one outlet (01) of the first gasifier G1 , and said second gasifier G2 downstream of said first gasifier G1. Said second gasifier G2 is downstream of and preferably fluidically connected by a fluid passage FP with the first gasifier G1. The gas stream GS1 is converted into a gas stream GS2 in said second gasifier GS2. This fourth aspect of the present invention is schematically shown in Figure 4. Preferably, the optional second gasifier G2 is an entrained flow gasifier. Preferably, the fluid passage FP comprises or more preferably consists of a pipe and / or a cyclone. Preferably, the temperature of gas stream GS1 in the fluid passage FP ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C.Undesired fouling starts already in case the temperature of the fluid passage FP, e.g., the inner walls of said fluid passage FP has a temperature of slightly less 800 °C, such as 799 °C or 795 °C. Such a fluid passage FP typically has a length of about 4 m or more. Such a fluid passage FP is typically isolated but the temperature along the 4 m or longer fluid passage FP may drop by 20 to 50 °C.Preferably, the CO content and / or the H2 content in gas stream GS2 is higher than the CO and / or H2 content in gas stream GS1.In case a second gasifier G2 is used, said second gasifier G2 downstream of and fluidically connected to the first gasifier G1 and wherein said second gasifier G2 is an entrained-flow gasifier, at least one fourth feedstock F4 may be co-fed with gas stream GS1 into said second gasifier G2. Said at least one fourth feedstock F4 is selected from the group comprising or preferably consisting of bio-oil, pyrolysis oil formed by pyrolysis of biomass, pyrolysis oil formed by pyrolysis of plastic waste, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, used oils, natural gas, industrial waste streams, coal dust and combinations thereof. Said at least one fourth feedstock F4 may comprise also two, three, four or even more bio-oils, manufactured from different biomass and / or different locations. Said at least one fourth feedstock F4 may also comprise a bio-oil and a pyrolysis oil formed by pyrolysis of plastic waste, and so on. The same options for the fourth feedstock F4 also apply to all other members of the above list.The optional at least one fourth feedstock F4 is preferably pre-heated and / or pressurized before fed into the second gasifier G2 to > 10 bar(abs.), more preferably > 20 bar(abs.) and most preferably > 40 bar(abs.). Suitable means for pre-heating and / or pressurizing the at least one optional fourth feedstock F4 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 at least one fourth feedstock F4 by the skilled person.Optionally, the gas stream GS1 or GS2 is subjected to at least one gas cleaning process in a gas treatment unit GTU whereby a clean synthesis gas stream OS is formed, said at least one gas cleaning process selected from the group comprising particle removal, water wash, CO2 removal, sulfur removal, HCI removal, Hg removal, HCN / NH3 removal and combinations thereof. The gas treatment unit GTU is preferably downstream of and fluidically connected to the first gasifier G1 in case only one gasifier is employed. The gas treatment unit GTU is preferably downstream of and fluidically connected to the second gasifier G2 in case two gasifiers are employed and wherein the second gasifier is downstream of and fluidically connected by a fluid passage FP to the first gasifier G1 .Typical impurities in the gas stream GS1 or gas stream GS2 comprise chlorides, sulfur-containing organic compounds such as sulfur dioxide, trace heavy metals (e.g., as respective salts), tars / condensable hydrocarbons and particulate residues. Various chemical and / or physical methods for removal of such impurities from said gas stream GS1 or gas stream GS2 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 or gas stream GS2 and the tolerance to such impurities in a further process (see below). Some selected methods for removal of impurities from said gas stream GS1 or gas stream GS2 will be discussed in more detail. One or more ofsaid methods can also be implemented into the optional gas treatment unit GTU. However, this selection of methods is not limiting the scope of the present invention.Other gaseous substances such as HCI and H2S are formed and / or separated from the gas stream GS1 or gas stream GS2 in the optional gas treatment unit GTU. The impurities are removed from the gas stream GS1 and a gas stream GS2 having a first molar ratio CO : H2is obtained.Particulate impurities can be removed from the gas stream GS1 or gas stream GS2 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.Fine particles can be optionally removed directly with filters after the gas stream GS1 leaves the first gasifier G1 or the gas stream GS2 leaves the second gasifier G2 in case two gasifiers G1 and G2 are employed. Hence, the removal of fine particles from the gas stream GS1 can be part of the first gasifier G1 , and / or part of the optional gas treatment unit GTU which is optionally fluidically connected to the first gasifier G1 in case only one gasifier is employed. In case a second gasifier G2, said second gasifier G2 downstream of and fluidically connected by a fluid passage FP to the first gasifier G1 , the removal of fine particles from the gas stream GS2 can be part of the second gasifier G2, and / or part of the optional gas treatment unit GTU which is optionally fluidically connected to the first gasifier G2.The optional gas treatment unit GTU preferably comprises a washing unit for removing CO2from the gas stream GS1 or the gas stream GS2. Most preferably, said washing unit is an “amine wash” or a “methanol” wash which uses one or more amine compounds such as alcohol amines or methanol to absorb CO2. Such washing units are known in the art and can be adapted for removal of CO2from a gaseous stream GS1 or a gas stream GS2 by the skilled person.CO and / or H2are optionally separated from the gas stream GS1, gas stream GS2 or gas stream CS. CO can be separated from the gas stream GS1, gas stream GS2 or gas stream CS in a synthesis gas separation unit which is, optionally, downstream of and fluidically connected to the optional gas treatment unit GTU. CO can be separated from gas stream GS1, gas stream GS2 or gas stream CS by cryogenic separation methods, commonly referred to as a “cold box” which makes use of the different boiling points of CO and H2. H2can be separated using H2-selective membranes thorough which H2permeates and is thereby separated from gas stream GS1, gas stream GS2 or gas stream CS.Optionally, the gas stream GS1, gas stream GS2 or gas stream CS is then subjected to a water-gas shift reaction in a water-gas shift unit in which the molar ratio CO : H2of the respective gas stream is changed by increasing the H2content. The hydrogen content in gas stream GS1, gas stream GS2 or gas stream CS can also be increased byadding 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 and about 480 °C. Optionally, at least a portion of the clean synthesis gas stream OS, optionally after increasing the hydrogen content as described above, is further converted into methanol, ethanol, mixed alcohols, methane or into a mixture of hydrocarbons HC by a Fischer-Tropsch process. Said mixture of hydrocarbons HC can be further converted into, for example, bio-naphtha and sustainable such as sustainable aviation fuels.Optionally, the gas stream gas stream OS can be converted into methane by a methanation reaction. The methanation reaction is described by chemical reaction schemes (1) and (2):The methanation reaction and suitable methanation units are for example described in S. Rbnsch, J. Schneider, S. Matthischke, M. Schluter, M. Gbtz, 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.Methanol can be manufactured from the clean gas stream CS, optionally after increasing the hydrogen content as described above, by a catalytic gas phase reaction generally at about 5 to 10 MPa and generally at a temperature of about 200 to 300 °C 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 known in the art and for example disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter “Methanol”, p. 3 to 12. Preferably, methanol is further converted e.g., by a methanol-to-olefins (MTO) process to olefins such as ethene and propene or by a methanol to gasoline (MTG) process to fuels, preferably to jet fuel.In the MTG process, methanol is converted over a catalyst, generally a zeolite, preferably an acidic zeolite, like SAPO-34 or HZSM-5 to a mixture of olefins, aliphatics, and aromatics, generally up to C11. Suitable reaction conditions are for example 350 to 400°C, and atmospheric pressure. The hydrocarbon mixture obtained is suitable as gasoline, especially as jet fuel.The MTO process is the catalytic conversion of methanol to lower olefins, especially ethene and / or propene. An interruption of the MTG reaction, by careful control over process conditions (T, space velocity), leads to the methanol-to-olefins process (MTO). As in the MTG process, generally a zeolite, preferably an acidic zeolite, like SAPO-34 or HZSM-5 is used as catalyst.Further details regarding the MTG and the MTO process are known in the art and for example described in Makarand R. Gogate (2019) Methanol-to-olefins process technology: current status and future prospects, Petroleum Science and Technology, 37:5, 559-565, DOI: 10.1080 / 10916466.2018.1555589 and the literature mentioned therein.Suitable MTG processes comprise the Mobile MTG Process, Topsoe improved gasoline synthesis (TiGAS) and Syngas to Gasoline plus Process (STG+).The clean gas stream OS, optionally after increasing the hydrogen content as described above, can also be converted into a mixture of hydrocarbons HO such as light synthetic crude oil in an optional Fischer-Tropsch (FT) reaction unit by the FT process. Such hydrocarbons are also denoted “Fischer-Tropsch hydrocarbons”. The “Fischer- Tropsch hydrocarbons”, generally in form of a light synthetic oil can be further converted to bio-naphtha, light olefins, gasoline, fuel (“FT fuels”) like diesel fuel or jet fuel (“sustainable aviation fuel”), most preferably jet fuel, generally by hydrocracking and / or isomerization. By said process, so called FT-SPK fuels and FT-SKA fuels are for example obtained. FT-SPK fuels are fuels using biomass resources (e.g. wood residues) and FT-SKA fuels are FT fuels with aromatics using biomass resources (e.g. wood residues). Suitable FT processes and reactors and suitable subsequent processes and reactors for obtaining bio-naphtha, light olefins, gasoline, fuel (“FT fuels”) like diesel fuel or jet fuel (“sustainable aviation fuel”) are known in the art. For production of bio-naphtha, gasoline, jet fuel and light olefins, the FT process is generally operated in a temperature range of about 330 to about 350 °C and generally at a pressure of about 2.5 MPa (high-temperature FT-process), for production of waxes and / or diesel fuel, generally in a temperature range of about 220 to about 250 °C and generally at a pressure of about 2.5 to about 4.4 MPa (low- temperature FT-process). Suitable reactors for low-temperature FT-processes comprise for example tubular fixed- bed reactors and slurry bed reactors. Suitable reactors for high-temperature FT-processes comprise for example circulating fluidized-bed reactors and SAS (Sasol advanced synthol) reactors. Iron- and / or cobalt-based catalysts are for example used for the FT-process. The Fischer-Tropsch process and reactor and suitable subsequent processes and reactors for obtaining bio-naphtha, light olefins, gasoline, fuel (“FT fuels”) like diesel fuel or jet fuel (“sustainable aviation fuel”) and various options thereof suitable to be combined with the process according to the present invention are for example disclosed in Ullmann's Encyclopedia of Industrial Chemistry (2012), Chapter “Coal Liquefaction”, p. 20 to 33 and Greg Perkins et al. Bioresource Technology 312 (2020) 123596 (https: / / doi.Org / 10.1016 / j.biortech.2020.123596) and the literature mentioned therein.The process optionally further comprises the step:converting the gas stream CS manufactured by said process or a chemical material manufactured by said process to obtain a product PRF1 .The clean gas stream CS, optionally after increasing the hydrogen content as described above, may also be further converted by into a product PRF1 , wherein said product PRF1 is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orHi) industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) 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 poly isocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate, wherein preferably the content of the clean gas stream CS in the product PRF1 is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the clean gas stream CS in the product PRF1 is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the product PRF1 is a product as described in Reference RF1 ; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process for the production of a product, preferably product PRF1 .The converting step to obtain the product PRF1 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 preferablycomprises 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, syngas 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)acry I ic 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 also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term “intermediate compound”, as used 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] ofReference 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'1, 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 nonphosphate 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, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1. The term “industrial use dispersant1, 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 agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1, paragraph

[4001] , The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and 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'1and “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, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2- propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinyl i m idazole / polyvi nylpyrrol idone- 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 sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph

[5003] of Reference RF1. The converting step(s) to obtain the aroma chemical and aroma compositionmay 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 polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsion polymer”, as used herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

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

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

[6016] of Reference RF1. The term “polymeric dispersant”, as used 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- crosslinkable 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 composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

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

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

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

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

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

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

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

[6021] of Reference RF1 .The term “cosmetic surfactant”, as used 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 any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term “UV filter”, as used 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 cosmeticsurfactant, 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 present invention further concerns a production plant which is suited for working the process according to the present invention. Different aspects of said production plant are schematically shown in Figures 1 to 4.Said production plant for converting agricultural residues from fast growing plants into synthesis gas comprises(a) at least one first pretreatment unit PU1 for pretreating at least one first feedstock F1, said first pretreatment unit PU1 comprising, preferably in this order, (ia) at least one first means for shredding MS1 , (iia) at least one first means for drying MD1 , and (iiia) at least one first means for milling MM1 ,(b) at least one second pretreatment unit PU2 for pretreating at least one second feedstock F2, said first pretreatment unit PU2 comprising, preferably in this order, (ib) at least one second means for shredding MS2, (iib) at least one second means for drying MD2, and (iiib) at least one second means for milling MM2,(c) a mixing unit MU, the mixing unit downstream of and directly or indirectly fluidically connected to the first pretreatment unit PU1 and downstream of and directly or indirectly fluidically connected to the second pretreatment unit PU2, the mixing unit MU preferably further comprising a dosing system DS,(d) optionally an agglomeration unit AU, the optional agglomeration unit AU downstream of and directly or indirectly fluidically connected to the mixing unit MU, and(e) at least a first gasifier G1 , the at least one gasifier G1 downstream of and directly or indirectly fluidically connected to the mixing unit MU or to the optional agglomeration unit AU.The description concerning the individual units and their location is described in detail further above in respect to the process according to the present invention also applies for the production plant according to the present invention.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 gasification of biomass comprising the steps(i) providing at least one first feedstock F1, wherein said at least one first feedstock F1 has a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995),(ii) pretreating said at least one first feedstock F1 , the pretreatment comprising comminution and drying,(iii) providing at least one second feedstock F2, wherein said at least one second feedstock F2 has a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995),(iv) pretreating the at least one second feedstock F2, the pretreatment comprising comminution and drying,(v) combining the at least one first feedstock F1 pretreated in step (ii) and the at least one second feedstock F2 pretreated in step (iv), and thereby forming a combined feedstock CF12,(vi) optionally agglomerating said combined feedstock CF12 and thereby forming an agglomerated combined feedstock ACF12,(vii) transferring said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 through a feeding system FS into a first gasifier G1 , and(viii) subjecting said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 to a gasification process in a first gasifier G1 whereby a gas stream GS1 is formed and wherein said first gasifier G1 has at least one outlet 01 for said gas stream GS1 . Process according to embodiment 1 wherein the at least one first feedstock F1 is selected from the group comprising or preferably consisting of stalks, peels, stems, leaves, husks, shells, cobs, ears, stovers, nuts and combinations thereof, from plants having a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995). Process according to embodiment 1 or 2 wherein the at least one first feedstock F1 is selected from the group comprising or preferably consisting of corn stalks, millet stalks, kenaf stalks, sorghum stalks, sunflower stalks, hemp stalks, rice straw, wheat straw, barley straw, rye straw, oat straw, flax straw, sugarcane bagasse, oil palm empty fruit bunches, bamboo, switchgrass, miscanthus, cassava stems, banana stems, jatropha residues, soybean residues, kenaf residues, moringa residues, wheat bran, maize cobs, pineapple leaves, coffee husks, coconut husks, rice husks, tea waste, peanut shells, sorghum bagasse, other agricultural residues from fast growing plants, and combinations thereof. Process according to any one of embodiments 1 to 3 wherein the at least one first feedstock F1 is collected in a location 1 a before provided in step (i). Process according to any one of embodiments 1 to 4 wherein the at least one first feedstock F1 is pretreated in step (ii) by, preferably in this order, (a1) shredding, (b1) drying and optionally (d) milling. Process according to embodiment 5 wherein the at least one first feedstock F1 is shredded in step (ii) in at least one means for shredding MS1 , said at least one means for shredding MS1 selected from the groupcomprising or preferably consisting of disc shredders, comprehensive shredders, shear shredders, chipper shredders, tub grinders, hammer mills, bale shredders, flail mowers, rotary cutters, disk harrows, chaff cutters, mulchers, silage cutters and combinations thereof.7. Process according to embodiment 5 or 6 wherein said at least one means for shredding MS1 is located where the at least one first feedstock F1 is collected (“location 1 a”) or where the at least one feedstock F1 is formed by processing the respective agricultural residue (“location 2a”) or where the at least one gasifier G1 is operated (“location 3”) or at a location different from where the at least one first feedstock F1 is collected, sourced or formed by processing the respective agricultural residue (“location 4a”) or, in case two or more means for shredding MS1 are utilized in step (ii), distributed over “location 1a”, “location 2a”, “location 3”, and “location 4a” in any combination.8. Process according to any one of embodiments 5 to 7 wherein the major axis length of particles of the at least one first feedstock F1 after (a1) shredding preferably ranges from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).9. Process according to any one of embodiment 5 to 8 wherein the at least one feedstock F1 is dried in step (ii), preferably after shredding, in at least one means for drying MD1 , said at least one means for drying MD1 selected from the group comprising or preferably consisting of rotary dryers, fluidized bed dryers, tray dryers, belt dryers, solar dryers, drum dryers, microwave dryers and combinations thereof.10. Process according to any one of embodiments 5 to 9 wherein said at least one means for drying MD1 is located where the at least one first feedstock F1 is collected (“location 1 a”) or formed by processing the respective agricultural plant (“location 2a”) or where the at least one gasifier G1 is operated (“location 3”) or at a location different from where the at least one first feedstock F1 is collected, sourced, or formed by processing the respective agricultural residue (“location 4a”) or where the at least one means for shredding MS1 is operated (“location 5a”), or in case two or more means for drying MD1 are utilized in step (ii), they may be distributed over “location 1 a”, “location 2a”, “location 3”, “location 4a”, and “location 5a” in any combination.11. Process according to any one of embodiments 1 to 10 wherein the at least one first feedstock F1 is dried in step (ii) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).12. Process according to any one of embodiments 5 to 11 wherein the at least one feedstock F1 is milled in step (ii), preferably after shredding and drying, the at least one means for milling MM1 is selected from the group comprising or preferably consisting of hammer mill, ball mill, roller mill, fluid energy mill, pulverizer, grinder, cryogenic grinder and combinations thereof.Process according to any one of embodiments 5 to 12 wherein said optional at least one means for milling MM1 is located where the at least one first feedstock F1 is collected (“location 1a”) or formed by processing the respective agricultural plant (“location 2a”) or located where the at least one gasifier G1 is operated (“location 3”) or at a location different from where the at least one first feedstock F1 is collected, sourced, or formed by processing the respective agricultural residue (“location 4a”) or and where the at least one means for shredding MS1 and / or the at least one means for drying MD1 is / are operated (“location 5a”) or in case two or more optional means for milling MM1 are utilized in step (ii), distributed over “location 1a”, “location 2a”, “location 3”, “location 4a”, and “location 5a” in any combination. Process according to any one of embodiments 5 to 13 wherein the at least one first feedstock F1 is milled in step (ii) after drying to particles having a major axis length of less than 1 cm, preferably less than 0.5 cm and more preferably less than 0.2 cm in case the combined feedstock CF12 is agglomerated in step (vi) whereby an agglomerated combined feedstock ACF12 is formed and wherein said particle size is determined by sieving with sieves having defined mesh sizes. Process according to any one of embodiments 1 to 14 wherein the at least one second feedstock F2 is comprises of preferably consists of wood. Process according to any one of embodiments 1 to 15 wherein the at least one second feedstock F2 is selected from the group comprising or preferably consisting of wood chips, sawdust, wood pellets, bark, logging residues, forest thinnings, wood shavings, forest residues, tree trimmings, wood bark mulch, wood residues from woodworking industries, wood pulp and paper byproducts, wood sawdust pellets, tree bark mulch, wood residues from furniture manufacturing, wood shreddings, wood residues from construction and demolition, wood bark chips, wood residues from pulp and paper mills, wood residues from forestry operations, wood residues from urban tree pruning and removal, other woody biomass, and combinations thereof. Process according to any one of embodiments 1 to 6 wherein the at least one second feedstock F2 is collected in a location 1 b before provided in step (iii). Process according to any one of embodiments 1 to 17 wherein the at least one second feedstock F2 is pretreated in step (iv) by, preferably in this order, (a2) shredding, (b2) drying and (c2) milling. Process according to embodiment 18 wherein the at least one second feedstock F2 is shredded in step (iv) in at least one means for shredding MS2, said at least one means for shredding MS2 selected from the group comprising or preferably consisting of woodchippers, shredder grinders, mulchers, industrial shredders, drum chippers, mobile shredders, handheld shredders and combinations thereof.20. Process according to embodiment 18 or 19 wherein said at least one means for shredding MS2 is located where the at least one second feedstock F2 is collected (“location 1 b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”) or where the at least one gasifier G1 is operated (“location 3”), or in case two or more means for shredding MS2 are utilized in step (ii) distributed over “location 1b”, “location 2b”, “location 3”, and “location 4b” in any combination.21. Process according to any one of embodiments 18 to 20 wherein the major axis length of particles of the at least one first feedstock F1 after (a2) shredding preferably ranges from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).22. Process according to any one of embodiments 18 or 21 wherein the at least one second feedstock F2 is dried in at least one means for drying MD2, said at least one means for drying MD2 selected from the group comprising or preferably consisting of rotary dryers, fluidized bed dryers, tray dryers, belt dryers, solar dryers, drum dryers, microwave dryers, rotary kilns, fluidized bed reactors, fixed bed reactors, drum torrefiers, microwave torrefaction systems, screw pyrolysis reactors, hybrid system torrefiers and combinations thereof.23. Process according to any one of embodiments 18 to 22 wherein the at least one second feedstock F2 is dried in step (iv) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).24. Process according to any one of embodiments 18 to 23 wherein said at least one means for drying MD2 is located where the at least one second feedstock F2 is collected (“location 1 b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”) or where the at least one gasifier G1 is operated (“location 3”) or at a location different from where the at least one second feedstock F2 is collected, sourced, or formed by processing the respective at least one second feedstock F2 (“location 4b”) or where the at least one means for shredding MS2 is operated (“location 5b”), or in case two or more means for drying MD2 are utilized in step (ii), distributed over “location 1 b”, “location 2b”, “location 3”, “location 4b”, and “location 5b” in any combination.25. Process according to any one of embodiments 18 to 24 wherein the at least one second feedstock F2 is milled in at least one means for milling MM2, said at least one means for milling MM2 selected from the group comprising or preferably consisting of hammer mill, tub grinder, ball mill, roller mill, fluid energy mill, pulverizer, grinder, cryogenic grinder and combinations thereof.26. Process according to any one of embodiments 18 to 25 wherein said optional at least one means for milling MM2 is located where the at least one second feedstock F2 is collected (“location 1 b”) or formed by processing the respective at least one second feedstock F2 (“location 2b”) or located where the at least one gasifier G1 is operated (“location 3”) or at a location different from where the at least one second feedstock F2is collected, sourced, or formed by processing the respective at least one second feedstock F2 (“location 4b”) and where the at least one means for shredding MS2 and / or the at least one means for drying MD2 is / are operated (“location 5b”), or in case two or more optional means for milling MM2 are utilized in step (ii), distributed over “location 1 b”, “location 2b”, “location 3”, “location 4b”, and “location 5b” in any combination.27. Process according to any one of embodiments 18 to 26 wherein the at least one second feedstock F2 is optionally milled in step (ii) after drying to a major axis length of particles of less than 1 cm, preferably less than 0.5 cm and more preferably less than 0.2 cm in case the combined feedstock CF12 is agglomerated in step (vi) whereby agglomerates of an agglomerated combined feedstock ACF12 are formed.28. Process according to any one of embodiments 1 to 27 wherein agglomerates of an agglomerated combined feedstock ACF12 or ACF123 are formed in a location which is different from the location where the first gasifier G1 is installed.29. Process according to embodiment 27 or 28 wherein the agglomerates of an agglomerated combined feedstock ACF12 have a major axis length which ranges from 1 to 10 cm in case the first gasifier G1 is a fixed bed gasifier or a plasma fixed bed gasifier or the agglomerates of an agglomerated combined feedstock ACF12 have a size which ranges from 0.3 to 5 cm in case the first gasifier G1 is a fluidized bed gasifier, wherein said size is determined by sieving with sieves having defined mesh sizes.30. Process according to any one of embodiments 1 to 29 wherein the weight ratio “first feedstock F1 : second feedstock F2” in the combined feedstock CF12 ranges from 10 : 90 to 90 : 10.31. Process according to any one of embodiments 1 to 30 wherein the feed rate of the at least one second feedstock F2 combined with the at least one first feedstock F1 in step (v) is sufficient to form a mixed feedstock CF12 having a deformation temperature of at least 850 °C (determined according to ISO 540:1995).32. Process according to any one of embodiments 1 to 31 wherein at least one third feedstock F3 is provided and combined in step (v) with the at least one first feedstock F1 and the at least one second feedstock F2 and thereby forming a combined feedstock CF123 and / or is transferred separately through a feeding system FS into a first gasifier G1.33. Process according to embodiment 32 wherein the at least one third feedstock F3 is pretreated by at least one method selected from the group comprising or preferably consisting of shredding, drying, hydrothermal carbonization, torrefaction, milling, sorting and combinations thereof, before combined with the at least one first feedstock F1 and the at least one second feedstock F2 in step (v) and or transferred separately through a feeding system FS into a first gasifier G1 .Process according to embodiment 32 or 33 wherein the at least one third feedstock F3 comprises or preferably consists of plastic waste. Process according to any one of embodiments 1 to 34 wherein the feed rate of the at least one second feedstock F2 combined with the at least one first feedstock F1 in step (v) is sufficient to form a mixed feedstock CF123 having a deformation temperature of at least 850 °C (determined according to ISO 540:1995). Process according to any one of embodiments 1 to 35 wherein step (vi) is applied with the proviso that the first gasifier G1 is a fixed bed gasifier, fluidized bed gasifier, plasma fixed bed gasifier and wherein step (vi) is not applied with the proviso that the first gasifier G1 is an entrained flow gasifier. Process according to any one of embodiments 1 to 36 wherein the combined feedstock CF12 or, optionally the combined feedstock CF123, is agglomerated in optional step (vi) whereby an agglomerated combined feedstock ACF12 or, optionally an agglomerated combined feedstock ACF123, is formed and wherein the first gasifier G1 is selected from fixed bed gasifiers, fluidized bed gasifiers, plasma fixed bed gasifiers. Process according to any one of embodiments 1 to 37 wherein the feeding system FS is selected from the group comprising or preferably consisting of hoppers, vibratory feeders, screw feeders, belt feeders, pneumatic feeders and combinations thereof. Process according to embodiment 38 wherein the feeding system FS is rinsed with an inert gas such as CO2and / or N2during feeding the combined feedstock CF12, the combined feedstock CF123, the optional agglomerated feedstock ACF12 or ACF123 into the first gasifier G1 . Process according to any one of embodiments 1 to 39 wherein the first gasifier G1 is selected from the group comprising or preferably consisting of fixed bed gasifier, fluidized bed gasifier, entrained flow gasifier, plasma fixed bed gasifier. Process according to any one of embodiments 1 to 40 wherein the first gasifier G1 is a plasma fixed bed gasifier comprising at least one plasma torch. Process according to any one of embodiments 1 to 41 wherein the temperature in the outlet 01 of the first gasifier G1 preferably ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C. Process according to any one of embodiments 1 to 42 wherein the gas stream GS1 comprises CO, H2, CO2, methane, tar, tar oils and combinations thereof.44. Process according to any one of embodiments 1 to 43 wherein the gas stream GS1 is further converted in a second gasifier G2, wherein said second gasifier G2 is downstream of and fluidically connected by a fluid passage FP with the first gasifier G1 and in which second gasifier G2 the gas stream GS1 is converted into a gas stream GS2.45. Process according to embodiment 44 wherein the second gasifier G2 is an entrained flow gasifier.46. Process according to embodiment 44 or 45 wherein said first gasifier G1 is a fixed bed gasifier or a fluidized bed gasifier and wherein said second gasifier G2 is an entrained flow gasifier.47. Process according to any one of embodiments 44 to 46 wherein the fluid passage FP comprises or preferably consists of a pipe and / or a cyclone.48. Process according to any one of embodiments 44 to 47 wherein the temperature of gas stream GS1 in the fluid passage FP preferably ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C.49. Process according to any one of embodiments 44 to 48 wherein the CO content and / or the H2 content in gas stream GS2 is higher than the CO and / or H2 content in gas stream GS1.50. Process according to any one of embodiments 44 to 49 wherein the gas stream GS1 or GS2 is subjected to at least one gas cleaning process in a gas treatment unit GTU whereby a clean synthesis gas stream CS is formed, said at least one gas cleaning process selected from the group comprising water wash, CO2 removal, sulfur removal, HCI removal, Hg removal, HCN / NH3 removal and combinations thereof.51. Process according to embodiment 50 wherein at least a portion of the clean synthesis gas stream CS is further converted into methanol, ethanol, mixed alcohols, methane or into a mixture of hydrocarbons HC by a Fischer-T ropsch process.52. Process according to any one of embodiments 1 to 51 , comprising the step: converting the gas stream CS manufactured by the process according to embodiment 49 or 50 or a chemical material manufactured by the process according to any one of embodiments 1 to 50 to obtain a product PRF1.53. Process according to embodiment 52, wherein the product PRF1 is selected from: i) building block or monomer; orii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orHi) industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) 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 vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate. Process according to embodiment 52 or 53, wherein the content of the gas stream GS1 , GS2 or OS in the product PRF1 is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the gas stream GS1, GS2 or OS in the product PRF1 is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard. Production plant for converting agricultural residues from fast growing plants into synthesis gas comprising(a) at least one first pretreatment unit PU1 for pretreating at least one first feedstock F1, said first pretreatment unit PU1 comprising, preferably in this order, (ia) at least one first means for shredding MS1 , (iia) at least one first means for drying MD1 , and optionally (iiia) at least one first means for milling MM1 ,(b) at least one second pretreatment unit PU2 for pretreating at least one second feedstock F2, said first pretreatment unit PU2 comprising, preferably in this order, (ib) at least one second means for shredding MS2, (iib) at least one second means for drying MD2, and optionally (iiib) at least one second means for milling MM2,(c) a mixing unit MU, the mixing unit downstream of and directly or indirectly fluidically connected to the first pretreatment unit PU1 and downstream of and directly or indirectly fluidically connected to the second pretreatment unit PU2, the mixing unit MU preferably further comprising a dosing system DS,(d) optionally an agglomeration unit AU, the optional agglomeration unit AU downstream of and directly or indirectly fluidically connected to the mixing unit MU, and(e) at least a first gasifier G1 , the at least one gasifier G1 downstream of and directly or indirectly fluidically connected to the mixing unit MU or to the optional agglomeration unit AU.The invention will be further explained by the following non-limiting examples.GeneralThe gasification of feedstocks F1 , F2 and mixtures thereof and their respective fouling behavior was simulated. Properties of the feedstocks used for the simulations are summarized in T able 1. All simulations were performed with the Aspen Plus simulation package, version 14. Undesired fouling was associated with the concentration of all C- containing molecules comprising more than one carbon atom formed in the first gasifier G1 of which at least a portion condensed as liquid in the outlet 01 of the gasifier G1 and in the fluid passage FP between gasifiers G1 and G2 and thereby caused undesired fouling in said fluid passage FP.Table 1 : Feedstocks for the simulations (HV represents the higher heating value in MJ / kg, DT represents the deformation temperature (determined according to ISO 540:1995 and given in °C), all other numbers in the following table are given in wt.-%, mixture data are also given as wt.-%:Rice straw is an agricultural residue having a deformation temperature of 800 °C and is, accordingly, a “first feedstock FT’. Beech wood is a wood having a deformation temperature of 1100 °C and is, accordingly, a “second feedstock F2”.Comparative example 1A first feedstock F1 (pretreated rice straw) having a low deformation temperature was converted in a fluidized bed gasifier (=first gasifier G1) into a gas stream GS2 and (downstream and fluidically connected to G1 by a fluid passage FP) further converted in an entrained flow gasifier (=second gasifier G2) into a gas stream GS2. The rice straw had the mass composition given in table 1 and was added at 35 °C, 4 bar and with a feed rate of 2.11 kg first feedstock F1 / kg gas stream GS1 . Additional to the first feedstock F1 , steam (5 bar, 200 °C) with a feed rate of 1 .06 kg steam / kg gas stream GS1 and pure oxygen (6 bar, 25 °C) with a feed rate of 0.31 kg oxygen / kg gas stream GS1 were added to reach a gasifier G1 outlet 01 temperature of the gas stream GS1 of 750 °C. This temperature needed to be applied to avoid undesired sticking and agglomeration of rice straw particles within the fluidized bed in gasifier G1 which destroys the fluidized bed. Such undesired sticking and agglomeration of rice straw particles starts at 800 °C, due to deformation temperature of 800 °C of the rice straw. The gas stream GS1 comprised under these conditions (caused by the deformation temperature of rice straw) 0.17 kg carbon / kg gas stream GS1 . Carbon referred in this comparative example to all C-containing molecules comprising more than one carbon atom formed in the first gasifier G1 . A certain part of these C-containing molecules condensed as liquid in the outlet 01 of the gasifier G1 and in the fluid passage FP between gasifiers G1 and G2 and thereby caused undesired fouling in said fluid passage FP. After the fluidized bed gasifier (first gasifier G1), the gas stream GS1 entered an entrained flowgasifier (second gasifier G2) via a burner nozzle. Additionally, pure oxygen was added (6 bar, 25 °C) with 0.71 kg oxygen / kg gas stream GS2 to convert gas stream GS1 into gas stream GS2 with 1350 °C at the outlet of the second gasifier G2. The gas stream GS2 comprised 0.93 kg CO / kg gas stream GS2, 0.07 kg H2 / kg gas stream GS2 and 1 .23 kg CO2 / kg gas stream GS2. The molar ratio of H2 : CO in gas stream GS2 was 0.99.Comparative Example 2The same first feedstock F1 (also same feed-rate, temperature and pressure) was converted in a fixed-bed gasifier G1 into a gas stream GS1 . To avoid undesired melting and / or plugging of the first feedstock F1 in the bottom section of gasifier G1, steam and pure oxygen were added to reach a gasifier G1 outlet 01 temperature of the gas stream GS1 of 750 °C. The gas stream GS1 comprised under these conditions C-containing molecules comprising more than one carbon atom formed in the first gasifier G1. The gas stream GS1 was then converted into a gas stream GS2 in a second gasifier G2 (entrained flow gasifier). A certain part of these C-containing molecules condensed as liquid in the outlet 01 of the gasifier G1 . and in the fluid passage FP between gasifiers G1 and G2 and thereby caused undesired fouling in said fluid passage FP.Example 1A combined feedstock CF12 consisting of a mixture of a first feedstock F1 (rice straw) and a second feedstock F2 (beech wood) were converted in a fluidized bed gasifier (first gasifier G1) into a gas stream GS1 and the resulting gas stream GS1 was further converted into a gas stream GS2 in an entrained flow gasifier (second gasifier G2), said second gasifier G2 downstream of and fluidically connected by a fluid passage FP to the first gasifier G1. A combined feedstock CF12 consisting of a weight-based 50:50 mixture of the first feedstock F1 (rice straw) and the second feedstock F2 (beech wood) was fed at 35 °C, 4 bar and with 1.88 kg combined feedstock CF12 / kg gas stream GS1 into the first gasifier G1 . In addition to the combined feedstock CF12, steam (5 bar, 200 °C) with 0.94 kg steam / kg first gas stream GS1 and pure oxygen (6 bar, 25 °C) with 0.57 kg oxygen / kg gas stream GS1 were fed into the first gasifier G1 to reach a temperature of the gas stream GS1 at the outlet 01 of the first gasifier G1 of 900 °C. This temperature was a desired outlet temperature for a fluidized bed gasifier to maintain the fluidized bed, and which can be applied because the deformation temperature of the combined feedstock CF12 is above 900 °C. Due to the desired outlet temperature of 900 °C, gas stream GS1 comprised 0.0 kg carbon / kg gas stream GS1. Accordingly, no C-containing molecules were available that could have condensed as liquid in the fluid passage FP between the first gasifier G1 and the second gasifier G2. As the result, no undesired fouling was caused in said fluid passage FP. The gas stream GS1 was fed into an entrained flow gasifier (second gasifier G2) via a burner nozzle. Additionally, pure oxygen was fed (6 bar, 25 °C) with 0.39 kg oxygen / kg gas stream GS2 to convert gas stream GS1 into gas stream GS2 with 1350 °C at the outlet of the second gasifier G2. Gas stream GS2 comprised 0.93 kg CO / kg gas stream GS2, 0.07 kg H2 / kg gas stream GS2 and 1.17 kg CO2 / kg gas stream GS2. The molar ratio of H2 : CO in gas stream GS2 was 0.97.Example 2A combined feedstock CF12 consisting of a mixture of a first feedstock F1 (rice straw) and a second feedstock F2 (beech wood) were converted in a fixed bed gasifier (first gasifier G1 ) into a gas stream GS1 and the resulting gas stream GS1 was further converted into a gas stream GS2 in an entrained flow gasifier (second gasifier G2), said second gasifier G2 downstream of and fluidically connected by a fluid passage FP to the first gasifier G1. A combined feedstock CF12 consisting of a weight-based 50:50 mixture of the first feedstock F1 (rice straw) and the second feedstock F2 (beech wood) was ted into the first gasifier G1. In addition to the combined feedstock CF12, steam and pure oxygen were fed into the first gasifier G1 to reach a temperature of the gas stream GS1 at the outlet 01 of the first gasifier G1 of 900 °C. This temperature was a desired outlet temperature for a fluidized bed gasifier to maintain the fluidized bed, and which can be applied because the deformation temperature of the combined feedstock CF12 is above 900 °C. Due to the desired outlet temperature of 900 °C, gas stream GS1 comprised no C- containing molecules that could have condensed as liquid in the fluid passage FP between the first gasifier G1 and the second gasifier G2. As the result, no undesired fouling was caused in said fluid passage FP.

Claims

Claims1 . Process for gasification of biomass comprising the steps(i) providing at least one first feedstock F1, wherein said at least one first feedstock F1 has a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995),(ii) pretreating said at least one first feedstock F1 , the pretreatment comprising comminution and drying,(iii) providing at least one second feedstock F2, wherein said at least one second feedstock F2 has a deformation temperature of 1100 to 2000 °C (determined according to ISO 540:1995),(iv) pretreating the at least one second feedstock F2, the pretreatment comprising comminution and drying,(v) combining the at least one first feedstock F1 pretreated in step (ii) and the at least one second feedstock F2 pretreated in step (iv), and thereby forming a combined feedstock CF12,(vi) optionally agglomerating said combined feedstock CF12 and thereby forming an agglomerated combined feedstock ACF12,(vii) transferring said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 through a feeding system FS into a first gasifier G1 , and(viii) subjecting said combined feedstock CF12 or said optional agglomerated combined feedstock ACF12 to a gasification process in a first gasifier G1 whereby a gas stream GS1 is formed and wherein said first gasifier G1 has at least one outlet 01 for said gas stream GS1 .

2. Process according to claim 1 wherein the at least one first feedstock F1 is selected from the group comprising or preferably consisting of stalks, peels, stems, leaves, husks, shells, cobs, ears, stovers, nuts and combinations thereof, from plants having a deformation temperature of 700 to 1000 °C (determined according to ISO 540:1995).

3. Process according to claim 1 or 2 wherein the at least one first feedstock F1 is pretreated in step (ii) by, preferably in this order, (a1) shredding, (b1) drying and optionally (d) milling.

4. Process according to any one of claims 1 to 3 wherein the major axis length of particles of the at least one first feedstock F1 after (a1) shredding preferably ranges from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).

5. Process according to any one of claims 1 to 4 wherein the at least one first feedstock F1 is dried in step (ii) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).

6. Process according to any one of claims 1 to 5 wherein the at least one second feedstock F2 is comprises of preferably consists of wood.

7. Process according to any one of claims 1 to 6 wherein the at least one second feedstock F2 is pretreated in step (iv) by, preferably in this order, (a2) shredding, (b2) drying and (c2) milling.

8. Process according to any one of claims 1 to 7 wherein the major axis length of particles of the at least one first feedstock F1 after (a2) shredding preferably ranges from 0.5 to 5 cm, more preferably 0.5 to 4 cm and most preferably 0.5 to 3 cm (determined by sieving with sieves having defined mesh sizes).

9. Process according to any one of claims 1 to 8 wherein the at least one second feedstock F2 is dried in step (iv) to a residual water content preferably less than 25 wt.%, more preferably less than 20 wt.-% and most preferably less than 17.5 wt.-% (residual water content measured according to ISO 21660-3:2021).

10. Process according to any one of claims 1 to 9 wherein the feed rate of the at least one second feedstock F2 combined with the at least one first feedstock F1 in step (v) is sufficient to form a mixed feedstock CF12 having a deformation temperature of at least 850 °C (determined according to ISO 540:1995).

11. Process according to any one of claims 1 to 10 wherein the combined feedstock is agglomerated in optional step (vi) whereby an agglomerated combined feedstock ACF12 is formed and wherein the first gasifier G1 is selected from fixed bed gasifiers, fluidized bed gasifiers, plasma fixed bed gasifiers.

12. Process according to any one of claims 1 to 11 wherein the temperature in the outlet 01 of the first gasifier G1 preferably ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C.

13. Process according to any one of claims 1 to 12 wherein the gas stream GS1 is further converted in a second gasifier G2, wherein said second gasifier G2 is downstream of and fluidically connected by a fluid passage FP with the first gasifier G1 and in which second gasifier G2 the gas stream GS1 is converted into a gas stream GS2.

14. Process according to claim 13 wherein the temperature of gas stream GS1 in the fluid passage FP preferably ranges from 800 to 1000 °C, more preferably 825 to 1000 °C and most preferably 850 to 1000 °C.

15. Process according to claim 13 or 14 wherein the gas stream GS1 or GS2 is subjected to at least one gas cleaning process in a gas treatment unit GTU whereby a clean synthesis gas stream CS is formed, said at least one gas cleaning process selected from the group comprising water wash, CO2 removal, sulfur removal, HCI removal, Hg removal, HCN / NH3 removal and combinations thereof.

16. Process according to any one of claims 1 to 15, comprising the step: converting the gas stream CS manufactured by the process according to claim 15 or a chemical material manufactured by the process according to any one of claims 1 to 15 to obtain a product PRF1 .

17. Process according to claim 16, wherein the product PRF1 is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orHi) industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) 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 vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.

18. Production plant for converting agricultural residues from fast growing plants into synthesis gas comprising(a) at least one first pretreatment unit PU1 for pretreating at least one first feedstock F1, said first pretreatment unit PU1 comprising, preferably in this order, (ia) at least one first means for shredding MS1, (iia) at least one first means for drying MD1 , and optionally (iiia) at least one first means for milling MM1 ,(b) at least one second pretreatment unit PU2 for pretreating at least one second feedstock F2, said first pretreatment unit PU2 comprising, preferably in this order, (ib) at least one second means for shredding MS2, (iib) at least one second means for drying MD2, and optionally (iiib) at least one second means for milling MM2,(c) a mixing unit MU, the mixing unit downstream of and directly or indirectly fluidically connected to the first pretreatment unit PU1 and downstream of and directly or indirectly fluidically connected to the second pretreatment unit PU2, the mixing unit MU preferably further comprising a dosing system DS,(d) optionally an agglomeration unit AU, the optional agglomeration unit AU downstream of and directly or indirectly fluidically connected to the mixing unit MU, and(e) at least a first gasifier G1 , the at least one gasifier G1 downstream of and directly or indirectly fluidically connected to the mixing unit MU or to the optional agglomeration unit AU.

Images