Method for producing synthesis gas from waste products by combining gasification and reforming reactions under heat energy recovery conditions

Abstract

The invention relates to a method and a device for producing synthesis gas from at least one waste product by combining a gasification reaction with a reforming reaction under heat energy recovery conditions. The method comprises the step S1 of feeding a feed material, in particular comprising at least one waste product in solid, liquid and / or gaseous state, as well as a first oxidizing agent and / or a second oxidizing agent into a gasification reactor. Furthermore, the method comprises the step S2 of gasifying the feed material by means of the first oxidizing agent and / or the second oxidizing agent in the gasification reactor to a hydrocarbon gas mixture and at least one by-product, in particular comprising bottom ash and / or fly ash, under input of heat energy. The method further comprises the step S3 of feeding the hydrocarbon gas mixture from the gasification reactor into a reformer unit, and the step S4 of processing the hydrocarbon gas mixture into a raw synthesis gas in the reformer unit under addition of the first oxidizing agent and / or the second oxidizing agent.

Description

Technical Field

[0001] This invention relates to a method and apparatus for producing syngas from waste products by combining gasification and reforming reactions under heat energy recovery conditions. Background Technology

[0002] Currently, large-scale production of fossil-based syngas is typically carried out in energy-intensive processes such as natural gas reforming or coal gasification. Here, syngas is defined as a gaseous mixture consisting of carbon monoxide (CO) and hydrogen (H2). However, various novel methods currently used for syngas production still have shortcomings.

[0003] For example, in biogas reforming, syngas is produced in a decentralized manner, resulting in high costs due to small-scale equipment, high investment and operating costs, and inefficient logistics. This leads to syngas prices being significantly higher than natural gas prices.

[0004] The method of using electrolysis combined with water-gas shift reaction or co-electrolysis requires extremely high electrical energy consumption and has low energy efficiency, which in turn leads to high prices for the syngas produced.

[0005] The thermally driven waste-to-syngas process utilizes the oxidation and combustion of a portion of waste feedstock to provide the energy required for the thermal reforming process to produce syngas. This results in significant carbon dioxide emissions, which cannot be effectively utilized in subsequent processes.

[0006] In the thermal treatment process for producing syngas from waste feedstock, it is known that carbonaceous waste materials are converted into syngas by adding oxidants such as oxygen or water vapor, where a gasification process is first carried out. The gaseous fractions produced during gasification have different chain lengths. A portion of these is condensed and sold as a substitute for crude oil. The gaseous fractions, after gasification, can be used to generate heat and electricity. However, from an economic perspective for industrial applications, the requirements for each fraction and the composition of the waste products used are very high. Therefore, existing gasification equipment is limited by being specifically customized for the type or different purity of the waste products. Furthermore, valuable byproducts generated during gasification (such as various types of ash, such as bottom ash, fly ash, or pool ash) cannot be further utilized. Additionally, potential fluctuations in the waste product input are detrimental to the safe and gentle operation of the gasification reactor. This also increases the difficulty of providing a stable supply of hydrocarbon gas mixture product streams.

[0007] Furthermore, methods for upgrading unpurified crude gas through reforming are known, which convert hydrocarbon-containing gas mixtures into hydrogen-rich syngas with pollutants removed. However, these methods still lack the recycling of substances already used in waste management. In known reforming processes, hydrocarbon mixtures such as natural gas, light gasoline, methanol, or even biomass are used as feedstocks and reformed into syngas along with oxidants (such as steam) while consuming thermal energy.

[0008] Overall, known methods exhibit high energy consumption throughout the process chain, from primary energy carrier to final product, making potential electrification uneconomical. This can be explained by significant waste heat loss, unconsumed feedstock, or unconsumed oxidant. Non-electric methods using waste, due to the use of oxygen or air as oxidant, result in the generation and subsequent emission of carbon dioxide, a pollutant. This, in turn, leads to a reduction in syngas quality. Summary of the Invention

[0009] Based on known background technology, one object of the present invention is to provide an improved method and corresponding apparatus for producing syngas from waste products by combining gasification reaction with reforming reaction under heat energy recovery conditions.

[0010] In this regard, improving energy efficiency and minimizing byproducts are of paramount importance. Therefore, one object of the present invention is to provide an improved method and system for producing syngas from waste products, which aims to effectively utilize waste and minimize energy consumption.

[0011] This objective is achieved by the method according to claim 1. Advantageous extensions are derived from the dependent claims, description, and drawings.

[0012] Accordingly, a method for producing syngas from at least one waste product by combining a gasification reaction with a reforming reaction under heat energy recovery conditions is proposed. The method includes a first step S1 of feeding a feedstock and a first oxidant and / or a second oxidant into a gasification reactor, wherein the feedstock specifically comprises at least one solid, liquid, and / or gaseous waste product. Furthermore, the method includes a second step S2 of gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct in the gasification reactor using the first oxidant and / or the second oxidant, with the input of heat energy, wherein the byproduct specifically comprises bottom ash and / or fly ash. The method further includes a third step S3 of feeding the hydrocarbon gas mixture from the gasification reactor to a reformer unit, and a fourth step S4 of processing the hydrocarbon gas mixture into crude syngas in the reformer unit with the addition of the first oxidant and / or the second oxidant, wherein at least a portion of the heat energy released in step S4 is fed back to the gasification reactor to provide at least a portion of the heat energy input in the second step S2.

[0013] In this document, the term "waste product" should be understood as the reactants used in the method for producing syngas. Generally, suitable reactants refer to substances that are generated as waste products in previous processes. However, the latter is not a necessary prerequisite for the application of this syngas preparation method. Therefore, the term "waste product" in this document also includes reactants that are not actually extracted from waste but are specifically prepared.

[0014] Herein, waste products are specifically understood as carbonaceous substances, particularly methane, propane, biogas, plastics, residual waste, wood waste, biomass, lignin and / or paper waste, or mixtures of substances containing the above, which, among other sources, are produced as residues, by-products and / or associated products from prior processes (particularly pyrolysis, recycling and / or Fischer-Tropsch synthesis).

[0015] Coupling the reformer unit with the upstream gasification reactor enables the production of high-quality syngas from a variety of waste products. Utilizing waste products promotes a sustainable circular economy and reduces the demand for valuable hydrocarbon feedstocks used in syngas production. Using waste products as feedstock helps reduce landfill waste and supports sustainable resource utilization. Simultaneously, it reduces the demand for fossil resources. The feed material can be fed from a dedicated waste material container, which serves as an intermediate storage and balances supply bottlenecks or fluctuations. This ensures smooth operation of the equipment and continuous production of high-quality syngas. Therefore, continuous full-load operation of the equipment and a stable output of the syngas product stream can be ensured. Furthermore, liquid and / or gaseous substances can be added to the process. If only liquid substances are used, an evaporator can be used instead of the gasification reactor. Dividing syngas production into four steps reduces the requirements for feed materials and leads to a wider applicability of syngas. Another advantage is that solid plastic waste can be added as feedstock to the method, which would otherwise have to be treated separately and in isolation during further waste treatment due to its interfering chemical properties. The use of a first oxidant and / or a second oxidant (which are fed into the gasification reactor in a variable mixing ratio) enables precise control of gasification conditions, such as reaction temperature and the products generated. This allows for targeted adjustments to the composition of the syngas. Furthermore, precise control of gasification and reforming conditions is possible. This improves the adaptability of the method to different feedstock and product requirements. The process of gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct in step S2 constitutes the initial preparation step for producing syngas from the feedstock. Gasification is an endothermic reaction. During gasification, the fed carbon-containing energy carrier is converted into a gaseous hydrocarbon gas mixture and byproducts through chemical transformation under the input of thermal energy. This gasification is specifically carried out at a temperature of 400 to 650°C. By feeding heat energy back from the reformer unit to the gasification reactor, the external energy requirement for gasification in step S2 is reduced, and the overall energy efficiency of the method is improved. This results in a cost-effective and sustainable process design. Furthermore, the heat energy feedback allows for a uniform supply of heat energy to the gasification reactor, thereby minimizing fluctuations in energy input and achieving stable syngas production.

[0016] To produce crude syngas, the hydrocarbon gas mixture is directed to a reformer unit in step S3. Subsequently, the hydrocarbon gas mixture is processed in the reformer unit in step S4, resulting in the crude syngas obtained upon the addition of a first oxidant and / or a second oxidant. The syngas produced in step S4 has a purity suitable for a variety of applications, such as chemical synthesis.

[0017] In the fourth step S4, a portion of the heat energy present in the crude syngas is extracted and fed back into the gasification reactor. This fed-back heat energy provides a portion of the heat energy required in S2, which in turn improves the energy efficiency of the method.

[0018] In an alternative embodiment, the method includes a first step S1 of feeding a substantially or solely gaseous feedstock into a reformer unit, wherein the gaseous feedstock comprises a hydrocarbon gas mixture. Furthermore, the method includes a subsequent step S4, in which the substantially or solely gaseous feedstock is processed into crude syngas in the reformer unit, with the addition of a first oxidant and / or a second oxidant, and wherein at least a portion of the heat energy released in step S4 is recycled.

[0019] In another preferred embodiment of the method, step S4, which processes the hydrocarbon gas mixture in the reformer unit, includes, in addition to reforming the hydrocarbon gas mixture into crude syngas in a plasma reformer, at least the following steps: step S44, wherein step S44 includes cooling the syngas; step S444, wherein step S444 includes adjusting the temperature of the crude syngas in a hot residence chamber to improve the reaction yield; and step S4444, wherein step S4444 includes quenching the crude syngas in a cooling zone.

[0020] In step S44, the cooling of the syngas can be performed via a heat exchanger, which can return the heat energy to the entire system via a heat transfer medium. Utilizing the heat energy released during the cooling of the crude syngas improves the energy efficiency of the method. Positioning the heat exchanger between the hot residence chamber and the cooling zone maximizes the utilization of waste heat from the nearby plasma reformer and the heat energy of the produced syngas without adversely affecting the reaction in the overall system. Temperature regulation in the hot residence chamber in step S444 improves reaction yield, destroys contaminants present in the gas, and controls the product composition of the crude syngas. Here, only a small amount of heat energy is needed in the hot residence chamber to maintain the temperature of the crude syngas. In step S4444, the crude syngas is quenched in the cooling zone, rapidly reducing its temperature. Here, the heat energy present in the crude syngas is rapidly extracted. Therefore, no undesirable further reactions occur in the gas. Water cooling via jet cooling is a cost-effective option. Another advantage is that water cooling does not impair the quality of the syngas.

[0021] In another preferred embodiment of the method, a portion of the energy released in step S4 is fed back into the gasification reactor via a first oxidant and / or a second oxidant, which serve as heat transfer media.

[0022] The energy released in step S4 is selectively fed back into the gasification reactor via a first oxidant and / or a second oxidant, significantly improving the efficiency of the method. This integration optimizes the use of thermal energy, thereby further reducing external energy requirements. Furthermore, the feedback via the oxidant allows for more flexible control of the gasification process, as the input energy can be precisely metered and uniformly distributed. This design not only improves process stability but also allows for finer adjustments to reaction conditions, contributing to the production of uniform and high-quality syngas.

[0023] In another preferred embodiment of the method, in order to recover heat energy, the recovered first oxidant and / or second oxidant is heated via a heat exchanger (particularly via a radiant heat exchanger or a ceramic heat exchanger located between the hot residence chamber and the cooling zone).

[0024] Post-treatment of the returned first and / or second oxidant via a heat exchanger provides the advantage of effectively post-treating the returned first and / or second oxidant, thereby optimizing its quality and reactivity for the gasification process. The use of a heat exchanger (e.g., an evaporator such as a radiant heat exchanger or a ceramic heat exchanger) ensures efficient heat transfer from the hot residence chamber or the cooling zone. Consequently, the thermal energy from the process is further utilized efficiently, improving energy efficiency and reducing the overall energy demand of the method. Furthermore, the post-treatment in the heat exchanger ensures uniform conditioning of the oxidant, enabling stable and controlled reactions in the gasification reactor. This contributes to improved process stability, uniform syngas quality, and extended service life of process components.

[0025] In an extended embodiment of the method, the return of thermal energy is carried out via a heat exchanger located between the hot residence chamber and the cooling zone, wherein the heat exchanger heats the medium in the intermediate loop, and wherein the medium then releases the heat to at least one heat sink via at least one second heat exchanger, wherein the at least one heat sink comprises a heat sink having a first oxidant and / or a second oxidant flow.

[0026] Using an intermediate loop filled with a heat transfer medium to transfer waste heat from the plasma reformer to the oxidant stream offers the advantage of lower losses when the waste heat loop and oxidant loop may be located far apart. Furthermore, the risk of contamination between the two loops is also lower. The temperature levels of the oxidant loop and waste heat loop can be freely adjusted via the intermediate loop. This eliminates the possibility of damage to the heat exchanger due to excessive temperature. Additionally, it allows for the release of process heat to other energy-consuming equipment.

[0027] In an extended embodiment of the method, at least one superheater is included between the heat exchanger and the gasification reactor.

[0028] By using at least one superheater between the heat exchanger and the gasification reactor, the first oxidant and / or the second oxidant can be further heated, specifically to 650°C, to further increase the heat input to the gasification reactor via the first oxidant and / or the second oxidant. This, in turn, reduces the primary energy requirement of the gasification reactor and reflects an improvement in the overall process efficiency. Furthermore, at least one superheater is used to control the gasification conditions to adjust the quantity and component ratio of the generated hydrocarbon gas mixture.

[0029] In another preferred embodiment of the method, at least a portion of the post-treated first oxidant and / or second oxidant accelerates process step S2.

[0030] The targeted use of the treated first and / or second oxidants improves the reaction rate and efficiency of the gasification process, thereby enabling a faster and more complete conversion of the feedstock into a hydrocarbon gas mixture. This is due, in addition to the heat input, to the faster removal of reaction products from the gasification reactor. This not only increases the productivity of the method but also improves energy utilization and the consistency of syngas quality. Furthermore, the accelerated reaction allows for a reduction in residence time in the gasification reactor, resulting in higher throughput and more efficient use of equipment resources.

[0031] In another preferred embodiment, the method includes separating the bottom ash generated during gasification in step S2, and includes at least partially separating the fly ash generated during conversion and carried by the hydrocarbon gas mixture, and returning it to the gasification reactor, wherein, preferably, the separation further includes separating the bottom ash via an ash removal system, wherein, preferably, the separation and return step includes separating the fly ash in the hydrocarbon gas mixture after gasification via an ash collector (particularly via a cyclone separator).

[0032] Ash types such as bottom ash or fly ash are generated as byproducts during gasification. Due to the high reaction temperatures in the gasification reactor, these byproducts also have high medium temperatures, which helps maintain high temperature levels during gasification when they are separated and returned to the reactor. Separating and returning these high-temperature byproducts helps improve the purity of the final gasification product and increases the energy efficiency of the overall process.

[0033] The ash removal system for separating the bottom ash ensures continuous and trouble-free operation of the gasification reactor by preventing sedimentation and clogging. This system enables efficient and controlled discharge of byproducts, thereby maintaining stable operating conditions and extending equipment lifespan. Furthermore, separating the bottom ash facilitates its further utilization or environmentally friendly treatment. This contributes to improved sustainability of the entire process, as valuable resources can be recovered or waste can be professionally treated. Additionally, the ash removal system can reintroduce the separated bottom ash into the gasification reactor for reuse at the high temperature levels during gasification.

[0034] Fly ash particles generated during gasification can be extracted from the final product of the hydrocarbon gas mixture using ash collectors (such as cyclone separators) or other filtration methods. Effective removal of fly ash improves the purity of the hydrocarbon gas mixture, which in turn improves the quality of the syngas produced. This benefits the purity of the hydrocarbon gas mixture for further processing and also allows for the potential further utilization of normally unwanted byproducts. The use of cyclone separators enables reliable and mechanically robust particle separation, even at high temperatures and flow rates, thereby improving process stability. Furthermore, targeted separation and recirculation of fly ash prevents potential deposition in downstream components, reducing maintenance costs and extending equipment life. Fly ash recirculation also allows for further utilization of residues, improving the resource efficiency of the method and contributing to minimizing waste. Moreover, separating and recirculating fly ash present in the hydrocarbon gas mixture stream before the plasma reformer is intended to utilize byproducts to improve the overall energy efficiency of the process. Here, the high temperature level of fly ash in the gasification reactor is utilized to reduce the high energy consumption required to heat it to the reaction temperature there.

[0035] In another preferred embodiment of the method, the component ratio of hydrogen (H2) and carbon monoxide (CO) in the synthesis gas is adjusted by the mixing ratio of the first oxidant and the second oxidant.

[0036] The ratio of hydrogen to carbon monoxide in the syngas (also known as the syngas ratio) is controlled by adjusting the mixing ratio of the oxidant fed into the gasification reactor and reformer unit. Here, the syngas ratio can be adjusted via the mixing ratio of steam and CO2. This allows for variable adjustment of the syngas composition and quality, thereby ensuring a constant product quality. A constant oxidant mixing ratio would hinder adjustments to the system due to fluctuations in the feed composition. In existing mature processes, the CO and H2 mixing ratio is set via a water-gas shift reaction. This is not necessary in this paper, which in turn saves resources and improves the overall system energy efficiency. The syngas ratio is adjusted via the oxidant mixing ratio by using non-catalytic (i.e., thermal or plasma-based) reforming in step S4.

[0037] In another preferred embodiment of the method, the method includes, after step S4, cooling the crude syngas in a condenser unit and separating the condensate.

[0038] This cooling step in the condenser unit is used to process the crude syngas to separate dust particles, salts, volatile heavy metals, and residual vapors that may still be present in the crude syngas stream.

[0039] The separated substances are ultimately removed from the syngas stream via condensate, thus producing purified syngas. Furthermore, targeted temperature reduction allows for optimized processing of the syngas for subsequent steps, which in turn improves the efficiency and flexibility of the method. Separating the condensate additionally enables the removal of unwanted byproducts, such as water or condensable compounds, thereby improving the purity and quality of the syngas. Moreover, the condenser unit facilitates effective heat recovery by extracting excess heat from the gas stream, improving the overall energy efficiency of the process. This integration also minimizes the workload required for downstream gas purification.

[0040] In another preferred embodiment of the method, the operating pressure of the gasification reactor and the operating pressure of the plasma reactor are between 1 bar and 20 bar absolute pressures, preferably between 1.5 bar and 4 bar absolute pressures.

[0041] The required operating pressure in the reactor for this method is between 1 bar and 20 bar absolute pressure to achieve high syngas reaction yields and enable gasification and reforming reaction steps. Alternatively, the operating pressure in the reactor can be set between 1.5 and 4 bar absolute pressure. Furthermore, the various process steps are carried out substantially isobarically. Here, the compressor must also perform less work, resulting in lower energy consumption. Moreover, low-pressure piping can be used within this moderate pressure range, which constitutes a lower cost factor compared to high-pressure piping. It reduces the mechanical load on the reactor walls and components, extending equipment life and reducing maintenance workload. Selecting an operating pressure within a low pressure range also reduces the requirements for the plasma reactor used in step S4, as high gas pressures increase the difficulty of stable operation of the plasma reactor.

[0042] In another preferred embodiment of the method, the step of adjusting the temperature of the crude syngas in the hot residence chamber includes maintaining the temperature of the crude syngas at at least 850°C for at least two seconds, preferably at 1200°C for at least two seconds.

[0043] The crude syngas is held at a minimum temperature of 850°C, preferably 1200°C, for two seconds to ensure compliant combustion conditions for waste incineration plants as stipulated in Section 6 of the Implementing Regulation of Article 17 of the German Federal Emissions Control Act. This ensures that emission limits for specific pollutants are met. Furthermore, maintaining this temperature increases the yield of the reforming reaction.

[0044] In another preferred embodiment of the method, the first oxidant comprises water vapor (H2O), and the second oxidant comprises carbon dioxide (CO2).

[0045] Water vapor and CO2 are used as reactants and oxidants in gasification and reforming. These two oxidants are added in an adjustable mixing ratio throughout the system, which can also consist of a single pure substance. They significantly influence the reaction temperature and product composition. Both water vapor and CO2 oxidants have been extensively tested technically, require only limited safety precautions, and are readily available and inexpensive. Furthermore, the conversion and utilization of carbon dioxide, which would otherwise be a pollutant, is achieved. In the reforming reaction, water vapor helps increase the H2 content in the syngas by providing hydrogen, resulting in high-quality and versatile products. Simultaneously, CO2, as a secondary oxidant, enables the utilization of potential waste or byproducts from other processes, contributing to a circular economy and reducing CO2 emissions. The combination of these two oxidants allows for precise control of gasification and reforming conditions, as the reaction temperature and the composition of the products can be flexibly adjusted. Moreover, the simultaneous use of water vapor and CO2 enables efficient conversion of the feedstock during gasification, thereby improving process efficiency and reducing reliance on external resources. Overall, this implementation plan results in a more sustainable, cost-effective, and environmentally friendly syngas production process.

[0046] In another preferred embodiment of the method, the gasification in step S2 is carried out in a fluidized bed gasification, a fixed bed gasification, a spiral gasification, or an evaporator.

[0047] In fluidized bed gasification, a heated oxidant serves as the fluidizing agent for the solid bed in the gasification reactor, thereby accelerating the gasification process. This is due to the high medium temperature of the heated oxidant. Gasification in a fluidized bed offers the advantage of highly variable feed material. Furthermore, it provides good controllability for both the feed and gas inputs in the reactor and good scalability over a wide power range. In helical gasification, a reactor with a rotating helix is ​​used, where the helix is ​​formed with a specific geometry. This ensures optimal heat transfer and good mixing of the feed product on the reactor wall. Similar methods can also be used for gasification.

[0048] In another preferred embodiment of the method, a substance, particularly a metal carbonate, metal oxide, metal hydride, or bicarbonate, is added during the gasification process in step S2 to bind the generated acidic gas.

[0049] Substances, particularly metal carbonates, metal oxides, metal hydrides, or bicarbonates, are added to the gasification reactor to neutralize acidic gases that may be generated during the gasification reaction. Acidic gases (especially hydrogen chloride or hydrogen fluoride) may be generated, particularly when using substances containing polyvinyl chloride, which could cause corrosion problems in subsequent process steps.

[0050] In another preferred embodiment of the method, an arc discharge is also performed in the plasma reformer during the processing.

[0051] Arc discharge generates high-energy plasma, which enables the efficient activation and decomposition of molecules, particularly compounds that are difficult to convert or stabilize in hydrocarbon gas mixtures. This leads to increased reaction efficiency and higher yields of valuable syngas components such as hydrogen and carbon monoxide. Specific reaction pathways can also be selectively activated using plasma reactions, allowing for precise control over product composition. Furthermore, the high temperature and energy of the plasma help optimize the conversion of residues and byproducts, thereby improving the overall economics and sustainability of the method.

[0052] In another preferred embodiment, the method includes separating impurity gases in the synthesis gas by condensation and feeding the impurity gases back to the reformer unit, wherein the impurity gases preferably include carbon dioxide, wherein the carbon dioxide preferably constitutes the second oxidant for feeding back the heat energy generated in step S4.

[0053] The purity requirements for syngas are achieved by separating impurity gases that may be present in the syngas stream. Carbon dioxide is a prime example of an impurity gas, although other gases may also be present in the syngas product stream. The separation of impurity gases can be implemented using various techniques, such as scrubbing, membrane separation, or pressure swing / temperature swing adsorption. The chosen separation technique depends on the purity requirements of possible subsequent processes. For example, if the syngas is subsequently used in a phosgene route, carbon dioxide must be almost completely separated, as only ppm levels of carbon dioxide are tolerable.

[0054] In another preferred embodiment, the feed material fed in step S1 consists essentially or only of at least one gaseous waste product, and step S2, which involves gasifying the feed material, is omitted.

[0055] In this embodiment, the feed material fed in step S1 comprises essentially or only at least one gaseous waste product. As a result, the subsequent gasification step S2 of the feed material is unnecessary because the feed material is already in a gaseous state. Therefore, the high primary energy required in step S2 is no longer necessary, and the energy demand of the method is reduced.

[0056] Accordingly, an apparatus for producing syngas from at least one waste product by combining a gasification reaction with a reforming reaction under heat energy recovery conditions is proposed. The apparatus includes a storage tank for storing feed material and a first oxidant and / or a second oxidant, wherein the feed material particularly comprises at least one solid, liquid, and / or gaseous waste product. Furthermore, the apparatus includes a gasification reactor for gasifying the feed material into a hydrocarbon gas mixture and at least one byproduct by means of the first oxidant and / or the second oxidant, with the input of heat energy, wherein the byproduct particularly comprises bottom ash and / or fly ash. The apparatus also includes a reformer unit for processing the hydrocarbon gas mixture into crude syngas with further addition of the first oxidant and / or the second oxidant; and a cooling device for cooling the crude syngas, wherein at least a portion of the heat energy released in the reformer unit is fed back to the gasification reactor to provide at least a portion of the heat energy input to the gasification reactor.

[0057] Here, the apparatus feeds the waste product stored in the waste material container to the gasification reactor. The waste product is solid, but may also exist in a liquid or gaseous state. Subsequently, in the gasification reactor, a process step is carried out to gasify the feed material and oxidant into a hydrocarbon gas mixture and by-products. Here, as by-products, in addition to the heat generated, bottom ash and / or fly ash are also generated. However, this bottom ash and / or fly ash is extracted from the hydrocarbon gas mixture stream and fed back to the gasification reactor for energy efficiency reasons to recover the residual heat after gasification. Subsequently, the hydrocarbon stream is fed to the reformer unit, where a process occurs to reform the hydrocarbon stream and oxidant into crude syngas. Furthermore, a step is taken in the reformer unit to process the crude syngas to finally produce syngas.

[0058] In a preferred embodiment, the apparatus is configured to perform the method according to any one of the foregoing embodiments.

[0059] Furthermore, the method may include a washing step after step S4, in which the acidic synthesis gas is washed in a washing tower with a washing solution (particularly Selexol and / or Rectisol) to provide synthesis gas.

[0060] By using a washing solution such as Selexol and / or Rectisol to wash acidic syngas, unwanted impurities (such as CO2, H2S, and other acidic gases) are effectively removed, resulting in high-purity syngas. This not only improves the quality of the syngas but also enhances its versatility in subsequent applications, such as in the chemical industry or energy production. Using Selexol and Rectisol as washing solutions enables selective absorption of acidic components and precise control of the washing process. This reduces the need for additional purification steps and lowers operating costs. Furthermore, the washing process contributes to improved equipment safety by minimizing the concentration of harmful or corrosive gases in the syngas. Overall, this also leads to better product quality.

[0061] After the washing step of washing the acidic syngas into syngas, the method may first include separating impurity gases and storing the syngas in a storage tank, and preferably includes compressing the syngas.

[0062] Storing the syngas in tanks provides a buffer for the product stream. This buffering allows for better handling of fluctuations in syngas demand. Furthermore, it helps to balance fluctuations in the syngas production process. In addition to the reduction in storage volume required due to compression, compressing the syngas also enables its direct introduction into gas pipelines and general pipelines at controlled pressure levels. Attached Figure Description

[0063] The preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings: Figure 1a and 1b The flowcharts of methods for producing syngas from waste products under heat recovery conditions are shown schematically. Figure 2a A method for producing syngas from waste products under heat recovery conditions is illustrated schematically. Figure 2b A method for producing syngas from waste products under heat recovery conditions with an intermediate loop is schematically illustrated. Figure 3 The schematic diagram illustrates the post-treatment of syngas; and Figure 4 The method for producing syngas from waste products and the post-treatment of syngas are illustrated schematically.

[0064] Explanation of reference numerals in the attached figures: 1 device 10 Waste Material Containers 20 Feeding System 30 Gasification Reactor 32 Ash Removal System 34 Ash Collector 40 reformer units 42 Plasma Reformer 44 Hot Residence Chamber 46 heat exchanger 47 intermediate loop 48 Cooling Zone 50 condenser unit 60 washing tower 70 storage tanks 80 compressor station 90 gas separator S1 feeds in the material. S2 gasification feed material S3 introduces a hydrocarbon gas mixture. S4 processes hydrocarbon gas mixtures. S44 Cooling of Crude Synthetic Gas S444 adjusts the temperature of the crude synthesis gas. S4444 rapid cooling of crude syngas Detailed Implementation exist Figure 1a and 1b The present invention illustrates a method for producing syngas from waste products in the form of an exemplary flowchart. The flowchart shows four steps, S1-S4. Specifically, step S1 shows the feeding of feed material, step S2 shows the gasification of the feed material, step S3 shows the feeding of a hydrocarbon gas mixture into a reformer unit, and step S4 shows the processing of the hydrocarbon gas mixture in the reformer unit.

[0065] In the first step S1, both the feed material and the oxidant stream are fed into the gasification reactor. Here, the oxidant stream can consist of a first oxidant and a second oxidant in an adjustable mixing ratio. This mixing ratio can be changed in both material directions, so that either a pure substance of the first or second oxidant can be present, or a mixture of the first and second oxidants can be present. In the described embodiment, the oxidant stream is understood here as a mixture of water vapor and carbon dioxide. Furthermore, the first and second oxidants can be composed of carbon monoxide (CO), oxygen (O2), or hydrogen (H2). The feed material can consist of solid, liquid, and / or gaseous waste products. For example, waste products can include solid plastic waste. Additionally, carbon sources (e.g., CO2) or organic waste (e.g., biomass or sorting residues) from within the system can be used as waste products. The feed material S1 and the oxidant stream are fed in via a feeding system. This feeding system is implemented, for example, as a screw conveyor, wherein any type of feeding system can be used, such as a belt conveyor, a lifting conveyor, or an industrial vehicle.

[0066] In the second step S2, the feed material introduced in step S1 is gasified in the gasification reactor by an oxidant stream. Due to the endothermic nature of the gasification reaction in S2, thermal energy must be input. As reaction products, a mixture of hydrocarbon gases and at least one byproduct are generated. Furthermore, two, three, four, or any number of byproducts may be generated, with various ash types constituting the most common byproducts. Here, bottom ash and fly ash are generated as byproducts. External thermal energy input is required in step S2 to provide the high process temperature required for gasification. In the embodiment shown in Figure 1, the thermal energy is provided by an electric heater, thus providing a return of the thermal oxidant. Alternatively, the thermal energy can be achieved through any heating method or thermal energy return method within the system. In the embodiment shown in Figure 1, a fluidized bed gasifier is used as the gasification reactor. Alternatively, an entrained flow gasifier or a fixed bed gasifier can also be used. The absolute pressure during the reaction within the gasification reactor is between 1 bar and 20 bar.

[0067] The bottom ash generated during the gasification of S2 settles from the hydrocarbon gas mixture to the bottom of the gasification reactor. Furthermore, the settled bottom ash is separated from the gasification reactor via an ash removal system.

[0068] The fly ash generated during the gasification process in the second step S2, along with the hydrocarbon gas mixture, is discharged from the fluidized bed gasifier at the top of the reactor. Here, the fly ash constitutes only a small portion of the mass stream. This mass stream passes through an ash collector after the gasification reactor to separate the fly ash from the hydrocarbon gas mixture. Here, the ash collector is constructed using a cyclone separator. Alternatively, the ash collector can be constructed using any separation system, such as a filter or adsorption device.

[0069] In the third step S3, the deashed hydrocarbon gas mixture is guided from the gasification reactor to the reformer unit. For example, the hydrocarbon gas mixture may be guided directly to the reformer unit via a pipeline for further processing into syngas. Accordingly, in the third step S3, the gasification reaction in step S2 and the reforming reaction in step S4 are coupled via the gasified medium. Furthermore, it is conceivable to introduce intermediate steps into the coupling, such as a filtration unit or a conveying unit for the medium.

[0070] In the fourth step S4, the hydrocarbon gas mixture is processed into crude syngas in the reformer unit. Here, an oxidant stream is added to the reformer unit to enable the reaction. The oxidant stream consists of a first oxidant and a second oxidant in an adjustable mixing ratio. This mixing ratio can be changed in both material directions, allowing for the presence of pure substances. The oxidants in the oxidant stream in S4 correspond to the first oxidant and / or the second oxidant in the first step S1, wherein the mixing ratio may differ from that in the first step S1. In the illustrated embodiment, water vapor is used as the first oxidant and carbon dioxide as the second oxidant. After the oxidant stream is added to the reformer unit, a reforming reaction to crude syngas occurs in a plasma reformer. Alternatively, a steam reformer can be used instead of the plasma reformer. The plasma reformer is driven by a plasma actuator. These actuators provide the necessary thermal energy for the high reaction temperature. High temperatures are required, such that the medium outlet temperature of the plasma reformer is between 1100°C and 1600°C. In a plasma reformer, the hydrocarbon gas mixture and oxidant stream are mixed to generate nonthermal plasma. This nonthermal plasma then reforms the hydrocarbon gas mixture and oxidant stream into crude syngas. The plasma reformer can perform reforming via arc discharge. The syngas produced in the plasma reformer consists of CO and hydrogen, the mixing ratio of which can be adjusted by the mixing ratio of the oxidant stream. The absolute pressure during the reaction within the plasma reformer is between 1 bar and 20 bar. Furthermore, operating pressures between 1.5 bar and 4 bar are also possible.

[0071] like Figure 1a As shown, the heat exchanger can return the heat energy released from the reformer unit to step S2. This heat energy can then be used for vaporization in step S2. Figure 1bAs shown, the treatment of the hydrocarbon gas mixture in step S4 may include the following additional steps: S44: cooling the crude synthesis gas; S444: adjusting the temperature of the crude synthesis gas in the hot residence chamber to improve the reaction yield; and S4444: quenching the crude synthesis gas in the cooling zone.

[0072] In step S44, heat energy is provided by cooling the crude syngas, which can then be fed back to step S2. During the cooling phase, a portion of the heat energy released to the crude syngas by the plasma reformer in step S4 is further transferred to the heat exchanger. In the illustrated embodiment, the heat exchanger is a ceramic radiant heat exchanger. Alternatively, heat exchangers made of other materials (e.g., iron or stainless steel) can also be used. Here, the heat exchanger transfers the heat energy of the syngas to the oxidant stream. This oxidant stream is supplied separately and / or separated from the syngas product stream by condensation and returned. The oxidant stream is then fed to the heat exchanger. Here, the oxidant stream is evaporated and superheated by the heat exchanger. Alternatively, only the oxidant stream can be evaporated. In this embodiment, the heat exchanger is used as an evaporator. Alternatively, in step S4, the heat exchanger can first transfer the heat energy released by the plasma reformer to an intermediate loop filled with a heat transfer medium. Here, heat transfer oil is used as the heat transfer medium, although any other heat transfer medium can also be used, such as molten salt, liquid metal, water, alcohol-water solution, or salt-water solution. The heat transfer medium then releases its heat energy to the oxidant stream via another heat exchanger. Here, the oxidant stream is evaporated again, and it can also be evaporated and superheated. The heat energy of the oxidant stream is then continued to be transferred to the gasification reactor in step S2. By increasing the heat energy of the oxidant stream and feeding it back, process step S2 is accelerated. This also provides a portion of the heat energy required in step S2.

[0073] In another stage of step S4, which processes the hydrocarbon gas mixture, the temperature of the crude syngas is adjusted in step S444 within the hot residence chamber of the reformer unit. Here, this adjustment is performed by maintaining the temperature at 850 °C for at least two seconds. Alternatively, this adjustment can be performed at a temperature higher than 850 °C for more than two seconds.

[0074] In another step of step S4, specifically step S4444, the crude syngas is quenched in a cooling zone. Here, the crude syngas passes through this cooling zone before exiting the reformer unit. Water is used for quenching, although oil or gas may also be used alternatively. The crude syngas is cooled to a temperature level at which it can be extracted from the reformer unit.

[0075] Figure 2a and 2b A schematic diagram of the first part of a method for producing syngas from waste products is shown.

[0076] Figure 2a Waste material container 10 is shown, in which feed material is stored. Solid plastic waste is used as feed material. The feed material is then conveyed to gasification reactor 30 via feed system 20. Feed system 20 is configured here as a screw conveyor. Figure 2a In the illustrated embodiment, the gasification reactor 30 is configured as a fluidized bed gasifier. Furthermore, an oxidant stream is fed into the gasification reactor 30. Here, a mixture of a first oxidant (e.g., steam) and a second oxidant (e.g., carbon dioxide) is used as the oxidant stream. Gasification of the feed material and the oxidant stream takes place in the gasification reactor 30. Here, in addition to the hydrocarbon gas mixture, ash in the form of bottom ash and fly ash is generated. The bottom ash generated in the gasification reactor settles at the bottom of the reactor after the reaction. The bottom ash is separated from the gasification reactor 30 by an ash removal system 32. The fly ash is drawn off together with the hydrocarbon gas mixture stream at the top of the gasification reactor 30. After the gasification reactor 30, the hydrocarbon gas mixture and fly ash stream pass through an ash collector 34, which in this embodiment is configured as a cyclone separator. The ash collector 34 separates the fly ash present in the stream and returns the fly ash to the gasification reactor 30. The hydrocarbon gas mixture after the fly ash has been removed is then passed through the ash collector 34 and continued to the reformer unit 40.

[0077] A plasma reformer 42 is provided in the reformer unit 40. A hydrocarbon gas mixture and a first oxidant and / or a second oxidant are fed into the plasma reformer 42 via an oxidant stream. The same oxidant as the oxidant stream of the gasification reactor 30 is used as the oxidant stream, although the mixing ratio may differ from that of the oxidant stream of the gasification reactor 30. Water vapor and carbon dioxide are used as oxidants here. Here, a reforming reaction to form crude syngas occurs in the reformer unit after the oxidant stream is added to the plasma reformer 42. The temperature of the crude syngas is regulated in the hot residence chamber 44 after the plasma reformer 42 in the reformer unit 40. Here, this regulation is performed by holding the temperature at 850 °C for two seconds. The crude syngas is also guided through a multi-stage cooling process. In one stage of cooling, the crude syngas releases a portion of its thermal energy to a heat exchanger 46. Here, the heat exchanger 46 is a ceramic radiant heat exchanger. Heat exchanger 46 releases a portion of the thermal energy of the crude syngas to an oxidant stream, wherein the oxidant stream is supplied separately and / or separated from the syngas product stream by condensation and returned. Here, the oxidant stream is evaporated, and may also be evaporated and superheated. In this embodiment, heat exchanger 46 is an evaporator.

[0078] like Figure 2bAs shown, heat exchanger 46 can alternatively transfer the heat energy released to the crude syngas by plasma reformer 42 to an intermediate loop 47 filled with a heat transfer medium. Here, heat transfer oil is used as the heat transfer medium. Two heat exchangers are provided in the intermediate loop 47. In the first heat exchanger, the heat energy continued to be transferred by heat exchanger 46 is received and transferred to the intermediate loop. In the second heat exchanger, the heat energy of the intermediate loop 47 is released to the oxidant stream. Here, the oxidant stream is evaporated again, and it can also be evaporated and superheated. In this embodiment, the intermediate loop functions as an evaporator.

[0079] An oxidant stream with increased thermal energy is fed to the gasification reactor 30. By increasing the thermal energy of the oxidant stream and by feeding it back, gasification in the gasification reactor 30 is accelerated. Here, a portion of the thermal energy required in the gasification reactor 30 is provided.

[0080] Furthermore, the hydrocarbon gas mixture is processed by quenching the crude syngas in cooling zone 48. Here, the crude syngas passes through cooling zone 48 before being discharged from reformer unit 40. Water is used for quenching here. Here, the crude syngas is cooled to a temperature level that can be extracted from reformer unit 40.

[0081] Figure 3 A schematic diagram of the second part of the synthesis gas production from waste products is shown. Here, the crude synthesis gas drawn from the reformer unit is directed to condenser unit 50. In the condenser unit, the crude synthesis gas is condensed and cooled. Here, condensate is separated, which is separated from the crude synthesis gas at the bottom of condenser unit 50. This produces acidic synthesis gas, which is then passed to a scrubbing tower.

[0082] In scrubbing tower 60, during the scrubbing process using a pure scrubbing solution, contaminants such as halogen acids and other acidic gases are introduced along with the acidic syngas. The pure scrubbing solution is fed into scrubbing tower 60. Potassium bicarbonate is used as the scrubbing solution here. Alternatively, Selexol or Rectisol scrubbing can be performed as the scrubbing process, where polyethylene glycol or methanol can subsequently be used as the scrubbing solution. The contaminants are compounds derived from plastic waste. Here, the contaminants are bound to the pure scrubbing solution and separated from the syngas. This results in syngas and a scrubbing solution contaminated with the contaminants. The syngas continues to be passed to storage tank 70, while the contaminated scrubbing solution enters a separate loop. Here, the contaminated scrubbing solution is treated in this loop, where the contaminants are separated from the scrubbing solution, and the pure scrubbing solution is fed back into scrubbing tower 60.

[0083] The crude syngas product stream is stored in storage tank 70. Here, the storage tank is constructed as a container, in which any type of storage tank can be used, such as a cavernous gas storage facility or an absorption gas storage facility. This allows for compensation against fluctuations in syngas production. The syngas is then continued from storage tank 70 to compressor station 80.

[0084] Here, compressor station 80 compresses the syngas to a higher pressure level so that it can be introduced into pipelines, gas networks, or subsequent processes. Compressor station 80 achieves this through compressors. One, two, three, four, or any number of compressors can be used. Subsequent processes include, for example, chemical synthesis, fuel production, hydrogen production, or power generation.

[0085] After compressor station 80, impurity gases are separated from the synthesis gas by condensation in gas separator 90 and returned to heat exchanger 46. Impurity gases are understood to be an oxidant stream consisting of carbon dioxide, from which other impurity gases can also be removed from the synthesis gas by gas separator 90.

[0086] exist Figure 4 The diagram shows a method for producing syngas from waste products. Here, a schematic diagram is shown. Figure 2a and Figure 3 Coupling of the various parts. Feed material is stored in waste material container 10. Solid plastic waste is used as feed material. The feed material is continuously conveyed to gasification reactor 30 via feed system 20. Feed system 20 is configured as a screw conveyor. Gasification reactor 30 is a fluidized bed gasifier. Furthermore, an oxidant stream is fed into gasification reactor 30. Here, a mixture of water vapor and carbon dioxide is used as the oxidant stream. Gasification of the feed material and oxidant stream takes place in gasification reactor 30. Here, in addition to the hydrocarbon gas mixture, ash in the form of bottom ash and fly ash is generated. The bottom ash generated in the gasification reactor settles at the bottom of the reactor after the reaction. The bottom ash is separated from gasification reactor 30 by ash removal system 32. Fly ash is drawn out together with the hydrocarbon gas mixture stream at the top of gasification reactor 30. The hydrocarbon gas mixture and fly ash stream pass through ash collector 34 after gasification reactor 30, where ash collector is a cyclone separator. The fly ash collector 34 separates the fly ash present in the stream and returns it to the gasification reactor 30. The hydrocarbon gas mixture with the fly ash removed is then passed through the fly ash collector 34 and continued to the reformer unit 40.

[0087] A plasma reformer 42 is provided in the reformer unit 40. A hydrocarbon gas mixture and an oxidant stream are fed into the plasma reformer 42. The first and / or second oxidants of the supplied oxidant stream correspond to the first and / or second oxidants of the gasification reactor 30, wherein the mixing ratio may differ from the mixing ratio of the oxidant stream in the gasification reactor 30. Water vapor and carbon dioxide are used as oxidants here. Here, after the oxidant stream is added to the plasma reformer 42 in the reformer unit, a reforming reaction to form crude syngas occurs. The temperature of the crude syngas is regulated in the hot residence chamber 44 after the plasma reformer 42 in the reformer unit 40. Here, this regulation is performed by maintaining the temperature at 850 °C for two seconds. The crude syngas is also guided through a multi-stage cooling process. In one stage of cooling, the crude syngas releases a portion of its thermal energy to a heat exchanger 46. Here, the heat exchanger 46 is a ceramic radiant heat exchanger. Heat exchanger 46 releases a portion of the thermal energy of the crude syngas to an oxidant stream, which is supplied separately and / or extracted from the syngas product stream by condensation and returned in gas separator 90. Here, the oxidant stream is evaporated, and may also be evaporated and superheated. In this embodiment, heat exchanger 46 is an evaporator.

[0088] An oxidant stream with increased thermal energy is fed to the gasification reactor 30. By increasing the thermal energy of the oxidant stream and by recirculating it, gasification in the gasification reactor 30 is accelerated. Here, a portion of the required thermal energy is provided in the gasification reactor 30. Furthermore, the syngas generated from the hydrocarbon gas mixture is processed by quenching the crude syngas in the cooling zone 48. Here, the crude syngas passes through the cooling zone 48 before exiting the reformer unit 40. Quenching is performed using water. Here, the crude syngas is cooled to a temperature level at which it can be drawn from the reformer unit 40 and fed into the condenser unit 50.

[0089] In condenser unit 50, the crude syngas is condensed and cooled. Condensate is separated here, with the condensate being separated from the crude syngas at the bottom of condenser unit 50. This generates acidic syngas, which is then passed to scrubbing tower 60.

[0090] In scrubbing tower 60, during the scrubbing process using a pure scrubbing solution, contaminants such as halogenated acids and other acidic gases are introduced along with the acidic syngas. The pure scrubbing solution is introduced into scrubbing tower 60. Potassium bicarbonate is used as the scrubbing solution here. The contaminants are compounds derived from plastic waste. Here, the contaminants are bound to the pure scrubbing solution and separated from the syngas. This generates syngas and a scrubbing solution contaminated with the contaminants. The syngas is then passed to storage tank 70, while the contaminated scrubbing solution enters a separate loop. Here, the contaminated scrubbing solution is treated in this loop, where the contaminants are separated from the scrubbing solution, and the pure scrubbing solution is fed back into scrubbing tower 60.

[0091] The crude syngas product stream is stored in storage tank 70. Here, the storage tank is configured as a container. This allows for the compensation of fluctuations caused by variations in syngas production. The syngas is then continuously transferred from storage tank 70 to compressor station 80.

[0092] Here, compressor station 80 compresses the syngas to a higher pressure level so that it can be introduced into pipelines, gas networks, or subsequent processes. Compressor station 80 achieves this through compressors.

[0093] After compressor station 80, impurity gases are extracted from the syngas by condensation in gas separator 90 and returned to heat exchanger 46. Here, impurity gases are specifically understood as carbon dioxide as the oxidant stream, and other impurity gases can also be removed from the syngas by gas separator 90.

[0094] Where applicable, all individual features shown in the embodiments may be combined and / or interchanged without departing from the scope of the invention.

Claims

1. A method for producing syngas from at least one waste product by combining a gasification reaction with a reforming reaction under heat energy recovery conditions, wherein, The method includes the following steps: S1: Feed material and first oxidant and / or second oxidant are fed into gasification reactor (30), wherein the feed material particularly includes at least one solid, liquid and / or gaseous waste product; S2: In the presence of the first oxidant and / or the second oxidant, and with the input of thermal energy, the feed material is gasified into a hydrocarbon gas mixture in the gasification reactor (30), wherein at least one by-product is produced, wherein the by-product specifically includes bottom ash and / or fly ash; S3: The hydrocarbon gas mixture is fed from the gasification reactor (30) to the reformer unit (40); S4: With the addition of the first oxidant and / or the second oxidant, the hydrocarbon gas mixture is processed into crude synthesis gas in the reformer unit (40); At least a portion of the heat energy generated in step S4 is fed back to the gasification reactor (30) to provide at least a portion of the heat energy input in step S2.

2. The method for producing syngas according to claim 1, wherein, Step S4, which processes the hydrocarbon gas mixture into crude syngas in the reformer unit (40), includes, in addition to reforming the hydrocarbon gas mixture into crude syngas in the plasma reformer (42), at least one of the following steps: -S44: Cool the crude syngas; -S444: Adjust the temperature of the crude syngas in the hot residence chamber (44) to increase the reaction yield; and -S4444: The crude syngas is quenched in the cooling zone (48).

3. The method for producing syngas according to claim 1 or 2, wherein, A portion of the heat energy generated in step S4 is returned to the gasification reactor (30) via a first oxidant and / or a second oxidant.

4. The method for producing syngas according to claim 3, wherein, In order to recover heat energy, the first oxidant and / or the second oxidant are heated via a heat exchanger (46), particularly via a radiant heat exchanger or a ceramic heat exchanger located between the hot residence chamber (44) and the cooling zone (48).

5. The method for producing syngas according to claim 3, wherein, The return of heat energy is carried out via a heat exchanger (46) located between the hot residence chamber (44) and the cooling zone (48), wherein the heat exchanger (46) heats the medium in the intermediate loop, and wherein the medium then releases the heat to at least one heat sink via at least one second heat exchanger (47), wherein the at least one heat sink comprises a heat sink having the first oxidant and / or the second oxidant flow.

6. The method for producing syngas according to claim 3, wherein, At least one superheater is included between the heat exchanger (46) and the gasification reactor (30).

7. The method for producing syngas according to any one of claims 3 to 6, wherein, Heating the first oxidant and / or at least a portion of the second oxidant accelerates step S2.

8. The method for producing syngas according to any one of the preceding claims, wherein, Step S2 includes separating the bottom ash generated during gasification and includes at least partially separating and returning the fly ash generated during gasification and carried by the hydrocarbon gas mixture to the gasification reactor (30), wherein preferably, the separation also includes separating the bottom ash via an ash discharge system (32), wherein preferably, the separation and return step includes separating the fly ash in the hydrocarbon gas mixture after gasification via an ash collector (34), particularly a cyclone separator.

9. The method for producing syngas according to any one of the preceding claims, wherein, The ratio of hydrogen (H2) to carbon monoxide (CO) in the synthesis gas is adjusted by the mixing ratio of the first oxidant and the second oxidant.

10. The method for producing syngas according to any one of the preceding claims, wherein, The method, after step S4, includes cooling the crude synthesis gas in a condenser unit (50) and separating the condensate.

11. The method for producing syngas according to any one of the preceding claims, wherein, The operating pressure of the gasification reactor (30) and the operating pressure of the plasma reactor (42) are between 1 bar and 20 bar absolute pressures, preferably between 1.5 bar and 4 bar absolute pressures.

12. The method for producing syngas according to any one of claims 2 to 11, wherein, The step of adjusting the temperature of the crude syngas in the hot residence chamber (44) includes maintaining the temperature of the crude syngas at at least 850°C for at least two seconds, preferably at 1200°C for at least two seconds.

13. The method for producing syngas according to any of the preceding claims, wherein the first oxidant comprises water vapor (H2O) and the second oxidant comprises carbon dioxide (CO2).

14. The method for producing syngas according to any one of the preceding claims, wherein, The gasification in step S2 is carried out in a fluidized bed gasification, fixed bed gasification, spiral gasification or evaporator.

15. The method for producing syngas according to any one of the preceding claims, wherein, In the vaporization process described in step S2, a substance is added, particularly a metal carbonate, metal oxide, metal hydroxide, or bicarbonate, to bind the generated acidic gas.

16. The method for producing syngas according to any one of claims 2 to 15, wherein, when claim 2 is cited, During the process, an electric arc discharge also occurs in the plasma reformer (42).

17. The method for producing syngas according to claim 3 or any one of claims 4 to 16, wherein, when claim 3 is referenced, The method includes separating impurity gases in the synthesis gas by condensation and feeding the impurity gases back to the reformer unit (40), wherein the impurity gases preferably include carbon dioxide, wherein the carbon dioxide preferably constitutes the second oxidant for feeding back the heat energy generated in step S4.

18. The method for producing syngas according to claim 1, wherein, The feed material fed in step S1 consists essentially or only of at least one gaseous waste product.

19. An apparatus (1) for producing syngas from at least one waste product by combining a gasification reaction with a reforming reaction under heat recovery conditions, said apparatus (1) comprising: a. A storage container for storing feed material and a first oxidant and / or a second oxidant, wherein the feed material particularly includes at least one solid, liquid and / or gaseous waste product; b. A gasification reactor (30) for gasifying the feed material into a hydrocarbon gas mixture and at least one byproduct by means of the first oxidant and / or the second oxidant, provided that thermal energy is input; wherein the byproduct specifically includes bottom ash and / or fly ash; c. A reformer unit (40) for processing the hydrocarbon gas mixture into crude syngas upon further addition of the first oxidant and / or the second oxidant; and d. Cooling equipment for cooling the crude syngas. At least a portion of the heat energy released in the reformer unit (40) is fed back to the gasification reactor (30) to provide at least a portion of the heat energy input into the gasification reactor (30).

20. The apparatus (1) according to the preceding claim, wherein, The device (1) is configured to perform the method according to any one of claims 1 to 18.

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