Reactor, plant, and method for producing synthesis gas and coke by thermochemical conversion of organic raw materials by means of steam
Patent Information
- Application Number
- PCT/EP2026/054118
- Authority / Receiving Office
- WO · WO
- Patent Type
- Applications
- Current Assignee / Owner
- Priority Date
- 2025-03-18
- Filing Date
- 2026-02-16
- Publication Date
- 2026-09-24
Smart Images
Figure EP2026054118_24092026_PF_FP_ABST
Abstract
Description
[0001] Reactor, plant and process for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam
[0002] The invention relates to a reactor for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, comprising a reactor chamber surrounding a reaction space, an inner reactor shell surrounding the reactor chamber and an outer reactor shell surrounding the inner reactor shell, wherein the reactor chamber comprises at least one material inlet opening, at least one fluid inlet opening, at least one material outlet opening and at least one fluid outlet opening.
[0003] The invention further relates to a plant for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, comprising at least one metering device, in particular a screw conveyor, for conveying and / or metering at least one organic raw material, at least one reactor for the thermochemical conversion of the organic raw material to raw synthesis gas and coke, at least one gas conditioning device for conditioning the raw synthesis gas to synthesis gas, and at least one steam generator device for generating steam, in particular superheated steam from water, wherein the steam can be introduced into the reactor and / or into the gas conditioning device.
[0004] Furthermore, the invention relates to a process for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, for a plant.
[0005] Various reactors for the production of synthesis gas and / or coke via thermochemical conversion are known in the prior art. Reactors of the type in question convert organic raw materials, in particular organic solids, liquids, or gases, with steam into combustible synthesis gas. The main components of the resulting synthesis gas are hydrogen (H₂), carbon monoxide (CO), carbon dioxide (CO₂), methane (CH₄), and steam. Inorganic components of the raw material, such as ash or slag, remain; if the raw material is not completely converted, coke is also produced. This type of thermochemical conversion is called gasification.
[0006] Some of the reactions involved in thermochemical conversion are exothermic. However, the overall gasification process is an endothermic conversion. Therefore, the conversion of the organic feedstock occurs exclusively with the input of heat of reaction. If the heat for the thermochemical conversion is supplied externally, the gasification is referred to as "allothermal." The heat can be introduced into the process, for example, through the reactor's outer walls or via a heat transfer medium, such as hot sand. Another possibility is the introduction of steam into the reactor, which serves as both the gasification medium and the energy carrier in the process. With the external input of heat of reaction, no fuel is burned in allothermal gasification. By using steam as the gasification medium, hydrogen-rich synthesis gas is simultaneously produced.
[0007] In general, the composition of the product gas is influenced by a multitude of factors during thermochemical conversion. This composition depends on the feedstock used, the gasification medium, the process parameters (temperature, pressure, and residence time of the organic feedstock in the reactor), the reactor design, and the heat input into the reaction chamber. These individual factors cannot be controlled independently; rather, they interact and affect the efficiency of the conversion process as well as the composition and purity of the synthesis gas.
[0008] A process for converting organic raw materials, particularly biomass, into fuels is known from US Patent 2011 / 0035990 A1. In a first process step, the raw materials are allothermally gasified in a gasification reactor using heated steam. The crude synthesis gas formed during the thermochemical conversion is purified in a second process step by reducing the temperature of the synthesis gas stream. This purification step separates particulate impurities and tars from the crude synthesis gas stream using a cyclone, and these impurities and tars are then recycled back into the gasifier.
[0009] From WO 01 / 21735 A1, a device and a method for the gasification of liquid or solid fuel are known. The device comprises a gasification reactor and a heating unit. The heating unit superheats steam and air, which are supplied to the gasification reactor as gasification media. The gasification reactor comprises a gasification zone and a reforming zone. In the gasification zone, a raw synthesis gas is produced from a liquid or solid feedstock by a thermal decomposition reaction. In the reforming zone, the raw synthesis gas is reformed in the presence of superheated steam, so that it is converted into synthesis gas. The steam reforming reaction of the liquid or solid fuel occurs through an exothermic reaction between the high-temperature air and the hydrocarbons contained in the thermally decomposed gas, as well as through an endothermic reaction between the hydrocarbons and the high-temperature steam.
[0010] US Patent 2017 / 066983 A1 discloses a plant for the production of synthesis gas for liquid fuels or chemical processes. The plant comprises multiple interconnected reactor stages to form a bioreforming reactor that produces synthesis gas from biomass for various chemical products. The first stage includes a circulating fluidized bed reactor with at least one feed for heat-absorbing media. The fluidized bed reactor also has a vessel for circulating the heat-absorbing media, at least one feedstock inlet, and a steam inlet. The first stage is configured to gasify the biomass into raw synthesis gas, which is discharged from the first stage via a reactor outlet. The fluidized bed of the reactor is operated with a superheated fluidizing gas mixture of steam, argon, and nitrogen.The raw synthesis gas is then chemically reacted in a second-stage cracking reactor to convert the raw synthesis gas from the first stage into a chemically pure synthesis gas. This is achieved by cracking the tars contained in the raw synthesis gas using catalysts and / or by introducing steam. The second stage is spatially separated from the first stage.
[0011] Despite a wide variety of designs, the reactors in question have disadvantages. After gasification, various long-chain hydrocarbons, especially tars, can be present in the synthesis gas as condensable components. These long-chain hydrocarbons are, on the one hand, volatile components inherent in the raw material. On the other hand, the thermochemical conversion process can thermally break down chemical compounds with larger molecular structures. During gasification, the tars are undesirable byproducts in the synthesis gas. They can condense when the synthesis gas cools after gasification, leading to blockages and clogging in technical plant components. Furthermore, depending on the raw material used, chlorine, nitrogen, and sulfur compounds can be formed.Overall, the formation of all these undesirable byproducts means that the synthesis gas requires extensive post-treatment in order to comply with environmental standards and process-specific requirements of downstream processes, such as chemical syntheses.
[0012] Furthermore, precise control of the reaction parameters during operation is required to ensure a uniform gas composition and high cold gas efficiency. In addition, reactors for solid organic feedstocks are particularly susceptible to slagging and deposits. Moreover, thermochemical conversion requires a high energy input.
[0013] The present invention is therefore based on the objective of designing and further developing a reactor, a plant and a process of the type mentioned above in such a way that the reactor, the plant and the process is more efficient, more flexible and easier to operate than conventional reactors, plants and processes compared to the prior art.
[0014] Furthermore, the reactor, the plant, and the process are intended to differ from competing products. The aforementioned problem is solved with regard to the reactor according to the invention by the features of claim 1. According to this claim, the reactor in question for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, comprises a reactor chamber surrounding a reaction space, an inner reactor casing surrounding the reactor chamber, and an outer reactor casing surrounding the inner reactor casing. The reactor chamber comprises at least one material inlet opening, at least one fluid inlet opening, at least one material outlet opening, and at least one fluid outlet opening.A flow channel is formed through at least a portion of the outer surface of the reactor chamber and at least a portion of the inner surface of the inner reactor casing, wherein the flow channel is designed such that steam from outside the reactor can be directed to the fluid inlet openings and the steam can be introduced into the reactor chamber via the fluid inlet opening. A space is formed through at least a portion of the outer surface of the inner reactor casing and at least a portion of the inner surface of the outer reactor casing, through which thermal energy provided by at least one heat source can be transferred to the inner reactor casing.
[0015] With regard to the plant, the preceding problem is solved by the features of dependent claim 9. The plant in question for the production of synthesis gas and / or coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, comprises at least one metering device, in particular a screw conveyor, for conveying and / or metering at least one organic raw material, at least one reactor according to any one of claims 1 to 8, for the thermochemical conversion of the organic raw material to raw synthesis gas and coke, at least one gas conditioning device for conditioning the raw synthesis gas to synthesis gas, and at least one steam generator device for generating steam, in particular superheated steam, from water, wherein the steam can be introduced into the reactor and / or into the gas conditioning device.The metering device is connected to at least one reactor in such a way that the organic raw material can be conveyed and / or metered into the reactor. The reactor is fluidically connected to the gas processing device.
[0016] With regard to the process, the foregoing problem is solved by the features of dependent claim 12. The process in question for the production of synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, for a plant according to any one of claims 9 to 11, comprises the process steps:
[0017] • drying of the organic raw material if necessary;
[0018] • Introducing the organic raw material into the reactor;
[0019] • Thermochemical conversion of the raw material in the reaction chamber to crude synthesis gas and / or coke with the addition of steam;
[0020] • Discharge of the generated raw synthesis gas and / or removal of the generated coke from the reactor; and
[0021] • Processing the raw synthesis gas into synthesis gas.
[0022] In accordance with the invention, it has first been recognized that the aforementioned problem is solved in a surprisingly simple way by cleverly designing the reactor.
[0023] Specifically, the reactor comprises a reactor chamber that encloses a reaction space. The reaction space is designed such that an organic feedstock can be thermochemically converted using steam by breaking down the feedstock's molecular structures with heat. The products formed during the thermochemical reaction are raw synthesis gas and coke. The organic feedstock can be introduced into the reactor chamber via at least one material inlet, and the steam via at least one fluid inlet. The coke produced can be discharged from the reactor chamber through at least one material outlet, and the raw synthesis gas produced through at least one fluid outlet. The material inlet and fluid inlet, and / or the material outlet and fluid outlet, can be configured as a single opening. The reactor chamber has an inner reactor casing surrounding it.A flow channel is formed between at least a portion of the outer surface of the reactor chamber, preferably the entire outer surface of the reactor chamber, and at least a portion of the inner surface of the inner reactor casing, preferably the entire inner surface of the inner reactor casing. The flow channel is designed to guide the steam between the outer surface of the reactor chamber and introduce it into the reactor chamber via at least one of the fluid inlet openings. Furthermore, a space is formed between at least a portion of the outer surface of the inner reactor casing, preferably the entire outer surface of the inner reactor casing, and at least a portion of the inner surface of the outer reactor casing, preferably the entire inner surface of the outer reactor casing. This space is designed to transfer thermal energy to the inner reactor casing.The thermal energy is provided by at least one heat source.
[0024] The heat required for thermochemical conversion is transferred via the flow channel into the reactor chamber or reaction chamber. This involves the transfer of thermal energy from the intermediate space through the inner reactor casing to the steam flowing in the flow channel. The steam stores the transferred heat. As it flows through the flow channel, the steam also transfers heat to the outer wall of the reactor chamber, which then conducts the heat into the reaction chamber. This allows for a simple and controlled heat input into the reaction chamber, thus enabling efficient thermochemical conversion.
[0025] The foregoing explanations make it clear that the claimed teaching provides a reactor that is more efficient, flexible, and easier to operate than conventional reactors compared to the prior art. Furthermore, the reactor differs from competing products.
[0026] For the purposes of the invention, the term "reaction space" is understood to mean a defined, enclosed area in which chemical and / or physical processes take place in a controlled environment. It serves to control process conditions and to carry out the conversion of substances in a targeted and safe manner. A reaction space is, for example, a closed system, in particular a chamber, or a zone within a system defined by process conditions.
[0027] The term "reactor cladding" is to be understood in the broadest sense in relation to the underlying invention. The term generally refers to an outer structure of any contour that completely or partially encloses the reactor chamber and, if applicable, at least one further reactor cladding. In particular, the reactor cladding has a form-fitting outer contour that accommodates the reactor chamber and, if applicable, at least one further reactor cladding from all sides.
[0028] For the purposes of the invention, the term "flow channel" is to be understood as a specifically designed flow area that directs the movement, in particular the direction, speed and / or pressure, of a fluid.
[0029] The term "heat source" is to be understood in the broadest sense in relation to the underlying invention. The term refers to a device that provides thermal energy through a chemical and / or physical process and releases it to its surroundings. Preferably, the heat source is an electric heating element, combustion heat, and / or waste heat. The heat can additionally or alternatively be provided indirectly via a heat transfer fluid, for example, steam, thermal oils, and / or liquid metals.
[0030] For the purposes of this invention, the term "thermochemical conversion" is to be understood in its broadest sense and describes the conversion of organic raw materials in a chemical reaction using thermal energy. In particular, the term refers to the gasification, preferably allothermal, of organic raw materials with the addition of steam as a gasifying agent and, optionally, as a heating agent.
[0031] The term "organic raw material" generally refers to any organic material containing the element carbon. This includes, in particular, carbon-containing raw materials of plant, animal, fossil, and / or industrial origin that are generated during industrial, agricultural, and / or private use. Examples of organic raw materials include fossil raw materials, especially lignite and hard coal; biogenic raw materials, especially wood, peat, grasses, and / or straw; as well as agricultural crop residues and / or biological residues, preferably compost, sewage sludge, digestate from biogas plants, straw, green waste and shrub clippings, and residues from food production, especially pomace, peels, bones, and / or dairy residues. Furthermore, the term includes synthetic carbon sources, especially plastics, preferably in single-material or blended forms.Ultimately, the term also includes organic waste streams from consumer goods, in particular packaging material, used textiles, bulky waste and household waste, waste paper and / or used tires.
[0032] For the purposes of the invention, organic raw materials are preferably solid or highly viscous raw materials or a suspension mixture comprising solid and liquid raw materials. The solid raw material is advantageously in bulk form, particularly as a powdery, granular, or lumpy mixture, preferably as granules or powder. Alternatively, the solid raw material can be in the form of pellets or wood chips. Highly viscous raw materials and / or suspension mixtures have a viscosity between 500 and 100,000 mPa s, depending on the composition and temperature.
[0033] The term "coke" describes the portion of organic raw material that has not been completely converted to the gaseous state during thermochemical conversion. Coke has a high carbon content of between 80% and 95% and an ash content of between 1% and 15%, both based on the total mass. After the production process, coke is porous and has a low density, specifically between 1.8 and 2.2 g / cm³. 3 .
[0034] In the context of the underlying invention, the term "crude synthesis gas" refers to a gaseous mixture that essentially comprises hydrogen (H2), carbon monoxide (CO), carbon dioxide (CO2), methane (CH4), and water vapor as components. Depending on the process, the crude synthesis gas contains undesirable byproducts from the gasification of the organic raw material. Such byproducts include, for example, particulate substances, especially soot and / or fly ash, long-chain hydrocarbons, especially tars, and / or impurities such as alkali, chlorine, nitrogen, and sulfur compounds.
[0035] The term "superheated steam" refers to gaseous water that has been heated above its normal boiling point in a steam generation unit. For this purpose, process water is heated to its normal boiling point of 100 °C by the addition of heat. The boiling liquid water is then isobarically vaporized and further heated in its vaporous state to the required process temperature. Temperatures up to 1500 °C are used in allothermal gasification.
[0036] Further features, advantages and further embodiments of the invention are described below or become apparent therein.
[0037] According to an advantageous embodiment of the invention, the reactor chamber and / or the inner reactor casing and / or the outer reactor casing have a cylindrical shape, wherein the reactor chamber comprises a reactor wall surrounding the reaction chamber, a first end wall closing off the reactor wall at one end of the reaction chamber, and a second end wall opposite the first end wall. One of the advantages achieved thereby is optimal flow guidance in the reactor chamber and improved mixing in the reaction chamber. Furthermore, the cylindrical shape improves heat transfer in the reactor chamber.
[0038] According to a further advantageous embodiment of the invention, the axial extent of the reactor chamber and / or the inner reactor casing and / or the outer reactor casing runs essentially parallel to a horizontal axis oriented at a 90° angle to the direction of gravity. One of the advantages achieved by this is improved process control, since the raw material is not moved by gravity within the reactor chamber and, in particular, is not compressed during thermal conversion in the reaction chamber by the introduction of new raw material. This enables improved raw material conversion. According to a further advantageous embodiment of the invention, the material inlet opening and / or the material outlet opening are arranged on the reactor wall. The advantage of this is simple manufacturing of the reactor and simple connection of the reactor to peripheral components, for example, conveying systems, dosing systems, and / or storage devices.
[0039] According to a further advantageous embodiment of the invention, the material outlet opening is arranged on the reactor wall offset from the material inlet opening by an angle of rotation about the longitudinal axis of the reactor chamber, in particular between 90° and 270°, preferably by 180°. This provides a space-saving design for the reactor and facilitates easy maintenance.
[0040] According to a further advantageous embodiment of the invention, the material inlet and outlet openings are arranged on the reactor wall in such a way as to enable axial flow guidance within the reactor chamber. Axial flow guidance is a directed movement of the material and / or fluid flows occurring in the reactor chamber in a main flow direction that runs essentially parallel to the axial extent of the reactor chamber. This minimizes pressure losses, improves flow efficiency in the reaction chamber, and reduces energy losses.
[0041] According to a further advantageous embodiment of the invention, the material inlet opening is formed in a region of the reactor wall extending along the axial extent of the reactor chamber between 0% and 50%, preferably between 0% and 25%, from the first end wall, and / or the material outlet opening is formed in a region of the reactor wall extending along the axial extent of the reactor chamber between 0% and 50%, preferably between 0% and 25%, from the second end wall. By positioning the material inlet opening and / or the material outlet opening on the reactor wall in a region near the end face of the reactor chamber, a reaction space is formed that, on the one hand, enables axial flow guidance and, on the other hand, exhibits less dead space in the end face of the reactor chamber. The advantage of this is improved raw material conversion.According to a further advantageous embodiment of the invention, a transfer system is arranged at the material inlet opening, the material outlet opening, the fluid inlet opening, and / or the fluid outlet opening, such that the reactor, in particular the reactor chamber, is a system sealed off from the environment. The term "transfer system" is to be understood in the broadest sense in relation to the underlying invention and generally refers to a technical device that enables the controlled transfer of materials, in particular organic raw materials and / or coke, and fluids, in particular water vapor and / or raw synthesis gas, from the environment into the reactor, preferably the reactor chamber, and / or from the reactor into the environment. The transfer system prevents the undesired exchange of substances between the reactor and the environment, in particular the uncontrolled entry and exit of gases, liquids, or particles into the reactor chamber.For example, a material airlock, preferably a two-chamber airlock, and / or a gas valve, preferably a check valve, constitutes such a transfer system. The transfer system may preferably include a drop chute configured as a connecting element between the transfer system and an upstream and / or downstream device, wherein the transfer system is designed such that the material to be transported can be conveyed through the transfer system by gravity. A transfer system seals the reactor chamber from the environment, thus providing a controlled reaction atmosphere within the reaction chamber. One of the advantages achieved thereby is an efficient and easy-to-operate reactor.
[0042] According to a further advantageous embodiment of the invention, a mechanical conveying system for transporting and / or metering solid and / or highly viscous raw materials and / or suspension mixtures, in particular screw conveyors, is arranged inside the reactor chamber, wherein the raw material is preferably transportable from the material inlet opening to the material outlet opening. The conveying system enables controlled material transport through the reactor chamber, in particular through the reaction chamber. Furthermore, the material transport improves mixing, leading to a homogeneous temperature distribution in the reaction chamber and among the substances participating in the reaction. The advantages of this are improved raw material conversion and an easy-to-operate reactor.
[0043] According to a further advantageous embodiment of the invention, the mechanical conveying system can be driven from outside the reactor chamber, in particular by at least one drive unit, preferably an electric motor. The conveying element that effects the material transport within the reactor chamber is arranged inside the reactor chamber, with the drive unit positioned outside. Consequently, the drive unit is not exposed to the high temperatures or the reaction atmosphere. This results in a reactor that is easy to maintain and has a long service life.
[0044] According to an advantageous embodiment of the invention, the fluid inlet opening comprises a flow control element for distributing water vapor in the reaction chamber. The term "flow control element" generally refers to a technical component that selectively influences the direction, velocity, pressure, or distribution of a fluid flow. The flow control element guides the fluid in a specific direction or to a specific point, regulates the flow parameters, reduces and / or generates targeted flow turbulence, and / or optimizes the energy transfer of the fluid flow, in particular the introduction of the fluid into the reaction chamber. Examples of flow control elements include nozzles, guide elements, and / or baffles. The advantage of a flow control element is the controlled introduction of energy, especially heat, and the gasification medium into the reaction chamber.
[0045] According to a further advantageous embodiment of the invention, the flow control element comprises a plurality of nozzles, which are preferably arranged uniformly distributed within the reactor chamber over its axial extent and / or circumference. The distribution of the water vapor in the reaction chamber and the targeted direction of the water vapor input onto the raw material to be processed result in improved raw material conversion.
[0046] According to a further advantageous embodiment of the invention, the flow channel forms an annular cross-section with an inner radius and an outer radius, wherein the inner radius and / or the outer radius is essentially the same along the axial extent of the flow channel. This provides a flow-optimized geometry in the flow channel, minimizing pressure losses. The advantage of this is an efficient reactor.
[0047] According to a further advantageous embodiment of the invention, at least one flow element for selectively influencing the flow dynamics of the fluid flowing through the flow channel and / or at least one heat transfer element for transferring heat from the outer reactor casing to the steam flowing through the flow channel and / or from the steam flowing through the flow channel to the inner reactor casing are arranged in the flow channel. A flow element is a technical component or geometric structure that selectively influences the course, velocity, or pressure of a fluid flow in the flow channel. Examples of flow elements are baffle plates, vortex generators, grids, and / or guide elements. A heat transfer element is a technical component or geometric structure that transports, stores, or distributes heat between the steam flowing in the flow channel and the reactor chamber.Heat transfer elements include, for example, metal plates, finned and / or needle structures, and / or fins. Preferably, a technical component or geometric structure is designed simultaneously as a flow element and as a heat transfer element. One of the advantages achieved through further development is improved heat transfer and more efficient flow guidance in the flow channel.
[0048] According to a further advantageous embodiment of the invention, the heat source is an electric heating element. This provides a simple and flexibly adjustable way to supply thermal energy for the thermochemical reaction.
[0049] According to a further advantageous embodiment of the invention, the reactor comprises thermal insulation, wherein the thermal insulation is arranged, in particular, on at least a portion of the outer surface of the outer reactor casing, preferably on the entire outer surface of the outer reactor casing. The material of the thermal insulation is, in particular, refractory bricks, preferably made of fireclay and / or silicon carbide, mineral insulating materials, ceramic fibers, polymer-based insulating materials, preferably made of polytetrafluoroethylene (PTFE), polyetheretherketone (PEEK) and / or polyimide (PA), and / or metallic insulating foams and / or films. In particular, the thermal insulation comprises a plurality of materials, which are preferably arranged in layers. The advantage is improved thermal management and a minimization of heat losses in the reactor.
[0050] According to a further advantageous embodiment of the invention, the reactor chamber and / or the inner reactor casing and / or the outer reactor casing are made of corrosion-, pressure- and / or temperature-resistant material and / or thermally conductive material, in particular metal, preferably stainless steel. This results in a longer service life, lower maintenance costs, increased safety and better efficiency of the reactor.
[0051] In one embodiment of the present invention, a plant for the production of synthesis gas and / or coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, comprises at least one metering device, in particular a screw conveyor, for conveying and / or metering at least one organic raw material, at least one reactor according to one of the preceding embodiments for the thermochemical conversion of the organic raw material to raw synthesis gas and coke, at least one gas conditioning device for conditioning the raw synthesis gas to synthesis gas, and at least one steam generator device for generating steam, in particular superheated steam, from water, wherein the steam can be introduced into the reactor and / or into the gas conditioning device.The metering device is connected to at least one reactor so that the organic raw material can be conveyed and / or metered into the reactor, and wherein the reactor is fluidically connected to the gas processing device.
[0052] In the thermochemical conversion of organic feedstock to synthesis gas and / or coke, the feedstock is conveyed via a metering device into a reactor connected to the metering device. In the reactor chamber, the feedstock is exposed to steam generated by a steam generator. The steam serves both as a gasifying agent and as a heat source for the endothermic thermochemical reaction. During thermochemical conversion, the molecular structures of the organic feedstock are broken down and converted into gaseous compounds, raw synthesis gas, and coke. Raw synthesis gas is the unprocessed product immediately after thermochemical conversion or upon exiting the reactor, and it contains undesirable byproducts.Such byproducts include, for example, particulate substances, long-chain hydrocarbons, especially tars, and / or impurities such as alkali, chlorine, nitrogen, and sulfur compounds. Only after processing, in particular purification and composition adjustment, does the raw synthesis gas become synthesis gas that can be used in downstream chemical processes. Processing in a gas processing unit comprises separating and / or converting the undesired byproducts contained in the raw synthesis gas. For this purpose, the gas processing unit is connected to the reactor fluidically, preferably via the shortest path, without the interposition of further devices and / or separation of components contained in the synthesis gas.The fluidic connection between the reactor and the gas processing device provides a system that enables efficient raw material conversion, easy operation, and high synthesis gas quality.
[0053] Preferably, the dosing device includes a feed container to compensate for discontinuous material input.
[0054] According to a further advantageous embodiment of the invention, the gas processing device comprises at least one cracking device for cracking, preferably thermally cracking, long-chain hydrocarbons, particularly tars, contained in raw synthesis gas. The term "cracking" is to be understood in the broadest sense in relation to the invention and generally describes the splitting of long-chain hydrocarbons, particularly tars, into shorter compounds, preferably into the synthesis gas components hydrogen (H2), carbon monoxide (CO), carbon dioxide (CO2), methane (CH4), and / or water vapor. Cracking preferably takes place non-catalytically with the input of thermal energy. This thermochemical conversion of the hydrocarbons is summarized under the term "thermal cracking" within the meaning of the invention. One of the advantages achieved with this embodiment is improved synthesis gas quality as well as increased plant efficiency.At the same time, the accumulation of by-products on plant components is avoided, so that the plant can be operated with less maintenance.
[0055] According to a further advantageous embodiment of the invention, the cracking device is designed as a continuous flow reactor, in particular a tubular reactor, preferably a coiled tube reactor. A continuous flow reactor is a type of chemical reactor in which the byproducts in the raw synthesis gas are cracked during flow. An advantage of continuous flow reactors is the simple and precise control of the reaction conditions, in particular temperature, pressure, and flow characteristics, to enable uniform and efficient cracking. A tubular reactor has a cylindrical flow path. In a coiled tube reactor, the flow path in the cracking device has a spiral or helical geometry. A coiled tube reactor offers high heat transfer rates, precise flow control, a compact design, and low-maintenance operation.
[0056] According to a further advantageous embodiment of the invention, the cracking device comprises at least one heating device, in particular an electric heating element. Upon introduction into the cracking device, the raw synthesis gas is heated to the temperature required for the thermal cracking of the long-chain hydrocarbons contained in the raw synthesis gas and decomposed, thereby substantially reducing the tar content in the raw synthesis gas. By reducing undesirable byproducts, the chemically bound energy in the synthesis gas is increased, and the deposition of byproducts on the plant components is prevented.
[0057] According to an advantageous embodiment of the invention, the gas processing device comprises at least one separation device for removing solid and / or liquid components from the raw synthesis gas. The separation device is, in particular, a separator for removing particulate substances and / or condensable components from the raw synthesis gas, preferably a centrifugal separator, and / or a condenser for removing condensate from the raw synthesis gas. The separation device removes unwanted byproducts based on differences in physical properties, especially density and boiling or dew point. The separation device thus represents a simple and effective method for processing the raw synthesis gas and improving its quality.
[0058] According to a further advantageous embodiment of the invention, the system comprises a product receiving device for cooling and / or storing the coke from the reactor. The coke can therefore be temporarily stored and cooled in its heated state before subsequent use. Cooling and temporarily storing the coke after the thermochemical reaction facilitates further processing, saves energy, and makes production more flexible. It consequently improves the efficiency of the system.
[0059] After intermediate storage, coke can be used as a valuable material, particularly as a soil improver, water reservoir, fertilizer depot in agriculture, carbon sink (to CO2 sink), activated carbon, and / or wastewater filter. Alternatively or additionally, coke can be used as an energy carrier, especially in gasification and / or partial oxidation, and / or as a reducing agent in metallurgical engineering. If the coke is converted to synthesis gases during gasification with a suitable gasifying agent, especially atmospheric oxygen, the heat energy generated as waste heat during this conversion can be fed back into the plant, for example, via the steam generator.
[0060] According to a further advantageous embodiment of the invention, the product receiving device comprises at least one heat transfer unit, in particular a heat transfer surface, for dissipating the heat. The thermal energy contained in the coke after discharge from the reactor can therefore be extracted from the coke and preferably used for the thermochemical conversion of the organic raw material. One of the advantages achieved thereby is an increase in the efficiency of the plant.
[0061] According to a further advantageous embodiment of the invention, the product receiving device comprises a product chamber for receiving the coke and a chamber shell surrounding the product chamber, wherein at least a portion of the outer surface of the product chamber, preferably the entire outer surface of the product chamber, and at least a portion of the inner surface of the chamber shell, preferably the entire inner surface of the chamber shell, form a cooling channel for a fluid, in particular water. This allows the thermal energy contained in the coke to be transferred during cooling to the fluid, in particular water, which is converted to steam, preferably superheated steam, in a steam generator. This minimizes heat loss in the system.
[0062] In one embodiment of the present invention, a process for producing synthesis gas and coke by thermochemical conversion of organic raw materials using steam, in particular superheated steam, for a plant according to one of the preceding embodiments comprises the following process steps:
[0063] • drying of the organic raw material if necessary;
[0064] • Introducing the organic raw material into the reactor;
[0065] • Thermochemical conversion of the raw material in the reaction chamber to crude synthesis gas and / or coke with the addition of steam;
[0066] • Discharge of the generated raw synthesis gas and / or removal of the generated coke from the reactor; and
[0067] • Processing the raw synthesis gas into synthesis gas.
[0068] In the thermochemical conversion of organic feedstock to synthesis gas and / or coke, the organic feedstock is introduced into the reactor. Specifically, the organic feedstock is dried to a certain moisture content before being introduced to reduce the energy required to heat it to the reaction temperature. Preferably, the energy for drying the organic feedstock is provided by waste heat generated during the process, for example, during the cooling of the synthesis gas and / or coke. The feedstock undergoes thermochemical conversion in the reactor chamber, particularly in the reaction chamber, with the addition of steam. The steam serves both as a gasifying agent and as a heat source for the endothermic thermochemical reaction in the reaction chamber.In thermochemical conversion, the molecular structures of the organic feedstock are broken down and converted into gaseous compounds, the raw synthesis gas, and coke. The resulting raw synthesis gas is then discharged from the reactor and / or the coke is removed. In a further process step, the raw synthesis gas is upgraded to synthesis gas by separating and / or converting the unwanted byproducts contained within it. This upgrade is achieved without the need for further intermediate process steps, as the reactor and the gas upgrading unit are directly connected, preferably via the shortest possible path. This provides a process that enables efficient feedstock conversion, ease of operation, and high synthesis gas quality.
[0069] According to a further advantageous embodiment of the invention, the processing of the raw synthesis gas to synthesis gas comprises the following process steps in succession:
[0070] • Cracking, preferably thermal cracking, of long-chain hydrocarbons in raw synthesis gas;
[0071] • Separation of particulate substances and / or liquid components from the raw synthesis gas;
[0072] • Cooling of the raw synthesis gas; and
[0073] • Separation of condensate.
[0074] The unwanted byproducts contained in the raw synthesis gas are converted or successively separated from the raw synthesis gas. In a first process step, the long-chain hydrocarbons, especially tars, are preferably thermally cracked. High cracking temperatures, particularly above 800 °C, preferably above 1000 °C, thermally crack the raw synthesis gas and convert it into the synthesis gas components hydrogen (H₂), carbon monoxide (CO), carbon dioxide (CO₂), methane (CH₄), and water vapor. In particular, the added water vapor, which remains unreacted in the reaction chamber, serves as a reactant for the cracking reactions. The higher the temperature used for thermal cracking, the fewer long-chain hydrocarbons are present in the synthesis gas after completion of this process step.In the second process step, particulate substances and / or liquid components are separated from the hot raw synthesis gas stream by means of a separator, in particular a centrifugal separator. In a third process step, the hot synthesis gas stream is cooled, in particular in stages via at least two heat exchangers, wherein the first heat exchanger is a gas-to-gas heat exchanger and the second heat exchanger is a condensing heat exchanger. Specifically, the raw synthesis gas is cooled to a temperature below the dew point of water, preferably less than 55 °C. Preferably, the cooling medium used in the gas-to-gas heat exchanger is steam, which enters the gas-to-gas heat exchanger at a temperature between 100 °C and 200 °C, preferably between 110 °C and 130 °C. The synthesis gas is cooled in the gas-to-gas heat exchanger to a temperature below 300 °C, preferably less than 200 °C.In particular, the steam is used for thermochemical conversion in the reactor. Preferably, water is used as the cooling medium in the condensation heat exchanger. In a fourth process step, the components that condense after cooling the raw synthesis gas, especially steam, are separated from the raw synthesis gas as condensate. Preferably, soluble gaseous components in the condensate, especially impurities such as alkali, chlorine, nitrogen, and / or sulfur compounds, are separated. After processing the raw synthesis gas, a high-calorific synthesis gas with high gas quality is obtained.
[0075] According to an advantageous embodiment of the invention, the coke discharged from the reactor is cooled and / or transported to the product receiving device and, if necessary, stored there. Cooling and intermediate storage of the coke after the thermochemical reaction facilitates further processing, saves energy, and makes production more flexible. This process step thus improves the efficiency of the plant.
[0076] Preferably, the coke is cooled directly after being discharged from the reactor and before entering the product receiving device. This is achieved, for example, by at least one cooling nozzle arranged in the transfer system, which preferably atomizes water. Additionally or alternatively, the heat energy of the coke can be dissipated via a heat transfer unit of the product receiving device and / or by the water flowing in the cooling channel between the product chamber and the chamber shell. Preferably, the water in the cooling channel is preheated to 100°C by the heat energy of the coke. The coke can then be temporarily stored in its cooled state for downstream use.
[0077] According to a further advantageous embodiment of the invention, water is evaporated to steam in a steam generator and optionally superheated to a temperature between 500°C and 1500°C, preferably between 800°C and 1400°C, and particularly preferably between 1000°C and 1300°C. Steam serves as a gasifying agent in the thermochemical conversion. Simultaneously, the introduction of steam provides thermal energy for the endothermic reaction into the reaction chamber. With a higher heat input into the reaction chamber, the organic raw material is converted more quickly and efficiently. Furthermore, fewer undesirable byproducts are formed during the thermochemical conversion, or these are broken down directly in the reaction chamber. One of the advantages achieved by this embodiment is faster and more efficient raw material conversion as well as improved gas quality.
[0078] According to a further advantageous embodiment of the invention, the water is preheated, in particular by heat removed from the coke and / or by heat removed from the raw synthesis gas. Preferably, the water in the cooling channel is preheated to 100°C by the heat energy of the coke. The advantage of this is a reduction in heat losses in the process, which makes it more efficient.
[0079] According to a further advantageous embodiment of the invention, the steam is superheated by heat removed from the raw synthesis gas and / or passed through the flow channel and superheated by the heat source and / or the reactor chamber. One of the advantages achieved thereby is a minimization of heat losses and consequently an increase in the efficiency of the process.
[0080] According to a further advantageous embodiment of the invention, the reaction chamber exhibits an isothermal, continuously decreasing, or continuously increasing temperature profile along its axial extent. The decreasing and / or increasing temperature profile is preferably continuous or stepped. This allows the process parameters in the reaction chamber to be individually adapted to the organic raw material, thereby increasing the efficiency of the raw material conversion and minimizing the production of undesirable byproducts.
[0081] According to a further advantageous embodiment of the invention, the thermochemical conversion takes place under increased pressure, in particular at an overpressure between 1 bar and 100 bar, preferably between 10 bar and 40 bar. Thermochemical conversion at increased pressure shifts the reaction equilibrium towards smaller molecules, thereby preferably resulting in the formation of the synthesis gas components hydrogen (H₂) and carbon monoxide (CO) during the thermochemical conversion. An advantage of this is improved gas quality in the process.
[0082] According to a further advantageous embodiment of the invention, the organic raw material is converted into coke with a carbon content between 80% and 95%, preferably between 85% and 90%. One of the advantages achieved thereby is improved raw material conversion and increased process efficiency.
[0083] There are now various ways to advantageously elaborate and further develop the teaching of the present invention. For this purpose, reference should be made, on the one hand, to the claims subordinate to claim 1 and, on the other hand, to the following explanation of preferred embodiments of the invention with reference to the drawings. In conjunction with the explanation of the preferred embodiments of the invention with reference to the drawings, generally preferred embodiments and further developments of the teaching are also explained. The drawings show
[0084] Fig. 1 is a schematic representation of a system according to an embodiment of the present invention; and
[0085] Fig. 2 shows an enlarged view of one reactor of the plant from Fig. 1.
[0086] In detail, Figure 1 shows a plant 1 for the production of synthesis gas 2 and coke 3 by thermochemical conversion of organic raw materials 4 using superheated steam 5, and Figure 2 shows an enlarged view of a reactor 10 of the plant 1 from Figure 1.
[0087] The system 1 comprises a metering device 6 with a screw conveyor 7 for conveying and / or metering preferably solid organic raw material 4. Upstream of the metering device 6 is a storage container 8 for receiving the organic raw material 4.
[0088] The dosing device 6 is connected to a reactor 10 via a transfer system 9. The transfer system 9 is designed as a two-chamber material lock with a first lock gate 9a and a second lock gate 9b. The transfer system 9 also includes a drop shaft 11 at both its upper and lower ends, which serve as connecting elements between the transfer system 9 and the upstream dosing device and the downstream reactor. The organic raw material 4 can be transported through the transfer system 9 by gravity.
[0089] The reactor 10 comprises a reactor chamber 13 surrounding a reaction space 12, an inner reactor casing 14 surrounding the reactor chamber 13, and an outer reactor casing 15 surrounding the inner reactor casing 14. The reactor chamber 13, the inner reactor casing 14, and the outer reactor casing 14 are essentially cylindrical in shape, with the axial extent of the reactor chamber 13, the inner reactor casing 14, and the outer reactor casing 15 running essentially parallel to a horizontal axis oriented at a 90° angle to the direction of gravity.
[0090] The reactor chamber 13 comprises a reactor wall 16 surrounding the reaction chamber 12, a first end wall 16a closing off the reactor wall 16 at one end of the reaction chamber 12, a second end wall 16b opposite the first end wall 16a, a material inlet opening 17, a fluid inlet opening 18, a material outlet opening 19, and a fluid outlet opening 20. The reaction chamber 12 is a closed system inside the reactor chamber 13. A flow channel 21 is formed between the outer surface of the reactor chamber 13 and the inner surface of the inner reactor casing 14. The flow channel 21 is suitable for guiding the steam 5 between the outer surface of the reactor chamber 13 and the inner surface of the inner reactor casing 14 and introducing it into the reactor chamber 13 via the fluid inlet opening 18.The flow channel 21 forms an annular cross-section with an inner radius and an outer radius, the inner and outer radii being essentially equal along the axial extent of the flow channel 21. Furthermore, a space 22 is formed between the outer surface of the inner reactor casing 14 and the inner surface of the outer reactor casing 15. The space 22 is designed to transfer thermal energy to the inner reactor casing 13. The thermal energy is provided by a heat source (not shown), preferably an electric heating element. The heat transfer occurs from the space 22 through the inner reactor casing 13 to the steam 5 flowing in the flow channel 21. The steam 5 stores the transferred thermal energy.On the other hand, as the water vapor 5 flows through the flow channel 21, it transfers heat to the reactor wall 16, which then conducts the heat into the reaction chamber 12.
[0091] The material inlet opening 17 and the material outlet opening 19 are arranged on the reactor wall 16. The material outlet opening 19 is offset from the material inlet opening 17 by a rotational angle of 180° around the longitudinal axis of the reactor chamber 13. The material inlet opening 17 is located in a region of the reactor wall 16 that extends along the axial extent of the reactor chamber 13 between 0% and 25% from the first end wall 16a. The material outlet opening 19 is located in a region of the reactor wall 16 that extends along the axial extent of the reactor chamber 13 between 0% and 25% from the second end wall 16b. This ensures axial flow guidance in the reactor chamber 13.
[0092] The material inlet opening 17 is connected to the transfer system 9, in particular to the drop chute 11. The material outlet opening 19 is also connected to a transfer system 23, in particular a two-chamber material airlock with a first airlock flap 23a and a second airlock flap 23b, via an airlock flap 11. The two transfer systems 9 and 23 prevent the undesired exchange of substances between the reactor 10 and the environment, in particular the uncontrolled escape and / or entry of gases, liquids, or particles into or out of the reactor chamber 13. The transfer systems 9 and 23 seal off the reactor chamber 13 from the environment, thus ensuring a controlled reaction atmosphere in the reaction chamber 12.
[0093] Inside the reactor chamber 13, a mechanical conveying system 24 for transporting and / or metering preferably solid materials is arranged in the form of a screw conveyor. This allows the organic raw material 4, introduced via the metering device 6, to be transported in a controlled manner from the material inlet opening 17 through the reaction chamber 12 to the material outlet opening 19. The conveying system 24 is operatively connected to an electric motor 24a, so that the conveying system 24 can be driven from outside the reactor chamber 13.
[0094] Furthermore, the plant 1 includes a gas processing unit for processing the crude synthesis gas 25 formed during the thermochemical reaction into synthesis gas 2. In this process, the undesired byproducts contained in the crude synthesis gas 25 are converted or successively separated from the crude synthesis gas 25. The gas processing unit connects directly to the reactor via a pipeline to the fluid outlet 20, in particular without the interposition of any further devices. The gas processing unit has a cracking device 26 for the thermal cracking of the long-chain hydrocarbons contained in the crude synthesis gas 25. The cracking device 26 is designed as a continuously flowing tube reactor 27. The thermal energy for cracking the hydrocarbons is provided by an electric heating element 28.High temperatures in the cracking device 26 thermally crack the raw synthesis gas 25 and convert it into the synthesis gas components hydrogen (H2), carbon monoxide (CO), carbon dioxide (CO2), methane (CH4), and water vapor. In particular, the water vapor 5 supplied, which remains unreacted in the reaction chamber 12, serves as a reactant for the cracking reactions. The higher the temperature selected for thermal cracking, the fewer long-chain hydrocarbons are present in the synthesis gas 2 after completion of the process step. Furthermore, the gas processing device includes a centrifugal separator 29 for separating solid and / or liquid components from the raw synthesis gas 25. Particulate substances, especially fly ash 30, and any liquid components are separated from the hot raw synthesis gas stream.
[0095] Furthermore, the gas processing device comprises a condenser 31 for separating condensate 32, in particular water vapor, from the raw synthesis gas 25 after cooling. The raw synthesis gas 25 is cooled by a gas-to-gas heat exchanger (not shown) before entering the condenser 31. In the condenser 31, the raw synthesis gas 25 is cooled to a temperature below the dew point of water 39, preferably less than 55 °C. The condensable components in the raw synthesis gas 25, in particular water vapor 5, are separated from the raw synthesis gas 25 as condensate 32 and collected in a collection tank 34. Preferably, gaseous components soluble in the condensate 32, in particular impurities 33 such as alkali, chlorine, nitrogen, and / or sulfur compounds, are separated simultaneously with the condensate 32.After the raw synthesis gas 25 exits the condenser 31, a high-calorific synthesis gas 2 without unwanted by-products is present.
[0096] Furthermore, the plant 1 includes a product receiving device 35 for cooling and storing the coke 3 from reactor 10. The product receiving device 35 comprises a product chamber 36 for receiving the coke 3 and a chamber shell 37 surrounding the product chamber 36, wherein the outer surface of the product chamber 36 and the inner surface of the chamber shell 37 form a cooling channel 38 for water 39. This allows the thermal energy contained in the coke 3 to be transferred to the water 39 during cooling.
[0097] Furthermore, the system 1 includes a steam generator 40 for generating superheated steam 5 from water 39. For this purpose, the water 39, preheated in the product receiving device 35, is introduced into the steam generator 40 via a line 41 and evaporated. Subsequently, the steam 5 is directed into the reactor 10 via a steam channel 42. The steam channel 42 is fluidically connected to the flow channel 21. The steam 5 is passed through the flow channel 21 and superheated by the heat source and the reactor chamber 13. The flow channel 21 is fluidically connected to the fluid inlet opening 18. The fluid inlet opening includes a flow control element 43 for distributing the water vapor 5 in the reaction chamber 12. The flow control element 43 is formed from a plurality of nozzles which are arranged evenly distributed inside the reactor chamber 13 over the axial extent of the reactor chamber 13.
[0098] Regarding further advantageous embodiments of the reactor, the plant and the method according to the invention, reference is made to the general part of the description and to the attached claims to avoid repetition.
[0099] Finally, it should be expressly noted that the exemplary embodiments of the reactor, the plant, and the method according to the invention described above serve only to illustrate the claimed teaching and do not limit it to these exemplary embodiments.
[0100] 1 Annex
[0101] 2 Synthesis gas
[0102] 3 coke
[0103] 4 Organic raw material
[0104] 5 Water vapor
[0105] 6 Dosing device
[0106] 7 auger
[0107] 8 storage containers
[0108] 9 transfer system
[0109] 9a First lock gate
[0110] 9b Second lock gate
[0111] 10 Reactor
[0112] 11 Drop shaft
[0113] 12 reaction chamber
[0114] 13 Reactor chamber
[0115] 14 Inner reactor casing 15 Outer reactor casing 16 Reactor wall
[0116] 6a First end wall
[0117] 6b Second front wall
[0118] 17 Matenal entrance opening
[0119] 18 Fluid inlet opening
[0120] 19 Material outlet opening 20 Fluid outlet opening
[0121] 21 Flow channel
[0122] 22 space
[0123] 23 Transfer system
[0124] 3a First lock gate
[0125] 3b Second lock gate 24 Conveyor system
[0126] 4a Motor
[0127] 25 Raw synthesis gas splitting device Tube firing reactor Electric heating element Centrifugal separator Fly ash
[0128] capacitor
[0129] condensate
[0130] Contamination Collection Container Product Receiving Device Product Chamber Chamber Shell
[0131] Cooling channel
[0132] Water steam generator device line
[0133] Steam channel
[0134] Flow control element
Claims
Claims 1. Reactor for the production of synthesis gas (2) and coke (3) by thermochemical conversion of organic raw materials (4) using steam (5), in particular superheated steam (5), comprising a reactor chamber (13) surrounding a reaction space (12), an inner reactor shell (14) surrounding the reactor chamber (13) and an outer reactor shell (15) surrounding the inner reactor shell (14), wherein the reactor chamber (13) comprises at least one material inlet opening (17), at least one fluid inlet opening (18), at least one material outlet opening (19) and at least one fluid outlet opening (20), characterized in that a flow channel (21) is formed through at least a part of the outer surface of the reactor chamber (13) and at least a part of the inner surface of the inner reactor shell (14), wherein the flow channel (21) is designed such that the water vapor (5) can be directed from outside the reactor to the fluid inlet openings (18) and the water vapor (5) can be introduced into the reactor chamber via the fluid inlet opening (18), and wherein an intermediate space (22) is formed through at least a part of the outer surface of the inner reactor shell (14) and at least a part of the inner surface of the outer reactor shell (15), whereby thermal energy provided by at least one heat source can be transferred to the inner reactor shell (14).
2. Reactor according to claim 1, characterized in that the reactor chamber (13) and / or the inner reactor casing (14) and / or the outer reactor casing (15) have a cylindrical shape, wherein the reactor chamber (13) comprises a reactor wall (16) surrounding the reaction space (12), a first end wall (16a) closing off the reactor wall (16) at one end of the reaction space (12), and a second end wall (16b) opposite the first end wall, wherein preferably the axial extent of the reactor chamber (13) and / or the inner reactor casing (14) and / or the outer reactor casing (15) runs substantially parallel to a horizontal axis oriented at a 90° angle to the direction of action of gravity. 3.Reactor according to claim 2, characterized in that the material inlet opening (17) and / or the material outlet opening (19) are arranged on the reactor wall, wherein the material outlet opening (19) is preferably arranged on the reactor wall (16) offset by an angle of rotation about the longitudinal axis of the reactor chamber (13), in particular between 90° and 270°, preferably by 180°, from the material inlet opening (17).
4. Reactor according to claim 3, characterized in that the material inlet opening (17) and the material outlet opening (19) are arranged on the reactor wall (16) such that they enable axial flow guidance in the reactor chamber (13), wherein the material inlet opening (17) is preferably formed in a region of the reactor wall (16) which extends along the axial extent of the reactor chamber (13) between 0% and 50%, preferably between 0% and 25%, from the first end wall (16a) and / or that the material outlet opening (19) is formed in a region of the reactor wall (16) which extends along the axial extent of the reactor chamber (13) between 0% and 50%, preferably between 0% and 25%, from the second end wall (16b).
5. Reactor according to one of claims 1 to 4, characterized in that a transfer system (9, 23) is arranged at the material inlet opening (17), at the material outlet opening (19), at the fluid inlet opening (17) and / or at the fluid outlet opening (20), so that the reactor (10), in particular the reactor chamber (13), is a system closed off from the environment.
6. Reactor according to one of claims 1 to 5, characterized in that a mechanical conveying system (24) for transporting and / or metering solid and / or semi-liquid materials, in particular screw conveyors, is arranged inside the reactor chamber (13), wherein the material is preferably transportable from the material inlet opening (17) to the material outlet opening (18), wherein the mechanical conveying system (24) is preferably driveable from outside the reactor chamber (13), in particular with at least one drive unit, preferably an electric motor (24a). 7.Reactor according to one of claims 1 to 6, characterized in that the fluid inlet opening (18) comprises a flow control element (43) for distributing the water vapor (5) in the reaction chamber (13), wherein the flow control element (43) preferably comprises a plurality of nozzles which are arranged inside the reactor chamber (13) preferably uniformly distributed over the axial extent and / or over the circumference.
8. Reactor according to one of claims 1 to 7, characterized in that the flow channel (21) forms an annular cross-section with an inner radius and an outer radius, wherein the inner radius and / or the outer radius is substantially the same along the axial extent of the flow channel (21) and / or that at least one flow element for selectively influencing the flow dynamics of the fluid flowing through the flow channel (21) and / or at least one heat transfer element for transferring heat from the outer reactor shell (15) to the steam (5) flowing through the flow channel (21) and / or from the steam (5) flowing through the flow channel (21) to the inner reactor shell (14) are arranged in the flow channel (21).
9. Plant for the production of synthesis gas (2) and coke (3) by thermochemical conversion of organic raw materials (4) using steam (5), in particular superheated steam (5), comprising: • at least one metering device (6), in particular a screw conveyor, for conveying and / or metering at least one organic raw material (4); • at least one reactor (10) according to one of claims 1 to 8 for the thermochemical conversion of the organic raw material (4) to crude synthesis gas (25) and coke (3); • at least one gas processing device for processing the crude synthesis gas (25) into synthesis gas (3); and • at least one steam generator device (40) for generating steam (5), in particular superheated steam (5) from water (39), wherein the steam (5) can be introduced into the reactor (10) and / or into the gas conditioning device; wherein the metering device (6) is connected to at least one reactor (10) so that the organic raw material (4) can be conveyed and / or metered into the reactor (10), and wherein the reactor (10) is fluidically connected to the gas processing device.
10. Plant according to claim 9, characterized in that the gas processing device comprises at least one cracking device (26) for cracking, preferably thermal cracking, long-chain hydrocarbons, in particular tars, contained in raw synthesis gas (25), wherein the cracking device (26) is preferably designed as a continuous flow reactor, in particular a tubular reactor, preferably a tube-driven reactor (27), and / or that the gas processing device comprises at least one separation device for separating solid and / or liquid components from the raw synthesis gas (25), wherein the separation device is in particular a separator for separating particulate substances and / or condensable components from the raw synthesis gas, preferably a centrifugal separator (29), and / or a condenser (31) for separating condensate (32) from the raw synthesis gas (25).
11. Plant according to claim 9 or 10, characterized in that the plant comprises a product receiving device (35) for cooling and / or storing the coke (3) from the reactor (10), wherein the product receiving device (35) preferably comprises a product chamber (36) for receiving the coke (3) and a chamber shell (37) surrounding the product chamber (36), wherein at least a part of the outer surface of the product chamber (36) and at least a part of the inner surface of the chamber shell (37) form a cooling channel (38) for a fluid, in particular water (39).
12. Process for the production of synthesis gas (2) and coke (3) by thermochemical conversion of organic raw materials (4) using steam (5), in particular superheated steam (5), for a plant (1) according to one of claims 9 to 11, comprising the process steps: • if necessary, drying of the organic raw material (5); • Introducing the organic raw material (4) into the reactor (10); • Thermochemical conversion of the organic raw material (4) in the reaction chamber (12) to crude synthesis gas (25) and coke (3) with the addition of steam (5); discharge of the crude synthesis gas (25) formed and / or discharge of the coke (3) formed from the reactor (10); and Processing the raw synthesis gas (25) to synthesis gas (2).
13. The method according to claim 12, characterized in that the processing of the crude synthesis gas (25) to synthesis gas (2) comprises the following successive process steps: • Cracking, preferably thermal cracking, of long-chain hydrocarbons in raw synthesis gas (25); • Separation of particulate substances and / or liquid components from the raw synthesis gas (25); • Cooling of the crude synthesis gas (25); and • Separation of the condensate (32).
14. Method according to claim 12 or 13, characterized in that the coke (3) discharged from the reactor (10) is cooled and / or transported into the product receiving device (35) and optionally stored in the product receiving device (35).