Process for producing synthesis gas
Patent Information
- Authority / Receiving Office
- EP · EP
- Patent Type
- Applications
- Current Assignee / Owner
- ROSNEFT DEUTSCHLAND GMBH
- Filing Date
- 2024-05-08
- Publication Date
- 2026-06-17
Smart Images
Figure EP2024062843_13022025_PF_FP_ABST
Abstract
Description
[0001] Process for producing synthesis gas
[0002] The invention relates to a process for producing synthesis gas. In particular, the invention relates to a process for producing synthesis gas from a carbonaceous processing material.
[0003] Synthesis gas is a gas with variable proportions of various gaseous substances that can be used for chemical synthesis. Synthesis gas, also known as syngas, is a hydrogen-containing combustible gas that can be used for chemical syntheses, e.g., for the synthesis and thus for the production of methanol or for use in the Fischer-Tropsch process. Synthesis gas can also serve as a gaseous fuel.
[0004] Synthesis gas can be produced in a variety of ways. One method for producing synthesis gas is the gasification of natural or synthetic coal with the addition of steam and oxygen. In the terminology of the present invention, the term "coal" preferably refers to synthetic coal produced synthetically from a carbon-containing feedstock through a carbonization process. This coal can then be converted, for example, using oxygen, into a synthesis gas mixture of CO and hydrogen by partial oxidation and gasification with steam.
[0005] Synthesis gas can also be produced from natural gas or oil using steam reforming. This process involves converting hydrocarbons into carbon monoxide and hydrogen using steam under pressure and relatively high temperatures.
[0006] EP 4 121 496 A1 further describes the use of biomass for producing synthesis gas by biomass gasification. Since the biomass has a less uniform composition and, depending on the biomass composition used to produce the synthesis gas, may also contain undesirable substances such as sulfur (compounds), the synthesis gas thus produced is fermented to ethanol using predetermined microorganisms which are less sensitive to these undesirable substances than, for example, catalysts. Since this process uses biomass that is actually intended for disposal, the process is advantageous for climate and environmental protection reasons compared to the aforementioned processes for producing synthesis gas, especially since coal, natural gas, and petroleum reserves are finite. However, the process is complex and time-consuming.However, there is still a need for a process for producing syngas that is climate- and environmentally friendly, yet at the same time more time- and cost-efficient. Using carbon-containing upgrading materials of non-fossil origin results in a positive CO2 balance, particularly because, on the one hand, the syngas can be used to produce fuels that are then burned, and, on the other hand, the carbon-containing upgrading materials are not burned, which generates CO2, unlike previously.
[0007] Furthermore, DE10 2009 055 976 A1 describes a device and a method for producing a carbon monoxide- and hydrogen-rich, tar-free, and low-methane synthesis gas from biomass by entrained-flow gasification. In this process, coal is produced from biomass, which serves as fuel for the production of the synthesis gas. Wood, wood waste, green waste, grass, agricultural products, and biowaste, including straw, as well as residues from biomass processing, can serve as biomass. The coal is either gasified with a combustible liquid or ground and then gasified.
[0008] It is an object of the present invention to provide a process for producing synthesis gas which is climate and environmentally friendly and proves to be comparatively time- and cost-effective.
[0009] The invention relates to a process for producing synthesis gas from a carbonaceous processing material, comprising the following steps: a) subjecting the carbonaceous processing material to hydrothermal carbonization at a first temperature in a range of 100 to 400°C and a pressure of 20 to 50 atm (2.027 x 10 6 Pa up to 5.066 x 10 6 Pa) to produce coal, b) gasifying the coal produced in step a) at a second temperature in the range of 800 to 1,500°C using an electric heater to generate the second temperature and using CO2 as gasification agent to produce the synthesis gas.
[0010] By means of the process according to the invention, carbonaceous processing materials can be utilized cost- and time-efficiently, so that they do not have to be incinerated or otherwise disposed of, thereby increasing Ct emissions into the atmosphere. During hydrothermal carbonization, the carbonaceous processing material is carbonized into coal at the first temperature and the above-mentioned pressure, producing nutrient-rich process water as an additional product that can also be used for further purposes. The electric heating is provided to supply energy to a reactor in which step b) is carried out. The heating of the reactor in step b) can be achieved, for example, by resistance heating or inductive heating.
[0011] In a preferred embodiment, the process further comprises the following steps: c) optionally subjecting a further carbonaceous treatment material, which is different from the carbonaceous treatment material, to hydrothermal carbonization at a third temperature in a range of 100 to 400°C and a pressure of 20 to 50 atm (2.027 x 10 6 Pa up to 5.066 x 10 6Pa) separately from the carbonaceous processing material to produce further coal, d) gasifying the further coal or the further carbonaceous processing material produced in step c) at a fourth temperature in the range of 700 to 1,500°C using an electric heater to generate the second temperature and using CO2 as a further gasification agent separately from step b) to produce further synthesis gas, and e) combining the synthesis gas obtained in step b) and the further synthesis gas obtained in step d) to obtain the synthesis gas.
[0012] Using the process according to the invention, the carbonaceous processing materials and the further carbonaceous processing material can be recycled separately, cost-effectively and time-efficiently, so that they do not have to be incinerated or otherwise disposed of, thereby increasing CO2 emissions into the atmosphere. During hydrothermal carbonization according to steps a) and c), the various carbonaceous processing materials are carbonized into coal and further coal, producing nutrient-rich process water as additional products that can be separately recycled. The resulting process water can contain different nutrients and / or pollutants in varying concentrations.During gasification according to steps b) and d), the coal and the additional coal or the carbonaceous processing material are each gasified separately, producing ash and the additional synthesis gas as well as further ash, which can be separately recycled. The ashes produced during gasification may contain various nutrients and / or pollutants in varying concentrations.The invention is based in particular on the fundamental idea that, depending on the type of carbonaceous processing material used, synthesis gas is produced by means of the process according to the invention which has a quality and properties that are independent of the type of carbonaceous processing material. However, the further products produced in the process according to the invention in the form of process water and ash can have qualities and properties that depend on the type of carbonaceous processing material and can therefore be used separately for further purposes. Steps b) and d) can be carried out at different times or in parallel. While the carbonaceous processing material and the further carbonaceous processing material are different from one another, the gasification agent and the further gasification agent can be the same or different.The carbonaceous processing material and the further carbonaceous processing material are distinguished by at least one type (i.e., type of processing material) that is collected separately for processing. Examples of different processing materials include sewage sludge, biomass, paper waste, or plastic waste.
[0013] The process is suitable for dry and moist processing materials, and water can also be added in step a) and / or step c) if necessary. It is therefore not necessary to dry the carbonaceous processing material before step a) or the further carbonaceous processing material before step c). Rather, it can be used as it arises. The coal obtained after step a) and the further coal obtained after step c) contains little water after the subsequent dewatering and is suitable for direct use in steps b) and d). For example, the coal obtained in step a) and / or the further coal obtained in step c) is dewatered between steps a) and b) or c) and d), e.g. in a filter press, to a predetermined dry matter content, e.g. 65 to 70 wt.%, and optionally further dried, e.g. using heat.By converting the carbonaceous processing material into coal, a reactant is used in step b) which has a higher energy density than the carbonaceous processing material and can be transported to a plant for synthesis gas production with less effort than the latter.
[0014] For the purposes of the present invention, the term "recycling material" refers to recyclable waste material intended for recycling. The term "recycling" refers to the exploitation, development, or utilization of the material for further use or application, so that the material is reused or made usable again.
[0015] In a preferred embodiment, the first temperature and / or the third temperature is in the range of 150 to 350°C, more preferably 200 to 300°C. These temperatures are sufficient to carry out step a).
[0016] The second temperature is preferably in the range of 900 to 1,400°C, more preferably 1,000 to 1,300°C. In this temperature range, step b) is carried out particularly efficiently.
[0017] In a preferred embodiment, the gasification agent and / or the further gasification agent comprises essentially 100 vol.% CO2, i.e. it or it consists essentially of CO2. The gasification agent which has an oxidizing effect on the coal obtained in step a) is therefore essentially CO2. The same applies to the further gasification agent. This is the most preferred case, although CO2 often contains impurities such as H2O and / or O2 for technical reasons. Therefore, the gasification agent and / or the further gasification agent can have a proportion of CO2 and a proportion of H2O and / or O2 that is smaller than the proportion of CO2. The CO2 can therefore contain small amounts of H2O or O2, which represent technical impurities that are undesirable in the process according to the invention but not always avoidable. The gasification agent and / or the further gasification agent can therefore also, for technical reasons, be a mixture of 70 to 99 vol.-% CO2 and 1 to 30 vol.% H2O and / or O2 or alternatively a mixture of 80 to 98 vol.% CO2 and 2 to 20 vol.% H2O and / or O2. In step b), the CO2 is reacted with the coal to form CO. Therefore, the carbon in the CO contained in the synthesis gas also results from the CO2, i.e., the gasification agent. Furthermore, the coal reacts with H2O to form CO and H2. Similarly, in step d), the CO2 is reacted with the additional coal to form CO, and the additional coal reacts with H2O to form CO and H2. The H2O is preferably used in the form of steam in step b) and in step d). In a preferred embodiment, a carbon source is added as an additive to the carbonaceous processing material and / or the additional carbonaceous processing agent in step a). For the purposes of the invention, the term “carbon source” is understood to mean a substance which has a carbon content of more than 80% by weight, more preferably 85% by weight, even more preferably 90% by weight.-%. This allows the carbon-containing processing material used in step a) or the additional carbon-containing processing material used in the optional step c) to be enriched with carbon.
[0018] The carbonaceous processing material can be used in step a) in crushed or uncrushed form. The same applies to the further carbonaceous processing material in steps c) and d). The carbonaceous processing material and / or the further carbonaceous processing material preferably comprises a compostable mass. The compostable mass preferably contains agricultural, food, animal, slaughterhouse, commercial, municipal and / or industrial waste. Agricultural, food, animal and / or slaughterhouse waste includes any usable plant and / or animal part, i.e., not only fiber, but also liquid components, tendons, bones, fish bones, and crust parts of plants or animals, including fish. Commercial, municipal and / or industrial waste can, for example,Cardboard, paper, manure, municipal waste, paper mill residues such as paper mill sludge, used paper mill liquids, and / or compostable plastics. The carbonaceous upstream material and the further carbonaceous upstream material are different from each other, so that even if they both have compostable mass, they differ in at least one type (i.e., type of upstream material) that is collected separately for processing. For example, agricultural, food, and grocery waste are collected together for processing, while the compostable plastics waste and paper waste are collected separately for processing. In a preferred embodiment, the carbonaceous upstream material or the further carbonaceous upstream material comprises biomass.Biomass represents all of the organic substance produced or accumulating by plants or animals, so that the term “biomass” is understood to mean the mass of material of living organisms and / or their body or plant parts. Biomass is preferably biomass from dead and / or severed plant parts such as leaves, side shoots, twigs and branches, foliage, pollen, spermatozoids, non-germinated plant spores and / or seeds, fruits, flowers, roots or parts thereof, litter, whole dead plants and / or dead wood, and / or biomass from dead and / or severed body parts such as hair, fur, feathers, scales, bones, hooves, horns, bristles, fish bones, tendons, cartilage, skin, innards, exuviae, pupal cases, cocoon remains, eggs, eggshells, carcasses or parts thereof, animal excrement such as droppings. Furthermore, the usable biomass includes kitchen, food and other food waste.
[0019] For example, in the case of a plant-based processing material, the carbonaceous processing material or the further carbonaceous processing material may contain some or all of the plant parts of a plant. For example, if the carbonaceous processing material or the further carbonaceous processing material contains sugar beet, it may contain the beet body, beet pulp, roots, leaves, seeds, flowers, and / or parts thereof, e.g., also leached beet pulp, syrup, and / or molasses.
[0020] In the case of an animal processing material, the carbonaceous processing material or the further carbonaceous processing material may, for example, comprise some or all of the body parts of an animal. If the carbonaceous processing material contains, for example, cow waste, it may contain cartilage, tendons, udders, horns, meat, fatty tissue, hooves, eyes, marrow and / or parts thereof. The carbonaceous processing material and / or the further carbonaceous processing material preferably comprises at least one component selected from the group consisting of sewage sludge, wood, agricultural waste, green waste, grass and tree cuttings, plants, straw, silage, food waste, animal and slaughterhouse waste, paper sludge and / or pomace and / or plastic waste, but they are selected such that they are different from one another. These wastes have a carbon content that is advantageous for the process.Agricultural waste primarily includes agricultural waste such as plant residues from agriculture, which originate primarily from arable farming and horticulture and include all parts of crops. Food waste includes kitchen, dining, and raw and / or cooked food waste of plant and / or animal origin. Animal and slaughterhouse waste includes kitchen, dining, and other animal food waste, as well as all parts of animals, including marine animals such as fish.
[0021] The carbonaceous treatment material preferably comprises sewage sludge. The sewage sludge is preferably dewatered and / or dried. Advantages of dewatered and / or dried sewage sludge include a reduction in sewage sludge quantity and weight, and improved pumpability and dosing.
[0022] In a preferred embodiment, the process comprises steps a), b), d), and optionally c), and the carbon-containing treatment material comprises or consists of sewage sludge, while the additional carbon-containing treatment material is sewage sludge-free. The ash obtained after step b) has a very low pollutant content and can be used, for example, as fertilizer without further processing because it contains a relatively high amount of phosphorus. The additional ash can then be used separately for further purposes.
[0023] In a preferred embodiment, the process comprises steps a), b), and d), the carbon-containing processing material is free of plastic waste, and the further carbon-containing processing material contains or consists of plastic waste. Preferably, the fourth temperature is in the range of 700 to 1,000°C, more preferably 700 to 900°C. Step d) is carried out spatially separate from step b). Steps b) and d) are carried out independently of one another in different reactors, so that they are spatially separated.
[0024] By spatially and materially separating the carbonaceous processing material and the further processing material containing plastic waste, the ash and the further ash, which are obtained in addition to the synthesis gas and the further synthesis gas in steps b) and d) and which contain different components, are more specifically prepared for further use. Furthermore, the gasification of the plastic waste takes place without prior hydrothermal carbonization and at a lower temperature, thereby saving costs and energy. Furthermore, the composition of the synthesis gas can be further controlled depending on the desired carbon monoxide and hydrogen contents by controlling a mixing ratio of the synthesis gas obtained in step b) and the further synthesis gas obtained in step d).
[0025] The ashes produced in steps b) and d) may contain various ingredients such as nutrients and / or pollutants in varying concentrations. Steps b) and d) are based on the basic idea that, depending on the type of carbonaceous processing material used and the further processing material containing plastic waste, the process produces synthesis gas with a quality and properties that are independent of the type of carbonaceous processing material and the carbonaceous processing material. However, the additional products produced in steps b) and d) in the form of ash and further ash may have qualities and properties that depend on the type of carbonaceous processing material and the further carbonaceous processing material and should therefore be capable of being used separately for further purposes.
[0026] Preferably, each of steps a), b), c) and d) of the process is carried out in a reactor assigned to it. Preferably, step a) is carried out in a first reactor, step b) is carried out in a second reactor, the optional step d) is carried out in an optional third reactor and the optional step c) is carried out in an optional fourth reactor. Steps a) and b) are preferably carried out in one plant train containing the first reactor and the second reactor. Steps c) and d), if present, are carried out in a further plant train containing the third reactor and optionally the fourth reactor, the two plant trains being combined to combine the resulting synthesis gases in order to obtain the synthesis gas, which can then be stored and / or further processed.However, the ashes produced in the two plant lines are preferably not combined, but rather removed and stored separately or used for further purposes.
[0027] Preferably, the carbonaceous processing material used in step a) is used as a mixture of two different carbonaceous processing materials with different carbon contents, water contents, and / or dry matter contents. This allows the carbon content, water content, and / or dry matter content of the processing material used in step a) to be adjusted. Furthermore, this allows the composition of the synthesis gas obtained in step b) to be controlled with regard to a molar ratio of CO and H2. For example, to utilize and use a carbonaceous processing material with a relatively low carbon content in step a), a carbonaceous processing material with a relatively high carbon content can be added as an additional carbon source. The carbonaceous processing material preferably comprises a mixture of sewage sludge and wood.The wood acts as a good catalyst for the carbonization process carried out in step s). The additional carbonaceous processing material can also be used in step c) or d) as a mixture of two different carbonaceous processing materials with different carbon contents, water contents, and / or dry matter contents. However, the carbonaceous processing material and the additional carbonaceous processing material are still different in that one is free of a species or variety that the other contains.
[0028] In a preferred embodiment, the carbonaceous processing material and / or the further carbonaceous processing material has a potassium content in the range of 0 to 2.3 wt.%, measured according to DIN 38406-13. Preferably, the carbonaceous processing material and / or the further carbonaceous processing material has a calcium content in the range of 0 to 8 wt.%, measured according to DIN 11876:2010-12. These contents have a beneficial effect on the production of an optimized synthesis gas.
[0029] Preferably, the carbonaceous processing material and / or the further carbonaceous processing material has a carbon content of 35 to 77 wt.%, more preferably 35 to 50 wt.%, measured according to DIN 16948:2015-09. The process can be carried out particularly efficiently in this range.
[0030] Preferably, the carbonaceous processing material and / or the further carbonaceous processing material has a water content in the range of 50 to 80 wt.%, measured according to DIN 18134-1:2022. For use in step a), the carbonaceous processing material can optionally be dried. The further carbonaceous processing material can also optionally be dried before its use in step c) or d).
[0031] The synthesis gas produced in step b), the further synthesis gas produced in step d), and / or the synthesis gas combined in step e) preferably comprises CO and H2. In step b), the following reactions preferably take place:
[0032] C + CO2→ 2CO (1 )
[0033] C + H2O → CO + H2(2)
[0034] The water listed as reactant in reaction equation (2) can be supplied, for example, as steam.
[0035] The CO to H2 ratio is preferably in the range of 1:3 to 30:1, more preferably 1:2 to 25:1. These ratios are easily achievable with the process. By selecting the carbonaceous upstream material and, if necessary, the additional carbonaceous upstream material, the composition of the synthesis gas can be controlled depending on the desired carbon monoxide and hydrogen content. The composition of the synthesis gas contains different proportions of CO and H2 depending on the type or composition of the carbonaceous upstream material.
[0036] In a preferred embodiment, the electric heater is operated with surplus electrical power during step b) and / or step d). The surplus electrical power is preferably power generated from renewable energies which is not needed according to the current demand of consumers connected to the transmission grid and can therefore only be stored or alternatively used for the present process. The surplus electricity can be fed into the process, for example, from wind turbines, solar systems or the like, so that it is not necessary to use fossil fuels to generate the required electrical power. For the purposes of the invention, surplus electricity is electrical power that is produced in excess at one time or in more than required, so that it cannot be used by other electricity consumers.Steps a) and, if present, c) can also be carried out using excess electrical power. Further features and advantages of the invention are described in connection with preferred embodiments, which are explained in more detail with the aid of the following figure and the following example.
[0037] It shows:
[0038] Fig. 1 is a flowchart of a method according to the invention according to a first embodiment,
[0039] Fig. 2 is a sketched representation of a plant in which a method according to a second embodiment is carried out, and
[0040] Fig. 3 is a sketched representation of another plant in which a method according to a third embodiment is carried out.
[0041] Fig. 1 shows a flow diagram of a method according to a first embodiment. The method comprises a step a) in which a carbonaceous treatment material, such as sewage sludge, is subjected to hydrothermal carbonization at a first temperature in a range of 100 to 400°C and a pressure of 20 to 50 atm (2.027 x 10 6 Pa up to 5.066 x 10 6 Pa) to produce coal. Step a) is followed by step b) in which the coal produced in step a) is gasified at a second temperature in the range of 800 to 1,500°C using CO2 as the gasification agent to produce the synthesis gas.
[0042] Fig. 2 shows a schematic representation of a plant in which a process according to a second embodiment is carried out. The plant comprises a first reactor 1, a second reactor 2, and a third reactor 3.
[0043] The method according to the second embodiment comprises the following steps:
[0044] A carbonaceous processing material 5 is fed to the first reactor 1, as indicated by an arrow, and is subjected to hydrothermal carbonization in the first reactor 1 at a temperature in the range of 100 to 400°C and a pressure of 20 to 50 atm to produce coal 9. Process water 7 is also produced, which is discharged from the first reactor 1 separately from the coal 9, as indicated by an arrow.
[0045] The coal 9 produced in the first reactor 1 is fed to the second reactor 2, as indicated by an arrow. Furthermore, a gasification agent 11, as indicated by an arrow, and optionally steam (not shown) are fed to the second reactor 2. The coal 9 is gasified in the second reactor 2 at a temperature in the range of 800 to 1,500°C using an electric heater (not shown) and CO2 as the gasification agent 11 to produce a synthesis gas 15, which is discharged from the second reactor 2, as indicated by an arrow. Ash 13 is also produced, which is discharged from the second reactor 2 separately from the synthesis gas 15, as indicated by an arrow.
[0046] Furthermore, another carbonaceous processing material 6, which is different from the carbonaceous processing material, and another gasification agent 12 are fed to the third reactor 3, as indicated by arrows, and optionally steam (not shown). The other carbonaceous processing material 6 is gasified in the third reactor 3 at a temperature in the range of 700 to 1,500°C using an electric heater (not shown) and using CO2 as the other gasification agent 12, such that the gasification of the other carbonaceous processing material is carried out separately from the gasification of the coal 9 to produce another synthesis gas 16, which is discharged from the third reactor 3, as indicated by an arrow. In this case, another ash 14 is also produced, which is discharged from the third reactor 3 separately from the synthesis gas 16, as indicated by an arrow.
[0047] The synthesis gas 15 discharged from the second reactor 2 and the additional synthesis gas 16 discharged from the third reactor 3 are combined to obtain the synthesis gas 17. The ash 13 and the additional ash 14 are not combined but are separately used for further purposes.
[0048] Fig. 3 shows a schematic representation of a plant in which a process according to a third embodiment is carried out. The plant corresponds to the plant shown in Fig. 2, with the difference that it further comprises a fourth reactor 4.
[0049] The process according to the third embodiment corresponds to the process according to the second embodiment, with the difference that the further carbonaceous processing material 6, which is different from the carbonaceous processing material 5, is fed to the fourth reactor 4, as indicated by an arrow, and is subjected to hydrothermal carbonization in the fourth reactor 4 at a temperature in a range of 100 to 400°C and a pressure of 20 to 50 atm such that the further carbonaceous processing material 6 is subjected to hydrothermal carbonization separately from the carbonaceous processing material 5 in order to produce further coal 10 separately from the coal 9. In this process, further process water 8 is also produced, which is discharged from the fourth reactor 4 separately from the further coal 10, as indicated by an arrow.The additional coal 10 is fed to the third reactor 3 and is subjected there to gasification according to the second embodiment.
[0050] Example
[0051] 50 t of biomass with a carbon content of 45 wt.% were subjected to hydrothermal carbonization at a first temperature of 250°C and a pressure of 35 atm for a suitable period of time. Coal and process water were obtained from the hydrothermal carbonization as products, which were separated by filtration. The coal was optionally dried. The coal produced from the hydrothermal carbonization was then gasified at a second temperature of 1200°C using CO2 as the gasification agent, with up to 30 vol.% steam optionally being added to the CO2 during gasification. The gasification produced CO2- and H2-containing synthesis gas with a CO to H2 ratio of 20:1.
[0052] List of reference symbols
[0053] 1 first reactor
[0054] 2 second reactor
[0055] 3 third reactor
[0056] 4 fourth reactor
[0057] 5 carbonaceous processing material
[0058] 6 additional carbonaceous processing material
[0059] 7 Wastewater
[0060] 8 additional wastewater
[0061] 9 Coal
[0062] 10 more coal
[0063] 11 Gasifying agents
[0064] 12 further gassing agents
[0065] 13 Ashes
[0066] 14 more ashes
[0067] 15 Synthesis gas
[0068] 16 additional synthesis gas
[0069] 17 Synthesis gas
Claims
Patent claims: 1 . A process for producing synthesis gas from a carbonaceous processing material, comprising the following steps: a) subjecting the carbonaceous processing material to hydrothermal carbonization at a first temperature in a range of 100 to 400 °C and a pressure of 20 to 50 atm (2.027 x 10 6 Pa up to 5.066 x 10 6 Pa) to produce coal, b) gasifying the coal produced in step a) at a second temperature in the range of 800 to 1,500°C using an electric heater to generate the second temperature and using CO2 as gasification agent to produce the synthesis gas.
2. A method according to claim 1, characterized in that the method further comprises the following steps c) optionally subjecting a further carbonaceous processing material (6), which is different from the carbonaceous processing material (5), to hydrothermal carbonization at a third temperature in a range of 100 to 400°C and a pressure of 20 to 50 atm (2.027 x 10 6 Pa up to 5.066 x 10 6Pa) separately from the carbonaceous processing material (5) to produce further coal (10), d) gasifying the further coal (10) produced in step c) or the further carbonaceous processing material (6) at a fourth temperature in the range of 700 to 1,500°C separately from step b) using a further electrical heater to generate the fourth temperature and using CO2 as a further gasification agent (12) to produce further synthesis gas (16), e) combining the synthesis gas (15) obtained in step b) and the further synthesis gas (16) obtained in step d) to obtain the synthesis gas (17).
3. A method according to claim 1 or 2, characterized in that the first temperature and / or the third temperature is in the range of 150 to 350°C, more preferably 200 to 300°C and / or that the second temperature is in the range of 900 to 1,400°C, more preferably 1,000 to 1,300°C and / or that the fourth temperature is in the range of 700 to 1,000°C, more preferably 700 to 900°C.
4. Method according to one of the preceding claims, characterized in that the gasification agent (11) and / or the further gasification agent (12) comprises or comprise substantially 100 vol.% CO2 or a mixture of 70 to 99 vol.% CO2 and 1 to 30 vol.% H2O and / or O2 or a mixture of 80 to 98 vol.% CO2 and 2 to 20 vol.% H2O and / or O2.
5. Method according to one of the preceding claims, characterized in that a carbon source is added as an additive to the carbon-containing processing material (5) and / or the further carbon-containing processing material (6) in step a) and / or in step c).
6. Method according to one of the preceding claims, characterized in that the carbon-containing processing material (5) and / or the further carbon-containing processing material (6) comprises or comprises biomass, preferably at least one component selected from the group consisting of sewage sludge, wood, agricultural waste, green waste, grass and tree cuttings, plants, straw, silage, food waste, animal and slaughterhouse waste, paper sludge and / or pomace and / or plastic waste, wherein the carbon-containing processing material (5) and the further carbon-containing processing material (6) are different from one another.
7. Method according to claim 6, characterized in that - the carbonaceous treatment material comprises sewage sludge, more preferably a mixture of sewage sludge and wood, and optionally the further carbonaceous treatment material is free of sewage sludge, and / or - the carbon-containing processing material is free of plastic waste and the further carbon-containing processing material contains plastic waste.
8. Process according to one of the preceding claims, characterized in that the carbonaceous processing material and / or the further carbonaceous processing material has a potassium content in the range from 0 to 2.3 wt.%, measured according to DIN 38406-13, a calcium content in the range from 0 to 8 wt.%, measured according to DIN 11876:2010-12 and / or a carbon content of 35 to 77 wt.%, measured according to DIN 16948:2015-09.
9. Process according to one of the preceding claims, characterized in that the carbonaceous processing material and / or the further carbonaceous processing material has a water content in the range of 50 to 80 wt.%, measured according to DIN 18134-1:2022.
10. Method according to one of the preceding claims, characterized in that the synthesis gas (15, 17) and / or the further synthesis gas (16) comprises or comprises CO and H2.
11. Process according to claim 10, characterized in that a ratio of CO to H2 is in the range of 1:3 to 30:1, preferably 1:2 to 25:
1.
12. Method according to one of the preceding claims, characterized in that the electric heater is operated during step b) and / or step d) using excess electric current.