Process for reducing wastewater formed during gasification of locally sourced biomass

Abstract

The invention concerns the reduction of wastewater during the gasification of locally sourced biomass through a process involving a first gasifier G1 located at a first location L1, operating within an optimized capacity window of 80 to 100 % for the feedstock F1. Feedstock F1, sourced from a second location L2 within the same 40,000 km2 area in which the gasifier G1 is located, may be optionally pretreated in units at L1, L2, or L3. During a specific timeframe t, the availability of feedstock F1 and pretreated feedstock PF1 is assessed and compared to the requirements for maintaining optimized gasifier operation within an optimized capacity window of 80 to 100 % for the feedstock F1. If available feedstock is less than 50 % of maximum capacity, a second feedstock F2 is introduced to maintain synthesis gas production SG1, thereby reducing wastewater. The process also minimizes CO2 emissions by controlling the ratio of partial oxidation to total oxidation during gasification.

Description

240909W0021Process for reducing wastewater formed during gasification of locally sourced 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 inventionThe (petro-)chemical industry is facing a growing demand for biomass-derived products, including methanol and hydrocarbon-based fuels. These can be produced from synthesis gas via catalytic methods, such as methanol synthesis or Fischer-Tropsch synthesis followed by processes such as catalytic reforming and isomerization.Biomass gasification generates the synthesis gas essential for these pathways. The resulting methanol and hydrocarbon-based fuels are often termed "bio-methanol" and "sustainable (aviation) fuels".Gasification processes using biomass feedstocks, particularly using locally sourced biomass feedstocks, are susceptible to feedstock shortages caused by various factors such as severe weather conditions, lack of nutrition, insect infestations, and wildfires. On the other hand, the sourcing of biomass feedstocks is limited by the transportation fuel required to transport the feedstock from its source (e.g., arable land, forest) to the location of the gasifier(s) used in the gasification process. The distance between the feedstock source and the gasifier(s) should be smaller than the benefit gained from utilizing the biomass feedstock for synthesis gas production. Generally, biomass feedstocks should be sourced within an area of no more than 40,000 km2around the gasifier(s) location. Therefore, the availability of economically viable biomass feedstocks for gasification processes is limited and constantly under threat.The biomass needed to run a given gasifier effectively varies with the gasifier's size, layout and gasification process. Operating within 80 to 100 % of the feedstock capacity of a given gasifier, known as the "optimized operational window," ensures desirable synthesis gas production. Below this range, the gasifier produces increased amounts of wastewater and CO2compared to the operation of a gasifier within 80 to 100 % of the feedstock capacity of a given gasifier.In fluidized bed gasifiers, a medium such as sand creates a fluidized bed when exposed to steam. The quantity of this medium must be significantly greater than the feedstock to achieve the desired fluidized bed. This requirement is constant, irrespective of the feedstock amount fed into a gasifier, meaning the same amount of steam (which becomes wastewater loaded with organic residues such as tar during the gasification process) is needed regardless of feedstock input. Consequently, the volume of wastewater remains unchanged even if the gasifier operates below its optimal capacity (= below the respective “optimized operational window”).In fixed bed gasifiers, the means for feeding steam into the gasifier (e.g., one or more nozzle) provides steam in a quantity required for the optimized operational window of a given gasifier. Hence, the size and / or layout of the one or more nozzle is only suited for a steam feed amount required for 80 to 100 % of the feedstock capacity of a given240909W0022gasifier. The quantity of steam fed into said gasifier cannot be reduced below a certain quantity which represents the amount of steam required for the partial oxidation reaction at the lower margin of feedstock amount (less than 50 % of the gasifiers maximum feedstock capacity). Accordingly, the ratio “syngas produced” : “wastewater produced” decreases strongly in case less than about 50 % of the gasifiers maximum feedstock capacity are fed to a given fixed bed gasifier.In entrained flow gasifiers, the steam input remains almost constant regardless of the feedstock amount. This is because (1) steam prevents undesired backflow of oxygen into the supply pipes in case of a gasifier failure, and (2) steam protects the burner(s) from local temperature increases. Therefore, wastewater volume stays the same even if the gasifier operates below its optimal capacity.Generally, feeding a gasifier with less than about 50 % of its maximum feedstock capacity leads to excessive wastewater production (in relation to the yield of synthesis gas) and a low yield of synthesis gas.Additionally, gasifiers generate heat during operation, necessitating continuous heating of the internal reactor volume to sustain the temperature range required for the partial oxidation of the feedstock. This heating is achieved through the complete oxidation of a portion of the feedstock inside the gasifier. The total oxidation reaction resulting in CO2and H2O instead of CO and H2is exothermic. If less than about 50 % of the maximum capacity of feedstock is fed into a given gasifier, this also results in the production of more undesired CO2, related to the mass flow ratio “CO2: (CO + H2)”.It is an objective to provide a process for reducing the wastewater formed during gasification of locally sourced biomass.It is a further objective of the present invention to control the weight ratio “synthesis gas produced : wastewater generated in a first gasifier” during gasification of locally sourced biomass.It is a further objective to provide a process for reducing the CO2emission during gasification of locally sourced biomass.Summary of the inventionThese objectives are solved by a process for reducing wastewater during gasification of locally sourced biomass, said process comprising the steps(i) providing a first gasifier G1, wherein said first gasifier G1 is in a first location L1, and wherein said first gasifier G1 has an optimized operational window for converting at least one first feedstock F1 into synthesis gas SG1 by gasification in said first gasifier G1, wherein said optimized operational window is defined as 80 to 100 % capacity for the at least one first feedstock F1 in said first gasifier G1 and wherein 80 % is the lower boundary240909W0023and 100 % is the maximum capacity for the at least one first feedstock F1 or the sum of all feedstocks F1 in said first gasifier G1,(ii) sourcing at least one first feedstock F1 from at least a second location L2, wherein the first location L1 and the at least one second location L2 are co-located within an area AR of no more than 40,000 km2,(iii) transporting said at least one first feedstock F1 from the at least one second location L2 to the first location L1 or to a third location L3, said third location L3 also co-located within said area AR,(iv) optionally pretreating said at least one first feedstock F1 in at least one pretreatment unit PU, wherein said at least one pretreatment unit is in at least one of the locations selected from the group consisting of L1 , L2 and L3, and whereby at least one pretreated first feedstock PF1 is formed in said at least one pretreatment unit PU,(v) determining in all locations selected from the group consisting of L1 , L2 and L3 the amount of the at least one first feedstock F1 and / or the amount of the at least one optionally pretreated first feedstock PF1 available during a timeframe t, preferably during a timeframe t at location L1 only,(vi) comparing the amount of at least one first feedstock F1 and / or the amount of at least one optionally pretreated at least one first feedstock PF1 available during said timeframe t, preferably during a timeframe t at location L1 only, determined in step (v) with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t,(vii) providing at least one second feedstock F2 in case the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is less than 50 % of the maximum capacity for the at least one first feedstock F1 of said first gasifier G1 during said timeframe t,(viii) converting said at least one first feedstock F1 and / or the optionally pretreated at least one first feedstock PF1 and the at least one second feedstock F2 provided in step (vii) in the first gasifier G1 into synthesis gas SG1, whereby wastewater WW is formed.The weight ratio “synthesis gas SG1 produced : wastewater generated in the first gasifier G1” during gasification of locally sourced biomass can be controlled by the process according to the present invention. Thereby, the wastewater WW formed during gasification of locally sourced biomass is reduced.The CO2 emission during gasification of locally sourced biomass is reduced by the process according to the present invention, because the ratio “partial oxidation : total oxidation” can be kept in the desired range.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 or240909W0024substitutions within the basic spirit of the present invention are still within the scope of the present invention as claimed.The term “at least one”, particularly in respect to feedstocks may include one, two, three, four, five and so on types of feedstocks. For example, “at least one feedstock FT’ may include one, two, three, four, five and so on selected from the respective list for feedstocks F1 and “at least one feedstock F2” may include one, two, three, four, five and so on selected from the respective list for feedstocks F2.In step (i) of the process according to the present invention, a first gasifier G1 is provided. Said first gasifier G1 is in a first location L1. Said first gasifier G1 has an optimized operational window for converting at least one first feedstock F1 into synthesis gas SG1 by gasification in said first gasifier G1. Said optimized operational window is defined as 80 to 100 % capacity for the at least one first feedstock F1 in said first gasifier G1. 80 % is the lower boundary and 100 % is referred to as “maximum” capacity for the at least one first feedstock F1 or the sum of all feedstocks F1.The “optimized operational window” of a reactor in chemical processes (e.g., of a gasifier in a gasification process) refers to the specific set of conditions at which the reactor is designed to operate optimally. It is a combination of various parameters such as temperature, pressure, flow rate of the feedstock that are carefully chosen to ensure efficient and safe operation of the reactor. The optimized operational window of a gasifier in a gasification process is reached at 80 to 100 % of the capacity for the at least one first feedstock F1 or the sum of all feedstocks F1. The optimized operational window is determined and provided by the manufacturer of gasifiers to the operators of a given gasifier. Such manufactures use engineering methods known to the skilled person to determine said optimized operational window of a given gasifier.The first gasifier G1 is selected from the group consisting of fluidized bed gasifiers, fixed bed gasifiers and entrained flow gasifiers.In step (ii), at least one first feedstock F1 is sourced from at least one second location L2, wherein the first location L1 and the at least one second location L2 are co-located within an area AR of no more than 40,000 km2.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, empty fruit bunches, empty nut bunches and combinations thereof.The at least one first feedstock F1 is more preferably selected from the group comprising or most 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, 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.240909W0025The at least one first feedstock F1 is sourced from at least a second location L2 by a method selected from the group comprising or preferably consisting of harvesting, separating from mills, separating from presses, separating from means for shredding (e.g., harvesters, shredders), separating from dryers (e.g., rice dryers), separating from pelletizers and combinations thereof.In step (iii), said at least one first feedstock F1 is transported from the at least one second location L2 to the first location L1 or to a third location L3, said third location L3 also being co-located within said area AR.The at least one first feedstock F1 is transported from the at least one second location L2 to the first location L1 or to a third location L3 by a method selected from the group comprising or preferably consisting of transportation by truck, transportation by trailer, transportation by compact three-wheeled vehicles, transportation by train, transportation by drones, transportation by ship, transportation by boat and combinations thereof.The term "ship" is defined as larger vessels that meet certain regulatory standards. The term "boat" is defined as smaller vessels than “ships”. Boats are usually intended for shorter trips and are often used in inland waters such as rivers, lakes, and coastal areas.In step (iv), said at least one first feedstock F1 is optionally pretreated in at least one pretreatment unit PU, wherein said at least one pretreatment unit is in at least one of the locations selected from the group consisting of L1, L2 and L3, and whereby at least one pretreated first feedstock PF1 is formed in said at least one pretreatment unit PU.The at least one first feedstock F1 is optionally pretreated by a method selected from the group comprising or preferably consisting of, preferably in this order, (a1) shredding, (b1) drying and optionally (d) milling.The at least one first feedstock F1 is preferably shredded in step (iv) a1 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 is located at least one of the locations selected from the group consisting of L1, L2 and L3.240909W0026Chipper 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 first feedstock F1 is preferably dried in step (iv) b1, 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 first 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 is preferably located at least one of the locations selected from the group consisting of L1, L2 and L3.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. This240909W0027promotes 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 (iv) b1 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 (iv) d , 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 is preferably located at least one of the locations selected from the group consisting of L1, L2 and L3.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 (iv) a1.240909W0028In step (v), the amount of the at least one first feedstock F1 and / or the amount of the at least one pretreated first feedstock PF1 available during a timeframe t is determined in all locations selected from the group consisting of L1, L2 and L3. Preferably, the amount of the at least one first feedstock F1 and / or the amount of the at least one pretreated first feedstock PF1 available during a timeframe t is determined at location L1 only.The amount of at least one first feedstock F1 (or the sum all feedstocks F1 in case more than one feedstock F1 is employed) and / or the amount of optionally pretreated at least one first feedstock PF1 (and / or the sum of all optionally pretreated feedstocks PF1 in case more than one optionally pretreated feedstock PF1 is employed) in all locations selected from the group consisting of L1, L2 and L3 combined or, preferably only at location L1, is determined by a method selected from the group comprising or preferably consisting of weighting, determining the volume, receiving the weather forecast, obtaining a forecast by local feedstock providers and / or feedstock traders, and combinations thereof...Amount" of the at least one first feedstock F1 and / or the amount of optionally at least one pretreated first feedstock PF1 in all locations selected from the group consisting of L1, L2 and L3 combined during a timeframe t, preferably during a timeframe t at location L1 only, means weight or volume thereof. The weight can be measured with balances (scales). The volume of the at least one first feedstock F1 stored, e.g., in a silo or a bunker can be determined for example with level-sensors such as radar sensors, ultrasonic sensors, capacitive sensors and plumb bob sensors and / or rotating paddle detectors, vibrating level switches, and membrane switches. Devices utilizing such levelsensors and / or switches are for example available from MBA Instruments GmbH.The timeframe t is preferred as the basis for determining said amount to ensure a continuous production of synthesis gas SG1 by gasification in said at least first gasifier G1. This means that enough of the at least one first feedstock F1 and / or the at least one pretreated feedstock PF1 is stored at or will be available at location L1 (the location where the first gasifier G1 is located) during said timeframe t. Said continuous production is required to reduce the wastewater formed during gasification of locally sourced biomass and to control the weight ratio “synthesis gas SG1 produced : wastewater generated in the first gasifier G1” during gasification of locally sourced biomass. Said continuous production of synthesis gas SG1 is also required for reducing the CO2 emission during gasification of locally sourced biomass. Said timeframe t is preferably 5 to 10 days but may also be shorter, e.g., 3 or 4 days, or longer, e.g., 12 or 15 days. Hence, the timeframe t is preferably 3 to 15 days, more preferably 4 to 12 days and most preferably 5 to 10 days.The amount of available first feedstock F1 in at least one location selected from the group consisting of L1, L2 and L3 may be influenced by one or more of the following incidents: severe weather conditions (e.g., storm, flooding), climate conditions (e.g., too hot, too dry), lack of nutrition, fire, pest plague, incorrect fertilization, insect infestations and fungal infestation.240909W0029Said one or more incidents can be recognized for example by controlling the silo level of the silo in which the at least one first feedstock F1 and / or the at least one pretreated feedstock PF1 is / are stored at location L1 , when scheduled delivery of further at least one first feedstock F1 and / or further at least one pretreated first feedstock PF1 to location L1 expected during said timeframe t is delayed, by receiving a message from supplier and / or trader of at least one first feedstock F1 and / or at least one pretreated feedstock PF1 that at least a portion of the scheduled delivery to location L1 during said timeframe t is cancelled or will be postponed for after said timeframe t, by receiving an information about severe weather conditions (and / or an incident such as pest plague, insect infestations, fungal infestation, flooding) which will limit the available at least one first feedstock F1 and / or at least one pretreated first feedstock PF1 at location L1 during said timeframe t.In step (vi), the available amount of the at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is compared with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t.The available amount of the at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is compared with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for constant feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t by a method selected from the group comprising or preferably consisting of stock management, stock accounting, matching the existing amount of first feedstock F1 and the required amount of first feedstock F1 for the timeframe t at the location of said first gasifier G1 (location L1). Such methods may be performed manually or by or with support of IT such as dedicated software and / or hardware.A preferred method for “comparing” the amount of available first feedstock F1 and / or the amount of optionally pretreated first feedstock PF1 determined in step (v) with the feed rate of first feedstock F1 and / or the amount of optionally pretreated first feedstock PF1 required for the optimized operational window (80 to 100 % capacity for the first feedstock F1) of said first gasifier G1” is described in the following:The formula "A + B > C” expresses the desired regular operation of the first gasifier G1, i.e., operation within the optimized operational window of said first gasifier G1 during a timeframe t.“A” is the “amount” of the first feedstock F1 and / or optionally pretreated first feedstock PF1 available in location L1, which amount is preferably determined by weighting and / or determining the volume as described above.“B” is the “amount” of the at least one first feedstock F1 and / or at least one pretreated feedstock PF1 which is scheduled to be transported from location L2 and / or location L3 during a timeframe t to location L1.240909W00210“C” is the overall “amount” of feedstock(s) required for operating the first gasifier G1 at the optimized operation window of said first gasifier G1 during said timeframe t.In case the amount A and / or the amount B is less than amount C during said timeframe t, at least one second feedstock F2 needs to be fed into the first gasifier G1. Otherwise, the first gasifier G1 is operated below the optimized operation window of said first gasifier G1 during said timeframe t, whereby the amount wastewater formed during gasification of locally sourced biomass increases, particularly the amount of wastewater per synthesis gas produced. This technical effect is shown in the experimental section.In step (vii), at least one second feedstock F2 is provided in case the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is less than 50 % of the maximum capacity for the at least one first feedstock F1 of said first gasifier G1 during said timeframe t.The at least one second feedstock F2 is selected from the group comprising or preferably consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), coal, tar oils, natural gas, CO2, waste streams from tire production, presorted automotive shredder residue (ASR), and mixtures thereof, wherein said biomass is different than the first feedstock F1 and / or the pretreated first feedstock PF1 provided by steps (ii) to (iv).In step (viii), said at least one first feedstock F1 and / or the optionally pretreated at least one first feedstock PF1 and the at least one second feedstock F2 provided in step (vii) are converted in the first gasifier G1 into synthesis gas SG1 , whereby wastewater WW is formed. The synthesis gas SG1 formed in the first gasifier G1 comprises CO, H2, CO2, methane and wastewater WW. Wastewater WW is preferably separated from synthesis gas SG1 by condensation.Optionally, the synthesis gas SG1 is converted in a second gasifier G2 into a synthesis gas SG2. This aspect is preferred in case the first gasifier G1 is selected from fixed bed gasifiers and fluidized bed gasifiers. In such a case, the gasifier G2 is preferably an entrained flow gasifier. The synthesis gas SG2 formed in optional gasifier G2 comprises CO, H2, CO2, methane and wastewater WW. Wastewater WW is preferably separated from synthesis gas SG2 by condensation.Preferably, the first gasifier G1 is selected from the group comprising or preferably consisting of fixed bed gasifier, fluidized bed gasifier, and entrained flow gasifier.240909W00211An overview of suitable gasifiers G1 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 synthesis gas SG1 is further converted in a second gasifier G2. Said optional second gasifier G2 is fluidically connected to the first gasifier G1 and said optional second gasifier G2 is downstream of said first gasifier G1. Preferably, the optional second gasifier G2 is an entrained flow gasifier. The synthesis gas SG1 is converted in said optional second gasifier G2 into synthesis gas SG2. Preferably, the CO content and / or the H2 content in synthesis gas SG2 is higher than the CO and / or H2 content in synthesis gas SG1.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 optional further feedstock FF may be co-fed with synthesis gas SG1 into said optional second gasifier G2.Said optional at least one further feedstock FF is selected from the group comprising or preferably consisting of biooil, 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.The optional at least one further feedstock FF is preferably pre-heated and / or pressurized before fed into the optional 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 further feedstock FF 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 further feedstock FF by the skilled person.Optionally, the synthesis gas SG1 or SG2 is subjected to at least one gas cleaning process in a gas treatment unit GTU whereby a clean synthesis gas stream SOS 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 to the first gasifier G1.Typical impurities in the synthesis gas SG1 or synthesis gas SG2 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 said240909W00212synthesis gas SG1 or synthesis gas SG2 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 synthesis gas SG1 or synthesis gas SG2 and the tolerance to such impurities in a further process (see below). Some selected methods for removal of impurities from said synthesis gas SG1 or synthesis gas SG2 will be discussed in more detail. One or more of said 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 HOI and H2S are formed and / or separated from the synthesis gas SG1 or synthesis gas SG2 in the optional gas treatment unit GTU. The impurities are removed from the synthesis gas SG1 and synthesis gas SG2 having a first molar ratio CO : H2is obtained.Particulate impurities can be removed from the synthesis gas SG1 or synthesis gas SG2 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 synthesis gas SGI may also be removed with a quench in a soot water washing unit.Fine particles can be optionally removed directly with filters after the synthesis gas SG1 leaves the first gasifier G1 or the synthesis gas SG2 leaves the optional second gasifier G2 in case two gasifiers G1 and G2 are employed. Hence, the removal of fine particles from the synthesis gas SG1 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 to the first gasifier G1 , the removal of fine particles from the synthesis gas SG2 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 synthesis gas SG1 or the synthesis gas SG2. 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 the synthesis gas SG1 or synthesis gas SG2 by the skilled person.CO and / or H2are optionally separated from the synthesis gas SG1, synthesis gas SG2 or gas stream CS. CO can be separated from the synthesis gas SG1, synthesis gas SG2 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 synthesis gas SG1, synthesis gas SG2 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. In case CO is separated from the synthesis gas SG1 in a cold box, said cold box is preferably also suited to separate methane from synthesis gas SG1. H2can be separated using H2-selective membranes thorough which H2permeates and is thereby separated from synthesis gas SG1, synthesis gas SG2 or gas stream CS.240909W00213Optionally, the synthesis gas SG1, synthesis gas SG2 or gas stream OS is then subjected to a water-gas shift reaction in a water-gas shift unit in which the molar ratio CO : H2 of the respective gas stream is changed by increasing the H2 content. The hydrogen content in the synthesis gas SG1, synthesis gas SG2 or gas stream OS can also be increased by adding hydrogen provided by another source such as hydrogen formed by electrolysis of water, preferably using electrical energy from a renewable source such as solar and / or wind energy, or methane pyrolysis.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 CS, 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 CS can be converted into methane by a methanation reaction. The methanation reaction is described by chemical reaction schemes (1) and (2):CO + 3H2^ CH4+ H2O (1)CO2+ 4H2CH4+ 2H2O (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(abs.) and 200 to 700 °C, preferably 5 to 60 bar (abs.), more preferably 10 to 45 bar (abs.) and preferably 200 to 550 °C, more preferably 10 to 45 bar (abs.).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 (abs.) 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.240909W00214In 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, for example 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 preferably at a pressure of about 2.5 MPa (abs.) (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 (abs.) (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 Industrial240909W00215Chemistry (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; 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; oriv) 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; orvi) 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; orvii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; orviii) 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 wt.-% or more, preferably 2 wt.-% or more, more preferably 5 wt.-% or more, more preferably 15 wt.-% or more, more preferably 30 wt.-% or more, more preferably 40 wt.-% or more, more preferably 60 wt.-% or more, more preferably 80 wt.-% or more, more preferably 90 wt.-% or more, more preferably 95 wt.-% or more; and / or wherein the content of the clean gas stream CS in the product PRF1 is 100 wt.-% or less, preferably 95 wt.-% or less, more preferably 90 wt.-% or less, more preferably 50 wt.-% or less, more preferably 25 wt.-% or less, more preferably 10 wt.-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1, which is incorporated herein by reference in its entirety. Preferably, the240909W00216product 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 preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and / or steam cracking; and / or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing. In addition, the one or more step(s) are described in detail in Reference RF1; paragraphs

[1000] to

[8005] ,The term “building block”, as used herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0 °C and 0.1 MPa (abs.). 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 in240909W00217more detail in paragraphs

[2001] to

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

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

[2009] and

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

[2011] of Reference RF1.The term “industrial use polymer'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 other240909W00218precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer'’ and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1. The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, 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-Cie carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-Ci8, 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,240909W00219ketone, 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 composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term “aqueous polymer dispersion”, as used herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled “aqueous polymer dispersion” of Reference RF1. The dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion 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.240909W00220UV-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 “further240909W00221cosmetic ingredient”, as used herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term “composition and / or formulation thereof’ with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

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

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

[8000] to

[8005] of Reference RF1.The 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 reducing wastewater during gasification of locally sourced biomass, said process comprising the steps(i) providing a first gasifier G1, wherein said first gasifier G1 is in a first location L1, and wherein said first gasifier G1 has an optimized operational window for converting at least one first feedstock F1 into synthesis gas SG1 by gasification in said first gasifier G1, wherein said optimized operational window is defined as 80 to 100 % capacity for the at least one first feedstock F1 in said first gasifier G1 and wherein 80 % is the lower boundary and 100 % is the maximum capacity for the at least one first feedstock F1 or the sum of all feedstocks F1 in said first gasifier G1 ,(ii) sourcing at least one first feedstock F1 from at least a second location L2, wherein the first location L1 and the at least one second location L2 are co-located within an area AR of no more than 40,000 km2, (iii) transporting said at least one first feedstock F1 from the at least one second location L2 to the first location L1 or to a third location L3, said third location L3 also co-located within said area AR, (iv) optionally pretreating said at least one first feedstock F1 in at least one pretreatment unit PU, wherein said at least one pretreatment unit is in at least one of the locations selected from the group consisting240909W00222of L1 , L2 and L3, and whereby at least one pretreated first feedstock PF1 is formed in said at least one pretreatment unit PU,(v) determining in all locations selected from the group consisting of L1 , L2 and L3 the amount of the at least one first feedstock F1 and / or the amount of the at least one optionally pretreated first feedstock PF1 available during a timeframe t, preferably available during a timeframe t at location L1 only, (vi) comparing the amount of at least one first feedstock F1 and / or the amount of at least one optionally pretreated at least one first feedstock PF1 available during said timeframe t determined in step (v) with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t,(vii) providing at least one second feedstock F2 in case the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is less than 50 % of the maximum capacity for the at least one first feedstock F1 of said first gasifier G1 during said timeframe t,(viii) converting said at least one first feedstock F1 and / or the optionally pretreated at least one first feedstock PF1 and the at least one second feedstock F2 provided in step (vii) in the first gasifier G1 into synthesis gas SG1, whereby wastewater WW is formed.2. Process according to embodiment 1 wherein the first gasifier G1 is selected from the group consisting of fluidized bed gasifiers, fixed bed gasifiers and entrained flow gasifiers.3. Process according to embodiment 1 or 2 wherein the first feedstock F1 is selected from the group comprising or preferably consisting of stalks, peels, stems, leaves, husks, shells, cobs, ears, stovers, nuts, empty fruit bunches, empty nut bunches and combinations thereof.4. Process according to any one of embodiments 1 to 3 wherein 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, 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.5. Process according to any one of embodiments 1 to 4 wherein the at least one first feedstock F1 is sourced from at least a second location L2 in step (ii) by a method selected from the group comprising or preferably consisting of harvesting, separating from mills, separating from presses, separating from means for shredding, separating from dryers, and separating from pelletizers.240909W002236. Process according to any one of embodiments 1 to 5 wherein the at least one first feedstock F1 is transported from the at least one second location L2 to the first location L1 or to a third location L3 by a method selected from the group comprising or preferably consisting of transportation by truck, transportation by trailer, transportation by compact three-wheeled vehicles, transportation by train, transportation by drones, transportation by ship transportation by boat and combinations thereof.7. Process according to any one of embodiments 1 to 6 wherein the at least one first feedstock F1 is optionally pretreated by a method selected from the group comprising or preferably consisting of preferably in this order, (a1) shredding, (b1) drying and optionally (d) milling.8. Process according to any one of embodiments 1 to 7 wherein the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 in at least one location selected from the group consisting of L1, L2 and L3 during said timeframe t is determined in step (v) by a method selected from the group comprising or preferably consisting of weighting, determining the volume, assessing weather forecast data, receiving forecast data for availability of the at least one first feedstock F1 by local feedstock providers and / or traders, and combinations thereof.9. Process according to embodiment 8 wherein the volume of the at least one first feedstock F1 is determined with level-sensors such as radar sensors, ultrasonic sensors, capacitive sensors and plumb bob sensors and / or rotating paddle detectors, vibrating level switches, membrane switches and combinations thereof.10. Process according to any one of embodiments 1 to 9 wherein the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is compared with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t by a method selected from the group comprising or preferably consisting of stock management, stock accounting, matching the existing amount of first feedstock F1 and the required amount of first feedstock F1 for said timeframe t at the location of said first gasifier G1.11. Process according to any one of embodiments 1 to 10 wherein the timeframe t is preferably 3 to 15 days, more preferably 4 to 12 days and most preferably 5 to 10 days.12. Process according to any one of embodiments 1 to 11 wherein the at least one second feedstock F2 is selected from the group comprising or preferably consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils,240909W00224extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), coal, tar oils, natural gas, CO2, waste streams from tire production, pre-sorted automotive shredder residue (ASR), and mixtures thereof, wherein said biomass is different than the first feedstock F1 and / or the pretreated first feedstock PF1 provided by steps (ii) to (iv).13. Process according to any one of embodiments 1 to 12 wherein the synthesis gas SG1 formed in the first gasifier G1 in step (viii) comprises CO, H2, CO2and wastewater WW.14. Process according to any one of embodiments 1 to 13 wherein wastewater WW is separated from synthesis gas SGI by condensation.15. Process according to any one of embodiments 1 to 14 wherein the synthesis gas SG1 is converted in a gasifier G2 into a synthesis gas SG2, said second gasifier G2 being downstream of and fluidically connected to said first gasifier G1.16. Process according to embodiment 15 wherein the gasifier G2 is an entrained flow gasifier.17. Process according to embodiment 15 or 16 wherein the synthesis gas SG2 formed in gasifier G2 comprises CO, H2, CO2 and wastewater WW.18. Process according to any one of embodiments 15 to 17 wherein wastewater WW is separated from synthesis gas SG2 by condensation.19. Process according to any one of embodiments 1 to 18 wherein synthesis gas stream SG1 and / or synthesis gas SG2 is / are 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, CO2removal, sulfur removal, HCI removal, Hg removal, HCN / NH3 removal and combinations thereof.20. Process according to embodiment 19 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.21. Process according to embodiment 20, comprising the step:converting the gas stream CS manufactured by the process according to embodiment 1 to 20 or a chemical material manufactured by the process according to any one of embodiments 1 to 20 to obtain a product PRF1.240909W0022522. Process according to embodiment 21, 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; oriv) 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; orviii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.23. Process according to embodiment 21 or 22, wherein 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 invention will be further explained by the following non-limiting examples.ExamplesGeneral descriptionAll simulations were performed with the Aspen Plus simulation package, version 14. A gasifier set up comprising a first gasifier G1 and a second gasifier G2 wherein said second gasifier G2 was downstream of and fluidically connected to said first gasifier G and wherein said second gasifier G2 was an entrained flow gasifier was used throughout all examples.240909W00226Feedstocks used for the following examples and comparative examples (HV represents the higher heating value in MJ / kg, all other numbers are given in wt.-%, mixture data are also given as wt.-%):* MSW = municipal solid wasteExample 1A first feedstock F1 (rice straw, having the composition and properties given in table 1) was converted in a in a first gasifier G1 (fluidized bed gasifier) whereby a stream of synthesis gas SG1 is formed. Said stream of synthesis gas SG1 was then converted in a second gasifier G2 (entrained flow gasifier) into a synthesis gas stream SG2. The second gasifier G2 is downstream of and fluidically connected to the first gasifier G1. The amount of first feedstock F1 fed into the first gasifier G1 was 40 t / h which is within the optimized operational window of the first gasifier G1 used in the simulation (= 100 % capacity for feedstock F1). The first feedstock F1 was fed at 35 °C and 4 bar (abs.) into the first gasifier G1. Steam (5 bar (abs.), 200 °C) with 20 t / h and pure oxygen (6 bar (abs.), 25 °C) with 6.1 t / h were also fed into the first gasifier G1 to reach a temperature of synthesis gas stream SG1 of 750 °C at the outlet of the first gasifier G1. Next, the synthesis gas stream SG1 was fed into the second gasifier G2 via a burner nozzle. Additionally, pure oxygen (6 bar (abs.), 25 °C) was fed with 13.3 t / h into the second gasifier G2 to reach a temperature of 1350 °C of the resulting synthesis gas stream SG2 at the outlet of the second gasifier G2. The synthesis gas stream SG2 comprised 17.5 t / h CO, 1.25 t / h H2 and 23.5 t / h CO2. The molar ratio of H2 : CO of synthesis gas stream SG2 was 0.99. 28.9 t / h wastewater WW were separated from the synthesis gas stream SG2 after cooling the synthesis gas stream SG2 to 70 °C. The mass flow ratio “wastewater WW : CO + H2" in synthesis240909W00227gas stream SG2 was 1.5, which is acceptable. The mass flow ratio “CO2 : (CO + H2) in synthesis gas stream SG2 was 1.3, which is acceptable.Comparative Example 1A first feedstock F1 (rice straw, having the composition and properties given in table 1) was converted in a fluidized bed gasifier and entrained flow gasifier combination (the second gasifier G2 is downstream of and fluidically connected to the first gasifier G1) with a feed rate of 20 t / h at 4 bar (abs.), 25 °C was fed into the first gasifier G1. This feed rate for feedstock F1 is only about 50 % of the 100 % capacity of gasifier G1 for the first feedstock F1 required to operate inside the optimized operational window of the first gasifier G1. Additional to the first feedstock F1, 20 t / h steam (5 bar (abs.), 200 °C) and 4.4 t / h pure oxygen (6 bar (abs.), 25 °C) were added to reach a first gasifier G1 outlet temperature of the synthesis gas stream SG1 of 750 °C. Furthermore, steam with a feed rate of 20 t / h must be added to maintain the fluidized bed inside the first gasifier G1. The synthesis gas stream SG1 then enters the entrained flow gasifier (G1) via a burner nozzle. Additionally, pure oxygen is added (6 bar (abs.), 25 °C) with 7.1 t / h to convert the synthesis gas stream SG1 into a synthesis gas stream SG2 with 1350 °C at the gasifier G2 outlet. The synthesis gas stream SG2 comprised 6.3 t / h CO, 0.6 t / h H2 and 15.6 t / h CO2. The molar ratio of H2 : CO is 1.27. Wastewater WW in an amount of 24.9 t / h is separated after cooling the to 70 °C from the synthesis gas stream SG2. The mass flow ratio “wastewater WW : CO + H2" in synthesis gas stream SG2 was 3.6, which is not acceptable. The mass flow ratio “CO2: (CO + H2) in synthesis gas stream SG2 was 2.3, which is not acceptable.Comparative Example 2A first feedstock F1 (rice straw, having the composition and properties given in table 1) was converted in a fluidized bed gasifier and entrained flow gasifier combination (the second gasifier G2 is downstream of and fluidically connected to the first gasifier G1). The first feedstock F1 was fed with a feed rate of 10 t / h at 4 bar (abs.) and 35 °C into the first gasifier G1. Said feed rate is only about 25 % of the amount of first feedstock F1 required to operate inside the optimized operational window of the first gasifier G1. Additional to the first feedstock F1, 20 t / h steam (5 bar (abs.), 200 °C) and 3.5 t / h pure oxygen (6 bar (abs.), 25 °C) were added to reach a first gasifier G1 outlet temperature of the synthesis gas stream SG1 of 750 °C. Furthermore, steam with a feed rate of 20 t / h must be added to maintain the fluidized bed inside the first gasifier G1. The synthesis gas stream SG1 then enters an entrained flow gasifier G2 via a burner nozzle. Additionally, pure 4.1 t / h oxygen is added (6 bar (abs.), 25 °C) to convert the synthesis gas stream SG1 into a synthesis gas stream SG2 having a temperature of 1350 °C at the gasifier G2 outlet. The synthesis gas stream SG2 comprises 1.4 t / h CO, 0.2 t / h H2and 10.5 t / h CO2. The molar ratio H2 : CO is 1.77. Wastewater WW in an amount of 23.4 t / h is separated after cooling the synthesis gas stream SG2 to 70 °C therefrom. The mass flow ratio “wastewater WW : CO + H2'' in synthesis gas stream SG2 was 14.6, which is not acceptable. The mass flow ratio “CO2 : (CO + H2) in synthesis gas stream SG2 was 5.8, which is not acceptable.Example 2A mixture of first feedstock F1 and second feedstock F2 is fed with a feed rate of 40 t / h at 4 bar (abs.) and 35 °C into a fluidized bed gasifier and entrained flow gasifier combination (the second gasifier G2 is downstream of and240909W00228fluidically connected to the first gasifier G1). The mixed feedstock comprised a first feedstock F1 (rice straw, having the composition and properties given in table 1) and a second feedstock F2 (pretreated municipal solid waste (MSW), having the composition and properties given in table 1) in a mass ratio of 50:50, which have together as a mixed feedstock the mass composition provided in table 1. Additional to the mixture of first feedstock F1 and second feedstock F2, 20 t / h steam (5 bar (abs.), 200 °C) and 7 t / h pure oxygen (6 bar (abs.), 25 °C) were added to reach a first gasifier G1 outlet temperature of the synthesis gas stream SG1 of 750 °C. After the fluidized bed gasifier G1, the synthesis gas stream SG1 enters an entrained flow gasifier G2 via a burner nozzle. Additionally, 16 t / h pure oxygen is added (6 bar (abs.), 25 °C) to convert the synthesis gas stream SG1 into synthesis gas stream SG2 with 1350 °C at the gasifier G2 outlet. The synthesis gas stream SG2 comprised 22.6 t / h CO, 1.7 t / h H2 and 21.5 t / h CO2. The molar ratio H2 : CO is 1.06. Wastewater WW in an amount of 28.4 t / h is separated after cooling the synthesis gas stream SG2 to 70 °C therefrom. The mass flow ratio “wastewater W : CO + H2" in synthesis gas stream SG2 was 1.2, which is acceptable. The mass flow ratio “CO2 : (CO + H2) in synthesis gas stream SG2 was 0.9, which is acceptable.Example 333.8 t / h (4 bar (abs.), 35 °C) of a mixed feedstock consisting of a first feedstock F1 and a second feedstock F2 was converted in a fluidized bed gasifier G1 and an entrained flow gasifier G2 combination (the second gasifier G2 is downstream of and fluidically connected to the first gasifier G1) within the optimized operation window for the given fluidized bed gasifier G1. The mixed feedstock consisted of 20 t / h of rice straw (first feedstock F1) and 13.8 t / h of pretreated MSW (first feedstock F2), having a mass ratio: 59:41 ; further details for the mixed feedstock are provided in table 1). Additional to the mixed feedstock, 20 t / h steam (5 bar (abs.), 200 °C) and 6.2 t / h pure oxygen (6 bar (abs.), 25 °C) were fed into the first gasifier G1 to reach a gasifier G1 outlet temperature of the synthesis gas stream SG1 of 750 °C. After the fluidized bed gasifier G1 , the synthesis gas stream SG1 was fed into an entrained flow gasifier via a burner nozzle. Additionally, 13.2 t / h pure oxygen is added (6 bar (abs.), 25 °C) to convert the synthesis gas stream SG1 into a synthesis gas stream SG2 with 1350 °C at the gasifier G2 outlet. The synthesis gas stream SG2 comprised 17.5 t / h CO, 1.4 t / h H2and 19.9 t / h CO2. The molar ratio H2: CO is 1.10. Wastewater WW in an amount of 27.2 t / h was separated after cooling to 70 °C therefrom. The mass flow ratio “wastewater WW : CO + H2“ in synthesis gas stream SG2 was 1.4, which is acceptable. The mass flow ratio “CO2 : (CO + H2) in synthesis gas stream SG2 was 1.1, which is acceptable.

Claims

240909W00229Claims1. Process for reducing wastewater during gasification of locally sourced biomass, said process comprising the steps(i) providing a first gasifier G1, wherein said first gasifier G1 is in a first location L1, and wherein said first gasifier G1 has an optimized operational window for converting at least one first feedstock F1 into synthesis gas SG1 by gasification in said first gasifier G1, wherein said optimized operational window is defined as 80 to 100 % capacity for the at least one first feedstock F1 in said first gasifier G1 and wherein 80 % is the lower boundary and 100 % is the maximum capacity for the at least one first feedstock F1 or the sum of all feedstocks F1 in said first gasifier G1 ,(ii) sourcing at least one first feedstock F1 from at least a second location L2, wherein the first location L1 and the at least one second location L2 are co-located within an area AR of no more than 40,000 km2, (iii) transporting said at least one first feedstock F1 from the at least one second location L2 to the first location L1 or to a third location L3, said third location L3 also co-located within said area AR, (iv) optionally pretreating said at least one first feedstock F1 in at least one pretreatment unit PU, wherein said at least one pretreatment unit is in at least one of the locations selected from the group consisting of L1 , L2 and L3, and whereby at least one pretreated first feedstock PF1 is formed in said at least one pretreatment unit PU,(v) determining in all locations selected from the group consisting of L1 , L2 and L3 the amount of the at least one first feedstock F1 and / or the amount of the at least one optionally pretreated first feedstock PF1 available during a timeframe t, preferably during a timeframe t at location L1 only, (vi) comparing the amount of at least one first feedstock F1 and / or the amount of at least one optionally pretreated at least one first feedstock PF1 available during said timeframe t determined in step (v) with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t,(vii) providing at least one second feedstock F2 in case the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is less than 50 % of the maximum capacity for the at least one first feedstock F1 of said first gasifier G1 during said timeframe t,(viii) converting said at least one first feedstock F1 and / or the optionally pretreated at least one first feedstock PF1 and the at least one second feedstock F2 provided in step (vii) in the first gasifier G1 into synthesis gas SG1, whereby wastewater WW is formed.

2. Process according to claim 1 wherein the first gasifier G1 is selected from the group consisting of fluidized bed gasifiers, fixed bed gasifiers and entrained flow gasifiers.240909W002303. Process according to claim 1 or 2 wherein the first feedstock F1 is selected from the group comprising or preferably consisting of stalks, peels, stems, leaves, husks, shells, cobs, ears, stovers, nuts, empty fruit bunches, empty nut bunches and combinations thereof.

4. Process according to any one of claims 1 to 3 wherein 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, 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.

5. Process according to any one of claims 1 to 4 wherein the at least one first feedstock F1 is sourced from at least a second location L2 by a method selected from the group comprising or preferably consisting of harvesting, separating from mills, separating from presses, separating from means for shredding, separating from dryers, separating from pelletizers and combinations thereof.

6. Process according to any one of claims 1 to 5 wherein the at least one first feedstock F1 is transported from the at least one second location L2 to the first location L1 or to a third location L3 by a method selected from the group comprising or preferably consisting of transportation by truck, transportation by trailer, transportation by compact three-wheeled vehicles, transportation by train, transportation by drones, transportation by ship, transportation by boat and combinations thereof.

7. Process according to any one of claims 1 to 6 wherein the at least one first feedstock F1 is optionally pretreated by a method selected from the group comprising or preferably consisting of, preferably in this order, (a1) shredding, (b1) drying and optionally (d) milling.

8. Process according to any one of claims 1 to 7 wherein the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 in at least one location selected from the group consisting of L1, L2 and L3 is determined in step (v) by a method selected from the group comprising or preferably consisting of weighting, determining the volume, assessing weather forecast data, receiving forecast data for availability of the at least one first feedstock F1 by local feedstock providers and / or traders, and combinations thereof.

9. Process according to claim 8 wherein the volume of the at least one first feedstock F1 is determined with level-sensors such as radar sensors, ultrasonic sensors, capacitive sensors and plumb bob sensors and / or rotating paddle detectors, vibrating level switches, membrane switches and combinations thereof.240909W0023110. Process according to any one of claims 1 to 9 wherein the amount of available at least one first feedstock F1 and / or the amount of optionally pretreated at least one first feedstock PF1 determined in step (v) is compared with the amount of the at least one first feedstock F1 and / or the amount of the optionally pretreated at least one first feedstock PF1 required for feeding said at least one first feedstock F1 and / or said optionally pretreated at least one first feedstock PF1 within the optimized operational window of said first gasifier G1 during said timeframe t by a method selected from the group comprising or preferably consisting of stock management, stock accounting, matching the existing amount of first feedstock F1 and the required amount of first feedstock F1 for said timeframe t at the location of said first gasifier G1.

11. Process according to any one of claims 1 to 10 wherein the timeframe t is preferably 3 to 15 days, more preferably 4 to 12 days and most preferably 5 to 10 days.

12. Process according to any one of claims 1 to 11 wherein the at least one second feedstock F2 is selected from the group comprising or preferably consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end-of-life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, municipal solid waste (MSW), coal, tar oils, natural gas, CO2, waste streams from tire production, pre-sorted automotive shredder residue (ASR), and mixtures thereof, wherein said biomass is different than the first feedstock F1 and / or the pretreated first feedstock PF1 provided by steps (ii) to (iv).

13. Process according to any one of claims 1 to 12 wherein the synthesis gas SG1 is converted in a gasifier G2 into a synthesis gas SG2.

14. Process according to any one of claims 1 to 13 wherein synthesis gas stream SG1 and / or synthesis gas SG2 is / are 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.

15. Process according to claim 14 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.

16. Process according to claim 15, comprising the step:converting the gas stream CS manufactured by the process according to claims 1 to 15 or a chemical material manufactured by the process according to any one of claims 1 to 15 to obtain a product PRF1.240909W0023217. Process according to claim 16, 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; oriv) 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; orviii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.

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