Method and apparatus for producing a hydrogen-containing synthesis gas

Abstract

1. The invention relates to a method for producing a hydrogen-containing synthesis gas, comprising the following method steps: A) providing a solid (2) consisting substantially of carbon (C) in a first reaction chamber (8); B) feeding steam (H2O) and optionally oxygen (O2) into the first reaction chamber in such a way that a water gas reaction and / or an oxidation, in particular an at least partial combustion, of the solid (2) forms a raw gas (R) which comprises at least carbon monoxide (CO) and steam (H2O); C) heating the raw gas in a second reaction chamber such that a water gas shift reaction forms a mixture (G) comprising at least carbon dioxide (CO2) and hydrogen (H2) and steam (H2O); D) cooling the mixture (G), wherein the steam (H2O) contained in the mixture (G) is at least partially condensed and the hydrogen-containing synthesis gas (3) is formed.

Description

[0001] title

[0002] Method and apparatus for the production of a hydrogen-containing synthesis gas

[0003] Description

[0004] The invention relates to a method and a device for producing a hydrogen-containing synthesis gas.

[0005] The use of fossil fuels releases various greenhouse gases into the Earth's atmosphere, thereby increasingly intensifying the so-called greenhouse effect, which contributes to the growing warming of the Earth's climate. This has demonstrably negative consequences for all life on Earth. Therefore, it is essential to develop alternative energy sources to replace fossil fuels.

[0006] Besides emission-free energy generation through wind and solar power, the sustainable use of CO₂-neutral energy carriers from biomass also offers an alternative. The technological potential here is enormous, but so far only a very small portion of it is used for energy production. In conventional biogas plants, only about 40% of the energy contained in the biomass used is utilized. Furthermore, the CO₂ footprint of biogas plants that use so-called energy crops is particularly disadvantageous, as the effort required for cultivating the crops, as well as for the subsequent disposal of the digestate on agricultural land, results in considerable CO₂ emissions. Biogas plants that use waste as an energy carrier, on the other hand, are much more promising. For example, energy in the form of heat can be generated with low carbon dioxide emissions in wood combustion plants.However, these systems are almost exclusively limited to the use of wood and are usually very sensitive to moisture content, bark content, and natural variations in calorific value, as these factors can negatively affect combustion. This can lead to the generation of environmentally and health-damaging emissions such as particulate matter, nitrogen oxides, dioxins, and furans.

[0007] 35218-P-WO Bg / so 05.03.2026 From DE 102023 102586 A process is known by which carbon can be produced from any organic biomass. This process makes it possible to tap into the large, previously untapped biomass potential of residues and waste materials generated in society, agriculture, and industry for the production of carbon-neutral energy. By applying this technology, enormous quantities of solid carbon, especially in the form of biochar, can be produced. This solid carbon can be stored as a CO2 sink in the soil or in other applications such as building materials or road surfaces, thus representing a climate-friendly equivalent to the CO2 produced during the combustion of fossil fuels.

[0008] The object of the invention is to propose an energetic utilization of solid carbon. This object is achieved by a method according to claim 1 and a device according to claim 15. Advantageous embodiments are the subject of dependent claims.

[0009] The process according to the invention serves to produce a hydrogen-containing synthesis gas and comprises the following process steps:

[0010] A) Providing a solid consisting mainly of carbon (C) (2) into a first reaction chamber (8);

[0011] B) Supply of water vapor (H2O) and optionally oxygen (O2) into the first reaction chamber, such that a raw gas (R) is formed by carrying out a water gas reaction and / or an oxidation, in particular at least partial combustion, of the solid (2), which contains at least carbon monoxide (CO) and water vapor (H2O);

[0012] C) Heating the raw gas in a second reaction chamber such that a mixture (G) is formed by carrying out a water-gas shift reaction, which comprises at least carbon dioxide (CO2) and hydrogen (H2) and water vapor (H2O); D) Cooling the mixture (G), whereby the water vapor (H2O) contained in the mixture (G) is at least partially condensed and the hydrogen-containing synthesis gas (S) is formed.

[0013] 35218-P-WO Bg / so 05.03.2026The invention is based on the knowledge that the carbon, which can be generated in particular during the gasification of biomass products, can be used to produce a hydrogen-containing synthesis gas by means of further chemical treatment according to the above-mentioned process steps.

[0014] The solid, consisting essentially of carbon, may be the product of combustion or pyrolytic decomposition of an organic starting material. The solid consists primarily of elemental carbon, with the carbon comprising more than 70%, more particularly more than 80%, and preferably more than 90% by mass and / or volume. The solid may also contain trace amounts of impurities or residual components of the organic starting material and / or minerals.

[0015] In process step A), the solid is introduced into the first reaction chamber. This can be done manually or automatically. In particular, it is conceivable that the solid is introduced directly into the first reaction chamber or indirectly, via an intermediate section of the device, for example a magazine, from which the solid can enter the first reaction chamber.

[0016] In process step B), the solid is subjected to a thermochemical transformation in the first reaction chamber to convert it, at least partially, into carbon monoxide. This reaction can take place under controlled temperature and pressure conditions, whereby the supply of steam and, optionally, oxygen can be precisely controlled to enable a water-gas reaction and / or at least partial oxidation. It is also conceivable that the process can be carried out without the addition of oxygen, as will be explained in detail below. Therefore, it is within the scope of the invention for process step B) to occur before or simultaneously with process step C).

[0017] Depending on the composition of the solid and the reaction conditions, additional reaction products can be formed. The reaction parameters, including temperature, residence time, and gas atmosphere, are specifically adjusted to maximize the formation of a single reaction product.

[0018] 35218-P-WO Bg / so 05.03.2026 A high yield of carbon monoxide is achieved while minimizing unwanted byproducts.

[0019] It is within the scope of the invention that, for process step B), oxygen and carbon react in the first reaction chamber to form carbon monoxide, and water vapor is mixed with the carbon monoxide to form the raw gas. It is also conceivable that water vapor and oxygen are introduced into the first reaction chamber, wherein the oxygen reacts with a portion of the carbon to form carbon monoxide in the manner described above, and the water vapor reacts with another portion of the carbon, particularly at temperatures above 850°C, in a water-gas reaction to form carbon monoxide and hydrogen, and forms the raw gas with the remaining water vapor. It is also conceivable that no oxygen, but only water vapor, is introduced into the first reaction chamber to react in a water-gas reaction to form carbon monoxide and hydrogen, and to form the raw gas with the remaining water vapor.According to the invention, it is irrelevant in which of the described ways the raw gas is formed with the carbon monoxide and the water vapor. It is also within the scope of the invention that the first reaction chamber is divided into several sections or sub-chambers and, in particular, that the supply of water vapor and oxygen takes place in different sections.

[0020] The first reaction chamber is preferably equipped with temperature control and a defined gas flow to ensure uniform reaction control. If necessary, catalysts or special reactor materials can be used to further improve the selectivity of the conversion.

[0021] The supply of steam and / or oxygen can be continuous or intermittent and is specifically controlled with regard to pressure, temperature, and ratio to achieve an optimal synthesis gas composition. These process parameters are selected to maximize CO yield while minimizing the formation of undesirable byproducts.

[0022] 35218-P-WO Bg / so 05.03.2026 The first reaction chamber is preferably equipped with a steam injection unit and / or a mixing chamber that ensures uniform mixing of the steam with the reactants and the raw gas. Optionally, the steam supply can be optimized by catalytic or thermal assistance to further improve the reaction rate and selectivity.

[0023] The raw gas produced in the first reaction chamber is transferred to a second reaction chamber and heated there to a defined temperature, specifically above 1500°C, to enable a targeted chemical conversion. This heating initiates a water-gas shift reaction in which the carbon monoxide contained in the raw gas reacts with water vapor, producing a gas mixture consisting primarily of carbon dioxide and hydrogen, as well as water vapor, which did not react in the water-gas shift reaction.

[0024] The reaction temperature and pressure in the second reaction chamber are adjusted to achieve high conversion efficiency, allowing the water-gas shift reaction to be carried out in either a low-temperature or high-temperature process. To further optimize the reaction rate and selectivity, the second reaction chamber can be equipped with a catalyst, such as iron oxide, chromium oxide, or copper-zinc-aluminum oxide.

[0025] The process control ensures maximum carbon dioxide removal and optimizes the hydrogen content of the resulting gas mixture. The subsequent process stage can include gas purification or a separation stage for further processing of the gas streams.

[0026] The gas mixture (G) generated in the second reaction chamber is selectively cooled in a downstream cooling stage to cause the water vapor it contains to condense. This cooling process allows at least some of the water vapor to condense into liquid water, while the remaining hydrogen-containing synthesis gas is recovered.

[0027] 35218-P-WO Bg / so 05.03.2026 Cooling can be achieved using a heat exchanger, direct water cooling, or another suitable cooling technology. The temperature is controlled to ensure the most complete possible condensation of the water vapor without the formation of undesirable side reactions or impurities in the synthesis gas.

[0028] The hydrogen-rich synthesis gas obtained in this way can then be subjected to further purification, separation or storage in order to make it usable for subsequent applications, such as chemical synthesis or energy production.

[0029] In an advantageous further development of the process, in process step B) at least partial combustion of the solid takes place with the supply of oxygen, in particular hot air containing oxygen, whereby carbon monoxide is formed and the water vapor is mixed with the carbon monoxide to form the raw gas, in particular in a mixing section within the first reaction chamber.

[0030] The targeted supply of oxygen releases exothermic heat energy. This heat can be used to reach or maintain the additional temperatures required by the solid, thereby reducing the overall energy consumption of the process.

[0031] Additionally, the controlled oxygen supply ensures that the solid is not completely combusted to carbon dioxide, but rather that a high proportion of carbon monoxide is retained, which is used for subsequent process steps. The amount of oxygen is metered to ensure optimal reaction control between combustion and the desired conversion to synthesis gas.

[0032] This process variant enables efficient heat utilization, targeted process control and improved carbon utilization, which is particularly advantageous for industrial applications with high energy demands.

[0033] As mentioned above, ordinary air with a natural oxygen content of approximately 20% can be used instead of pure oxygen. Studies have shown that the high nitrogen content in the air does impair the reaction behavior.

[0034] 35218-P-WO Bg / so 05.03.2026, however, this simplifies the process and thus, contrary to expectations, makes it more efficient. Other gases or gaseous substances can also be added to the oxygen required for oxidation in order to selectively trigger further potentially advantageous reactions in the first or second reaction chamber, thereby eliminating the disadvantages of using air with a natural oxygen content.

[0035] In an advantageous further development of the process, the carbon-containing solid (C) is provided in process step A as a lump substance, in particular in the form of a briquette. In process step B), the solid partially protrudes into the first reaction chamber.

[0036] The further development described above offers several advantages. By partially introducing the solid material into the reaction zone, it can be converted gradually, ensuring a uniform reaction and consistent gas production. The unreacted portion of the briquette remains outside the hot reaction zone, allowing for controlled material feed and preventing undesirable overheating or complete combustion. This process enhancement results in overall good process control, high energy efficiency, and optimal material utilization, particularly in the industrial production of hydrogen-containing synthesis gas.

[0037] In an advantageous further development of the process, the carbon-containing solid is received in a magazine in process step A) and conveyed into the first reaction chamber via a feed chamber by means of a feeder.

[0038] The magazine enables the storage and on-demand supply of the solid material for carrying out the process steps according to the invention in the first reaction chamber. For this purpose, the solid material is transferred from the magazine into a feed chamber. Within this feed chamber, the material is metered and conveyed in a controlled manner towards the first reaction chamber. The movement of the solid material along the feed chamber is preferably effected by a mechanical or pneumatic feeding device, for example, a screw conveyor for a uniform and controllable material feed, or similar.

[0039] 35218-P-WO Bg / so 05.03.2026 A piston or plunger feed for discontinuous, yet pressure-stable conveying. This feed system allows for the controlled introduction of the solid material into the first reaction chamber, where it undergoes stepwise thermochemical conversion. This targeted feeding improves reaction control and process stability, as residence time, temperature load, and gas formation rate can be optimized. Additionally, this enables automated process control, which is particularly advantageous for continuous industrial applications. The combination of magazine, feed chamber, and conveying mechanism ensures an efficient, uniform, and reproducible supply of the solid material to the reactor, further improving synthesis gas yield and the energy efficiency of the process.In particular, the feed chamber can be arranged relative to the magazine such that a second solid, especially in the form of a briquette, is conveyed into the feed chamber by gravity or by means of a pusher mechanism as soon as a first solid previously located in the feed chamber has been completely conveyed into the first reaction chamber. In particular, the magazine is designed as a stacking magazine, which serves to hold several stackable briquettes and opens into the feed chamber at one end, especially on a bottom side, so that a briquette located at the bottom can enter the feed chamber as soon as the necessary space in the feed chamber is released.

[0040] In an advantageous further development of the process, the oxygen, in particular the hot air, is directed by means of a directed stream specifically onto a front end of the solid, which projects into the first reaction chamber.

[0041] The targeted oxygen supply described above offers several advantages. Direct application to the end face of the solid enables localized, targeted oxidation. This promotes the partial combustion of carbon to carbon monoxide and prevents uncontrolled, complete combustion to carbon dioxide. The directed oxygen or hot air flow results in focused heat generation at the reaction zone. This maintains a stable reaction temperature without the entire solid being heated uncontrollably. The targeted oxidation of the end face leads to controlled degradation of the solid while fresh material can be fed in. This allows for continuous or intermittent feeding of the solid.

[0042] 35218-P-WO Bg / so 05.03.2026, which increases process stability. The directed oxygen supply allows for targeted control of the flow dynamics of the reaction gases within the chamber, leading to more efficient synthesis gas production. This advanced training improves process control, energy efficiency, and carbon utilization, particularly in industrial applications for synthesis gas production or the thermochemical conversion of solid fuels.

[0043] In an advantageous further development of the process, a burned portion of the solid is mechanically separated from the unburned solid in the first reaction chamber. In particular, the burned portion falls off in the first reaction chamber.

[0044] By selectively separating the combustion residues, such as ash or non-reactive carbon, from the still-reactive solid, the reaction surface remains clear, allowing the conversion process to continue unimpeded. The removal of the spent solid components reduces deposits and prevents layer formation that could impede heat exchange and gas flow. Mechanical separation ensures that essentially only reactive carbon remains in the reaction zone. This results in a more stable CO and H₂ concentration. z-Formation and minimizes the formation of unwanted byproducts. Since the burnt solid is removed automatically or by a mechanical device, such as a shaking mechanism or scraper, fresh solid can be fed in, enabling continuous operation. Separation can be achieved through various mechanical principles, for example, by means of a shaking or vibration mechanism to detach the burnt layer and / or by means of a scraping device that selectively removes the burnt portion. This advanced technology significantly contributes to the process stability, energy efficiency, and ease of maintenance of the system and is particularly advantageous for high-throughput industrial applications.

[0045] In another advantageous further development, the carbon-containing solid (C) is provided as bulk material in process step A and placed on a gas-permeable substrate in the first reaction chamber for the execution of process step B).

[0046] 35218-P-WO Bg / so 05.03.2026 The bulk material can consist of granulated, pelletized, or crushed particles that allow for easy handling, storage, and conveying. It is conceivable that the shape of the bulk material results directly from the properties of its organic feedstock, which may itself already be in bulk form. It is also conceivable that the bulk material is obtained by mechanically breaking down a solid material that is present as lump material.

[0047] For process step B), the solid is placed on a gas-permeable substrate in the first reaction chamber. This gas-permeable substrate ensures that the reaction gases, such as oxygen, especially hot air, and / or steam, can flow evenly through the solid bed, enabling a homogeneous and efficient conversion of the solid. This allows for a high yield of carbon monoxide and, if applicable, hydrogen. Furthermore, the gas-permeable substrate prevents the solid bed from becoming blocked or clumped, thus ensuring continuous gas flow and process stability. This facilitates continuous operation, as spent solid material can fall through the openings in the substrate while new bulk material is fed in.The process offers flexible adaptation options for different solids and enables an effective and stable thermochemical conversion of the material.

[0048] In an advantageous further development of the process, the bulk material is at least partially permeated by oxygen and / or water vapor, particularly through the gas-permeable substrate. This measure enables a particularly efficient reaction, as the reaction gases are guided directly and uniformly through the bulk material bed, allowing a reaction zone to form within the bulk material. The uniform flow ensures optimal contact time between the reactants and the solid, thereby significantly improving the thermochemical conversion of the bulk material, such as the formation of carbon monoxide and, if applicable, hydrogen.

[0049] Using a grate or perforated plate as a gas-permeable base ensures that gases are evenly distributed not only from the surface of the bulk material but also deep within the material bed. This prevents hotspots and ensures that the entire solid is efficiently processed. This approach also supports the

[0050] 35218-P-WO Bg / so 05.03.2026 Control of the reaction temperature and promotes stable process control, as a uniform heat distribution is achieved.

[0051] By selectively flowing the reaction gases through the bulk material, the formation of undesirable byproducts such as carbon dioxide is minimized, while the desired gas composition is optimally achieved. This advanced training thus improves the energy efficiency and carbon utilization of the process, which is particularly advantageous in large industrial applications.

[0052] In an advantageous further development of the process, the solid reacts with a first part of the water vapor by carrying out a water-gas reaction to form carbon monoxide and hydrogen, and the raw gas contains the previously formed carbon monoxide, the previously formed hydrogen, and a second part of the water vapor.

[0053] This simultaneous process enables efficient use of the reaction gases, as both the conversion of the solid to carbon monoxide and the reaction with the steam to produce hydrogen can occur in parallel, generating the raw gas. This results in rapid and uniform gas production without the need for the two conversions to occur sequentially, significantly increasing the efficiency of the process. It is advantageous that this method eliminates the need to introduce oxygen separately into the first reaction chamber; instead, the oxygen bound in the steam can be used to generate the carbon monoxide. This is particularly feasible at temperatures above 850°C. Furthermore, it is beneficial that hydrogen can be produced not only in the second reaction chamber but also in the first.

[0054] It is conceivable that the process in the first reaction chamber involves a temperature increase, whereby oxygen is added to the first reaction chamber in an initial temperature range below 850°C and no oxygen is added above 850°C. It is also conceivable that the process is carried out exclusively above 850°C and entirely without the addition of oxygen to the first reaction chamber.

[0055] 35218-P-WO Bg / so 05.03.2026 In process step C), the raw gas already produced, which contains carbon monoxide and water vapor, is further processed. Here, the raw gas consisting of carbon monoxide, hydrogen, and water vapor undergoes an additional conversion to a mixture of carbon dioxide, additional hydrogen, and a portion of water vapor. This step can be supported by targeted temperature control or catalysts to achieve the desired gas composition. Performing the first two steps simultaneously maximizes efficiency and reduces energy consumption, as no additional reaction chambers or delay times are required.

[0056] This beneficial advanced training leads to optimized process control, in which the conversion of the solid material into valuable synthesis gases occurs in a continuous, virtually frictionless process. Furthermore, the overall production rate of the hydrogen content in the synthesis gas is maximized, and the energy efficiency of the entire process is increased.

[0057] In an advantageous further development of the process, the second reaction chamber is designed as a spiral tube, which is in thermally conductive contact with at least one heating element. Heat transfer to the spiral tube via radiation is advantageous, although heat transfer by convection is also possible. This special design enables very efficient heat transfer, since the spiral tube, due to its shape, offers a large surface area that optimally transfers heat to the flowing raw gas. The raw gas, which originates from the first reaction chamber and contains carbon monoxide and water vapor, can be heated to up to 1500°C in the second reaction chamber. Lower temperatures can also be used.

[0058] By directly coupling the gas to a heating element, in particular at least one electric heating coil, heat is radiated directly onto the coiled pipe. The gas temperature can be precisely controlled and kept constant, which is crucial for the conversion of carbon monoxide and water vapor to carbon dioxide and hydrogen. The high temperature of up to 1500°C promotes the water-gas shift reaction, in which carbon monoxide reacts with water vapor to form the desired gases.

[0059] 35218-P-WO Bg / so 05.03.2026 The coiled pipe also enables an optimal residence time of the raw gas in the reaction chamber, resulting in a more complete conversion. This heat transfer device reduces energy consumption by minimizing heat losses and efficiently maintaining the conversion temperature. The heating elements, which are in direct contact with the coiled pipe, can be electrically or thermally operated and allow for precise control of the temperature profiles within the chamber.

[0060] This further development of the process leads to a significant increase in the reaction rate, efficient use of energy and improved yield of the desired synthesis gases, making the process particularly advantageous for industrial applications.

[0061] In an advantageous further development of the process, the cooling device comprises a first heat exchanger containing a cooling coil that runs, at least partially, through a water bath. This design enables efficient cooling of the raw gas, which, after conversion in the second reaction chamber, is transferred to the cooling device. The cooling coil, which is installed in a heat exchanger, absorbs the heat from the gas stream and transfers it to the water bath.

[0062] The water bath serves as a cooling medium because it has a high specific heat capacity and is able to absorb a large amount of heat without itself heating up significantly. The direct heat transfer from the cooling coil to the water bath efficiently cools the raw gas, which is particularly important for the condensation of water vapor and the subsequent formation of the hydrogen-containing synthesis gas (S).

[0063] This process offers the advantage that cooling via the water bath not only enables efficient temperature control but also minimizes heat loss, as the heat is utilized in a controlled closed-loop system. The water bath can either be operated in a continuous closed-loop system or replaced regularly.

[0064] 35218-P-WO Bg / so 05.03.2026 Additionally, the use of the cooling coil in conjunction with the water bath supports gas purification, as some of the water vapor contained in the gas can condense, thus further purifying the gaseous synthesis gas. This further development leads to efficient and energy-optimized cooling of the gas and simultaneously contributes to improving overall process stability and product quality.

[0065] In an advantageous further development of the process, in process step D) the mixture is cooled such that the water in the water bath at least partially evaporates and this water vapor (D) is generated for process step B). The water vapor is thereby selectively fed into the first reaction chamber.

[0066] This measure enables efficient resource recovery within the process and ensures a closed-loop system for the steam. Instead of supplying external steam, the water generated during the cooling process is reused, contributing to energy and resource conservation. The heat contained in the gas is used to generate the steam produced by evaporating the water bath, which is then required in process step C for the conversion of carbon monoxide and the production of hydrogen.

[0067] The advantage of this advanced training lies in the efficient extraction of steam from the cooling phase, while simultaneously improving the utilization of heat within the system. This not only reduces the energy required for steam generation but also decreases the need for external energy for steam input in the process.

[0068] In an advantageous further development of the method, the cooling device comprises at least a second heat exchanger, in particular a condensation heat exchanger, in which the proportion of water vapor contained in the mixture is at least partially condensed.

[0069] The condensation heat exchanger utilizes the heat difference between the mixture and a cooling medium, such as water or another cooling fluid, to selectively condense the water vapor in the gas stream. This results in the water vapor contained in the gas being converted into liquid water, thereby selectively removing the gas phase of the mixture from the gaseous phase.

[0070] 35218-P-WO Bg / so 05.03.2026 excess water vapor is removed. This step not only contributes to temperature control, but also to the utilization and separation of the water vapor, which can be beneficial in subsequent processes.

[0071] One advantage of this advanced process is that the water vapor is efficiently removed from the gas stream, resulting in a purer gas mixture for subsequent reaction steps, such as in synthesis gas production. The condensed water can then be returned to the water cycle and integrated into the process, for example, by using it in process step C for steam generation.

[0072] In an advantageous further development of the method, the cooling device comprises at least a second heat exchanger, in particular a condensation heat exchanger, in which the proportion of water vapor contained in the mixture is at least partially condensed.

[0073] The condensation heat exchanger enables the targeted separation of water vapor from the mixture by transferring the heat of the gas to a colder cooling medium, thus converting the water vapor into liquid water. This process ensures that excess water vapor is removed from the gas stream, resulting in improved gas quality and better separation of the desired gases. The condensed liquid can then either be reused in the process or discharged as a byproduct.

[0074] Another advantage of this advanced process lies in its energy efficiency. The heat released during the condensation of the water vapor can be used to preheat other process streams, thus reducing the overall energy consumption of the process. Furthermore, the condensation heat exchanger helps to control the temperature of the mixture, which is important for subsequent steps in the process, such as synthesis gas production.

[0075] This type of cooling and condensation also offers the possibility of using the water vapor specifically for the water-gas reaction in process step B), thus creating a closed system.

[0076] 35218-P-WO Bg / so 05.03.2026 A closed-loop system is created for the process water. This increases resource efficiency and contributes to more sustainable process management.

[0077] In a further advantageous development of the process, an electrolyzer is used to generate oxygen and hydrogen. The oxygen obtained through the electrolysis of water is supplied in process step B) to support the combustion of the solid. In this step, the generated oxygen can contribute to promoting the conversion of carbon to carbon monoxide, thus increasing the efficiency of the entire process.

[0078] The hydrogen, also produced in the electrolyzer, is mixed with the hydrogen-containing synthesis gas generated in later process steps. This mixture of hydrogen and synthesis gas can then be used for further applications or to produce other valuable chemicals. Direct use of the hydrogen produced in the electrolyzer optimizes resource utilization, as no external hydrogen sources are required and the entire hydrogen cycle remains within the process.

[0079] This advanced training leads to a decentralized hydrogen supply within the process, further improving the energy efficiency and sustainability of the system. Using oxygen to support combustion and hydrogen to expand the synthesis gas mixture makes the process more resource-efficient overall and contributes to better process integration.

[0080] The problem is also solved by a device for generating hydrogen-containing synthesis gas. The device according to the invention comprises a first reaction chamber for receiving and combusting a carbon-containing solid, wherein a line for supplying oxygen and / or a steam line opens into the first reaction chamber. Furthermore, the device comprises a second reaction chamber, which is connected to the first reaction chamber by means of a gas conductor and is in thermally conductive contact with one or more heating elements, preferably by means of electrically heated coils.

[0081] 35218-P-WO Bg / so 05.03.2026 the device includes a cooling device which is connected to the second reaction chamber via a gas conductor.

[0082] In an advantageous further development, the second reactor chamber is designed as a metallic tube ring or metallic tube bundle and is at least partially surrounded by an electrical induction coil with which the second reactor chamber is in thermally conductive contact.

[0083] In an advantageous further development, the device has a magazine for receiving the carbon-containing solid and a feed chamber through which the carbon-containing solid can be conveyed from the magazine into the first reaction chamber.

[0084] In an advantageous further development, the device comprises a separating agent which is movably arranged in the first reaction chamber and is designed to come into contact with a part of the solid projecting into the first reaction chamber.

[0085] In an advantageous further development, the device comprises a gas-permeable base for receiving the carbon-containing solid, in particular as bulk material, which is arranged in the first reaction chamber.

[0086] In an advantageous further development, the oxygen line and / or the steam line lead into the first reaction chamber in such a way that a carbon-containing solid located on the substrate can be permeated, in particular from a side of the substrate facing away from the solid.

[0087] The device according to the invention is particularly suitable for carrying out the method according to the invention or one of its advantageous embodiments. In this respect, the descriptions regarding the features as well as their technical effects and advantages of the method are transferable to the device according to the invention and vice versa.

[0088] Advantageous embodiments of the invention are explained below with reference to the figures. They show

[0089] 35218-P-WO Bg / so 05.03.2026 Figure 1 shows a first variant of a device for producing a hydrogen-containing synthesis gas with a detailed representation of a first reaction chamber;

[0090] Figure 2 shows a second variant of a device for producing a hydrogen-containing synthesis gas;

[0091] Figure 3 shows the first variant of the device for generating hydrogen-containing synthesis gas in conjunction with different oxygen sources according to views a), b).

[0092] The use of fossil fuels leads to the release of numerous greenhouse gases into the atmosphere, thereby intensifying the so-called greenhouse effect and further warming the Earth's climate—a process that demonstrably has negative impacts on all life forms. Therefore, it is necessary to develop alternative energy sources that can replace fossil fuels. A promising solution is provided by plants that use waste to produce gaseous energy carriers. In this process, the waste itself is converted into carbon-rich solids through pyrolytic transformation. Figures 1 to 3 show devices that make it possible to utilize the energy from the produced solids in an optimal way.

[0093] Figure 1 shows a device 1 by means of which it is possible to convert a solid 2 consisting essentially of carbon into a hydrogen-containing synthesis gas 3. For this purpose, the solid 2 in the form of a briquette is first fed into a magazine 4, which can be closed by means of a flap 5, and can be stored there together with several other carbon briquettes.

[0094] The solid 2 enters a feed chamber 6 via the magazine 4, through which it is continuously conveyed into a first reaction chamber 8 by means of a feeder 7. In the embodiment shown here, the feeder 7 is...

[0095] 35218-P-WO Bg / so 05.03.2026um a movable piston which, by means of a motor 9, presses against the solid 2 and thereby conveys it into the first reaction chamber 8 from the front.

[0096] The first reaction chamber 8 is a heat-resistant chamber into which the feed chamber 6 opens. A hot air blower 10 comprises a heating coil and has a check valve 11 on the suction side, through which an air supply connection can be opened by creating a vacuum and ambient air L can be drawn in. On the pressure side, the hot air blower has the aforementioned heating coil, by means of which the ambient air L can be heated. If necessary, oxygen O2 can be mixed with the heated ambient air L. The amount of oxygen mixed can be adjusted by means of a valve 12, and an unwanted backflow can be prevented by means of a check valve 13.

[0097] The heated mixture of ambient air L and oxygen O2 is directed by means of a directed stream 14 onto the end face of the solid 2, which protrudes into the first reaction chamber 8, whereby in this embodiment combustion of the solid takes place and carbon monoxide CO is formed.

[0098] As shown in the detailed view, a separation device 15 is movably arranged in the first reaction chamber 8, by means of which a reacted component of the solid 2 is separated from the unreacted part of the solid 2 and can fall off as ash or non-reactable carbon fractions 16. By opening a bottom flap 17, the first reaction chamber 8 can be cleaned of the ash or the remaining carbon fractions 16.

[0099] By adding water vapor H2O, a raw gas R is produced in a mixing section 18 together with the carbon monoxide CO contained in the first reaction chamber 8, which is then directed into a second reaction chamber 19.

[0100] In the embodiment shown in Figure 1, the second reaction chamber 19 is designed as a tubular coil 19 wound around a heating element 20. The heating element 20 is supplied with energy via a connection 21 and serves to heat the raw gas R contained in the tubular coil 19. This process converts carbon monoxide (CO) and water vapor into hydrogen.

[0101] 35218-P-WO Bg / so 05.03.2026HjO a mixture G of carbon dioxide CO2, hydrogen H2 and excess water vapor H2O is produced.

[0102] The mixture G is fed from the second reaction chamber 19 into a cooling device, which includes a cooling coil 22 wound around a steam boiler 23. The steam boiler 23 can be filled with water H2O via the supply line 24, which is heated and at least partially evaporates as a result of heat exchange with the mixture G. A steam line 25 connects the steam boiler 23 to the first reaction chamber 8 and provides steam H2O for the production of the raw gas R.

[0103] The cooled mixture G is fed into a condensation heat exchanger 26, by means of which the water vapor H2O contained in the mixture G is separated by condensation, thereby producing the synthesis gas 3. The condensation heat exchanger 26 can be supplied with coolant 29 for its operation. The condensate H2O exits the device 1 via a siphon 30. An insulating jacket 31 serves for the thermal insulation of the device.

[0104] Figure 2 shows a device 1 by means of which it is also possible to convert a solid 2 consisting essentially of carbon into a hydrogen-containing synthesis gas 3. For identical or equivalent features, the same reference symbols are used for clarity as in Figure 1.

[0105] In contrast to the embodiment shown in Figure 1, the solid 2 is not present as a lump product in the form of briquettes, but as a bulk material, i.e., in a multi-layered, granular form. Such a state of the solid 2 can result, for example, if the organic starting material from which the solid 2 is obtained is present in a corresponding bulk material and is decomposed to carbon by pyrolytic conversion, or if a solid 2 present as a lump product is mechanically comminuted.

[0106] For use in the device according to Figure 2, the solid 2 is placed on a gas-permeable substrate 32 in a first reaction chamber 8. Oxygen O2 is heated, either in elemental form or as a component of ambient air, and introduced via line 33 into the

[0107] 35218-P-WO Bg / so 05.03.2026 first reaction chamber 8 introduced to react with the carbon of solid 2 to form carbon monoxide CO.

[0108] Simultaneously, liquid water can be introduced via the supply line 34 into a boiler 35 with a bottom-mounted heating element 36 and heated therein to generate steam H2O. This steam H2O rises into a heating device 37 with a coiled pipe 38, which is surrounded by several heating elements 39.

[0109] The water vapor H₂O is heated and fed into the first reaction chamber 8, where it mixes with the oxygen O₂ and the carbon monoxide already formed to produce the raw gas R. Investigations have shown that, particularly at temperatures above 850°C, the water vapor can also react directly with the carbon in a reaction zone 40, also producing carbon monoxide CO and hydrogen H₂. Above this temperature, the process described here can therefore proceed without the additional addition of oxygen O₂, and the raw gas, containing carbon monoxide, hydrogen, and excess water vapor, can be fed into the second reaction chamber 22. It is conceivable that the process involves a temperature increase, with oxygen being added to the first reaction chamber 8 in an initial temperature range below 850°C and no oxygen being added above 850°C.It is also conceivable that the process is carried out exclusively above 850°C and entirely without the addition of oxygen O2.

[0110] The second reaction chamber 22 is designed as a spiral tube and is surrounded by a plurality of heating elements 41. The raw gas R in the second reaction chamber 22 is heated, thereby initiating a water-gas shift reaction in which the carbon monoxide CO contained in the raw gas R and the water vapor H2O react to form carbon dioxide CO2 and hydrogen H2. The resulting mixture G is directed via a discharge into a condensing heat exchanger 26, in which the excess water vapor is separated. A coolant 29 flows through this heat exchanger, as shown in Figure 1. Separated water H2O is discharged from the device 1 via a siphon 30.

[0111] 35218-P-WO Bg / so 05.03.2026 Figure 3 shows various application configurations of the devices 1 according to Figures 1 and 2 in abstract form.

[0112] View a) of Figure 3 shows that one of the devices 1 shown in Figures 1 or 2 can be directly filled with the solid 2, which consists essentially of carbon, and supplied with tempered oxygen O2, water for the generation of steam H2O, and coolant 29 for the process. Based on the process principles described for Figures 1 and 2, a hydrogen-containing synthesis gas 3 is generated, and heated coolant 29 and separated water H2O are discharged.

[0113] View b) of Figure 3 shows that instead of the oxygen source shown in view a), an electrolyzer 42 can also be used, in which oxygen (O2) and hydrogen (H2) can be obtained by electrolysis of water (H2O). The oxygen can be used to operate the device 1. The hydrogen (H2) can be mixed with the synthesis gas 3.

[0114] Synthesis gas 3 can be used in households or, for example, as an energy carrier in means of transport.

[0115] 35218-P-WO Bg / so 05.03.2026

Claims

Claims 1. Process for producing a hydrogen-containing synthesis gas comprising the following process steps A) Providing a solid consisting mainly of carbon (C) (2) into a first reaction chamber (8); B) Supply of water vapor (H2O) and optionally oxygen (O2) into the first reaction chamber, such that a raw gas (R) is formed by carrying out a water gas reaction and / or an oxidation, in particular an at least partial combustion, of the solid (2), which comprises at least carbon monoxide (CO) and water vapor (H2O); C) Heating the raw gas in a second reaction chamber such that a mixture (G) is formed by carrying out a water-gas shift reaction, which comprises at least carbon dioxide (CO2) and hydrogen (H2) and water vapor (H2O); D) Cooling the mixture (G), whereby the water vapor (H2O) contained in the mixture (G) is at least partially condensed and the hydrogen-containing synthesis gas (3) is formed.

2. Method according to claim 1, wherein in process step B) an oxidation, in particular combustion, of the solid (2) takes place with the supply of oxygen (O2), in particular hot air containing oxygen (O2), in particular in an oxidation section of the first reaction chamber, whereby carbon monoxide (CO) is formed and the water vapor (H2O) is mixed with the carbon monoxide (CO) to form the raw gas (R), in particular in a mixing section of the first reaction chamber (8).

3. Method according to claim 1 or 2, wherein the carbon-containing solid (2) is provided in process step A) as a piece product, in particular in the form of a briquette, and in process step B) partially projects into the first reaction chamber (8). 35218-P-WO Bg / so 05.03.20264. Method according to claim 3, wherein the carbon-containing solid is received in a magazine in process step A) and conveyed into the first reaction chamber (8) via a feed chamber (6) by means of a feed means (7).

5. Method according to at least one of claims 2 to 4, wherein the oxygen, in particular the hot air, is directed by means of a directed stream onto an end face of the solid (2) which projects into the first reaction chamber (8).

6. Method according to at least one of claims 2 to 5, wherein a burned part of the solid (2) is mechanically separated from the remaining solid (2) in the first reaction chamber (8) and in particular falls off in the first reaction chamber (8).

7. Method at least according to claim 1, wherein the carbon-containing solid (2) is present as bulk material in process step A) and is introduced into the first reaction chamber (8) on a gas-permeable substrate for process step B).

8. Method according to claim 7, wherein the bulk material is at least partially permeated by the oxygen (O2) and / or the water vapor (H2O), preferably through the gas-permeable substrate.

9. Method according to claim 7 or 8, wherein the solid (2) in process step B) reacts with a first part of the water vapor (H2O) by carrying out a water-gas reaction to carbon monoxide (CO) and hydrogen (H2) and the raw gas (R) contains the carbon monoxide (CO), the hydrogen (H2) and a second part of the water vapor (H2O).

10. Method according to claim 9, wherein above a temperature of 850°C the supply of oxygen to the first reaction chamber (8) is prevented.

11. Method according to one of the preceding claims, wherein the second reaction chamber is designed as a spiral tube which is in thermally conductive contact with at least one heating element, and the raw gas is heated in particular to up to 1500°C. 35218-P-WO Bg / so 05.03.202612. Method according to one of the preceding claims, wherein the cooling device comprises a first heat exchanger which has a cooling coil which runs at least partially through a water bath.

13. Method according to claim 11, wherein in process step E) the mixture is cooled such that the water of the water bath is at least partially evaporated and the water vapor (H2O) for process step C) is generated from it and in particular is supplied to the first reaction chamber (8).

14. Method according to one of the preceding claims, wherein the cooling device has at least one second heat exchanger, in particular a condensation heat exchanger, in which the proportion of water vapor (H2O) contained in the mixture (G) is at least partially condensed.

15. Device for producing a hydrogen-containing synthesis gas by means of a method according to any one of claims 1 to 14, comprising a first reaction chamber for receiving and burning a carbon-containing solid, wherein a steam line and in particular a line for supplying hot or cold air, or pure oxygen, open into the first reaction chamber, furthermore with a second reaction chamber which is connected to the first reaction chamber by means of a gas conductor and is in thermally conductive contact with one or more heating elements, preferably by means of electrically heated coils, furthermore, with a cooling device which is connected to the second reaction chamber via a gas conductor. 35218-P-WO Bg / so 05.03.2026

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