A method of obtaining synthesis gas from waste by returning thermal energy and combining it with a reforming reaction in a gasification reaction.

Abstract

The present invention provides a method and apparatus for obtaining synthesis gas from at least one type of waste by returning thermal energy and performing a gasification reaction combined with a reforming reaction. [Solution] The method includes the step of supplying a supply material containing at least one solid, liquid and / or gaseous waste and a first oxidizing agent and / or a second oxidizing agent to a gasification reactor. Furthermore, it includes step S2 in which the supply material is gasified in the gasification reactor by the first oxidizing agent and / or the second oxidizing agent under the supply of thermal energy into a hydrocarbon gas mixture and by-products containing bottom ash and / or fly ash. Furthermore, it includes the step of supplying the hydrocarbon gas mixture from the gasification reactor to a reformer unit, and step S4 in which the hydrocarbon gas mixture is treated into crude synthesis gas by adding the first oxidizing agent and / or the second oxidizing agent in the reformer unit, wherein at least a portion of the thermal energy released in step S4 is returned to the gasification reactor and supplied in step S2.

Description

Technical Field

[0001] The present invention relates to a method and an apparatus for obtaining syngas from waste through a gasification reaction combined with a reforming reaction, with recycling of thermal energy (Rueckfuehrung). Background Art

[0002] Currently, large-scale production of fossil-based syngas is carried out by energy-intensive methods such as natural gas reforming or coal gasification. In this context, syngas is defined as a mixed gas of carbon monoxide (CO) and hydrogen (H2). However, several new methods for producing syngas still have drawbacks at present.

[0003] In the case of biogas reforming, syngas is produced in a distributed manner, which leads to high costs due to small-scale plants, high investment and operating costs, and inefficient logistics. As a result, the price of syngas is significantly higher than that of natural gas.

[0004] In methods where electrolysis is used paired with water-gas shift reaction or co-electrolysis, a very large amount of electrical energy consumption is required with low energy efficiency, which also results in a high price for the obtained syngas.

[0005] Heat-driven waste syngasification methods utilize partial oxidation and combustion of waste feedstock to provide the energy required for thermal reforming to generate syngas. As a result, a large amount of carbon dioxide, which cannot be efficiently utilized even in subsequent processes, is emitted by the process.

[0006] In thermal methods for producing synthesis gas from waste, carbon-containing waste is known to be converted into synthesis gas by adding an oxidizing agent such as oxygen or water vapor; in this case, gasification is performed first. The gaseous fractions generated during gasification have various chain lengths. Some of these are condensed and put on the market as a substitute for crude oil. The gaseous fractions can be used to generate heat or electricity after gasification. However, in terms of economics for industrial applications, the requirements for the individual fractions and compositions of the waste used are very high, and gasification plants to date are specified and therefore limited by the type of waste or certain purities. Furthermore, valuable by-products generated during gasification, such as various types of ash, including bottom ash, fly ash, or pond ash, cannot be used further. In addition, the supply of waste may fluctuate, which is detrimental to the stable, load-free operation of the gasification reactor. Therefore, it also becomes difficult to provide a constant supply of hydrocarbon mixtures.

[0007] Furthermore, while a method for purifying unrefined gases by reforming hydrocarbon-containing gas mixtures into hydrogen-rich synthesis gas from which harmful substances have been removed is known, the used materials from waste treatment are not reused. In known reforming methods, hydrocarbon mixtures such as natural gas, light gasoline, methanol, or biomass are reformed into synthesis gas using an oxidizing agent such as water vapor, consuming heat.

[0008] Overall, known methods use a large amount of energy throughout the entire process chain, from the primary energy carrier to the final product, making electrification uneconomical. Reasons for this include, for example, significant waste heat loss, incomplete use of raw materials, or incomplete use of oxidizers. Non-electric methods using waste materials generate carbon dioxide through the use of oxygen or air as an oxidizer, resulting in the continuous emission of this harmful substance. This also contributes to a decline in synthesis gas quality. [Overview of the project] [Problems that the invention aims to solve]

[0009] The objective of this invention is to provide an improved method and corresponding apparatus for obtaining synthesis gas from waste through a gasification reaction combined with a reforming reaction, starting from known prior art, by returning thermal energy.

[0010] In such cases, particular emphasis is placed on improving energy efficiency and minimizing by-products. Therefore, one of the objectives of the present invention is to provide an improved method and system for obtaining synthesis gas from waste, which aims at the efficient use of waste and the minimization of energy use. [Means for solving the problem]

[0011] The above problem is solved by the method described in claim 1. Advantageous developments will become apparent from the dependent claims, the following description, and the figures.

[0012] Therefore, a method is proposed to obtain synthesis gas from at least one waste by returning thermal energy and a gasification reaction combined with a reforming reaction. This method comprises a first step S1 of supplying a feed material, particularly comprising at least one solid, liquid, and / or gaseous waste, and a first oxidizing agent and / or a second oxidizing agent to a gasification reactor. Furthermore, the method comprises a second step S2 of gasifying the feed material in the gasification reactor with the first oxidizing agent and / or the second oxidizing agent under the supply of thermal energy to a hydrocarbon gas mixture and at least one by-product, particularly comprising bottom ash and / or fly ash. The method further comprises a step S3 of supplying the hydrocarbon gas mixture from the gasification reactor to a reformer unit, and a step S4 of treating the hydrocarbon gas mixture in the reformer unit by adding the first oxidizing agent and / or the second oxidizing agent to produce crude synthesis gas. To provide at least a portion of the thermal energy supplied in step S2, at least a portion of the thermal energy released in step S4 is returned to the gasification reactor.

[0013] In this specification, the term "waste" is understood to mean reactants in a method for obtaining synthesis gas. Typically, suitable reactants are those that arise as waste within the scope of prior methods. However, the latter are not essential conditions for suitability to this method for producing synthesis gas. Therefore, in this specification, the term "waste" also includes reactants that are not actually obtained from waste but are manufactured for a specific purpose.

[0014] Here, waste is understood to include carbon-containing materials in particular, especially methane, propane, biogas, plastics, residual waste, wood waste, biomass, lignin and / or paper waste, or mixtures of materials containing the aforementioned materials, which, among other things, arise as residues, by-products and / or by-products from preceding processes, especially cracking, recycling and / or Fischer-Tropsch synthesis.

[0015] By combining a reformer unit with an upstream gasification reactor, it becomes possible to obtain high-quality synthesis gas from a wide variety of waste materials. Utilizing waste promotes a sustainable circular economy and reduces the need for valuable hydrocarbon-containing raw materials for synthesis gas production. The use of waste as a raw material contributes to reducing landfill waste and promotes sustainable resource use. Simultaneously, the need for fossil resources decreases. The supply material can be supplied from a special waste container used as an intermediate storage unit to compensate for supply bottlenecks or fluctuations. This ensures stable plant operation and consistent production of high-quality synthesis gas. Thus, continuous full plant operation and a constant flow of synthesis gas can be ensured. Furthermore, liquid and / or gaseous substances can also be added to the process. If only liquid substances are used, an evaporator can be used instead of a gasification reactor. Dividing synthesis gas production into four stages lowers the requirements for supply materials and simultaneously broadens the applications of synthesis gas. Another advantage is that solid plastic waste, which normally needs to be treated individually and separately in waste disposal due to their mutually interfering chemical properties, can be added to the method as a supply material. The use of a first and / or second oxidizing agent supplied to the gasification reactor in a variable mixing ratio allows for precise control of gasification conditions, such as reaction temperature and the products generated. This enables precise adaptation of the synthesis gas composition. Furthermore, precise control of gasification and reforming conditions is possible. This improves the adaptability of the method to different starting materials and product requirements. In step S2, the initial step in producing synthesis gas from the feed material is to gasify the feed material into a hydrocarbon gas mixture and at least one by-product. Gasification is an endothermic reaction. During gasification, the supplied carbon-containing energy carrier is converted into a gaseous hydrocarbon gas mixture and by-products by chemical conversion under the supply of thermal energy. Gasification is carried out at temperatures, particularly between 400 and 650°C. By returning thermal energy from the reformer unit to the gasification reactor, the amount of external energy required for gasification in step S2 is reduced, improving the overall energy efficiency of the method. This leads to a cost-effective and sustainable process design.Furthermore, thermal energy feedback enables a uniform supply of thermal energy to the gasification reactor, which minimizes fluctuations in energy input and allows for stable synthesis gas production.

[0016] In step S3, a hydrocarbon gas mixture is supplied to a reformer unit to produce crude synthesis gas. In the subsequent step S4, the hydrocarbon gas mixture is processed in the reformer unit to obtain crude synthesis gas by adding a further first and / or second oxidizer. The synthesis gas produced in step S4 has a purity suitable for many applications, such as chemical synthesis.

[0017] In the fourth step, S4, some of the thermal energy present in the crude synthesis gas is released and returned to the gasification reactor. This returned thermal energy provides some of the thermal energy required in S2, which also improves the energy efficiency of the method.

[0018] In an alternative embodiment, the method comprises a first step S1 of supplying a gaseous supply material substantially or exclusively to a reformer unit, the gaseous supply material comprising a hydrocarbon gas mixture. Furthermore, the method comprises a subsequent step S4 of treating the gaseous supply material substantially or exclusively in the reformer unit to crude synthesis gas by adding a first oxidizer and / or a second oxidizer, wherein at least a portion of the thermal energy released in step S4 is returned.

[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 synthesis gas in the plasma reformer, at least one of the following steps: step S44, which includes cooling the synthesis gas; step S444, which includes adjusting the temperature of the crude synthesis gas in a heat retention chamber to increase the reaction yield; and step S4444, which includes rapidly cooling the crude synthesis gas in a cooling zone.

[0020] Cooling of the synthesis gas in step S44 can be performed by a heat exchanger, which can return thermal energy to the entire system via a heat transfer medium. Utilizing the thermal energy released during the cooling of the crude synthesis gas allows for improved energy efficiency of the method. By placing a heat exchanger between the heat retention chamber and the cooling zone, it is possible to maximize the use of waste heat from the nearby plasma reformer and the thermal energy of the generated synthesis gas without compromising the overall system reaction. Temperature control in the heat retention chamber in S444 is used to increase the reaction yield, destroy harmful substances present in the gas, and control the product composition of the crude synthesis gas. In this case, only a small amount of thermal energy is required in the heat retention chamber to maintain the temperature of the crude synthesis gas. Rapid cooling of the crude synthesis gas in the cooling zone in step S4444 allows for a rapid decrease in the temperature of the high-temperature crude synthesis gas. In this case, the present thermal energy is rapidly removed from the crude synthesis gas. This prevents unintended reactions of the gas. In this case, water cooling by injection is an inexpensive option. Another advantage is that water cooling does not compromise the quality of the synthesis gas.

[0021] In another preferred embodiment of the method, a portion of the energy released in step S4 is returned to the gasification reactor via a first oxidizing agent and / or a second oxidizing agent as a heat transfer medium.

[0022] The efficiency of the method can be significantly improved by precisely returning the energy released in step S4 to the gasification reactor via the first and / or second oxidizer. This integration optimizes the use of thermal energy, thereby further reducing the amount of external energy required. Furthermore, returning the energy via the oxidizer allows for precise and even distribution of the introduced energy, contributing to more flexible control of the gasification process. This embodiment not only enhances process stability but also allows for finer adjustment of reaction conditions, which contributes to the production of consistently high-quality synthesis gas.

[0023] In another preferred embodiment of the method, the returned first oxidizing agent and / or second oxidizing agent are heated via a heat exchanger, particularly a radiant heat exchanger or ceramic heat exchanger between a heat retention chamber and a cooling zone, to return thermal energy.

[0024] Post-treatment of the first and / or second oxidizers returned via a heat exchanger offers the advantage of efficient post-treatment of the returned first and / or second oxidizers, thereby optimizing their quality and reactivity for the gasification process. The use of heat exchangers, such as evaporators, including radiant or ceramic heat exchangers, ensures effective heat transfer from the heat retention chamber or cooling zone. This allows the thermal energy from the process to be used meaningfully, thereby improving energy efficiency and reducing the overall energy requirements of the method. Furthermore, post-treatment in the heat exchanger uniformly conditions the oxidizers, enabling a stable and controllable reaction in the gasification reactor. This contributes to improved process stability, uniform synthesis gas quality, and extended service life of process components.

[0025] In one developed form of the method, the return of thermal energy is carried out through a heat exchanger between a heat retention chamber and a cooling zone, the heat exchanger heats a medium in an intermediate circuit, the medium then releases this heat through at least a second heat exchanger to at least one heat sink, the at least one heat sink comprising a flow of a first oxidizer and / or a second oxidizer.

[0026] The use of an intermediate circuit filled with a heat transfer medium to transfer waste heat from the plasma reformer to the oxidizer flow has the advantage of reducing losses when the waste heat circuit and the oxidizer circuit can be located far apart from each other. Furthermore, the risk of contamination between the two circuits is also reduced. The temperature levels of the oxidizer circuit and the waste heat circuit can be freely adjusted by the intermediate circuit. This makes it impossible to damage the heat exchanger due to excessively high temperatures. In addition, it allows for the release of process heat to other consumers.

[0027] In a development of the method, at least one superheater is provided 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, particularly heated to 650°C, to further increase the heat input to the gasification reactor by the first oxidant and / or the second oxidant. This also reduces the primary energy requirement of the gasification reactor and improves the efficiency of the overall process. Furthermore, the use of at least one superheater helps to control the gasification conditions and control the amount and composition of the resulting 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] Appropriate use of the treated first oxidant and / or second oxidant increases the reaction rate and efficiency of the gasification process, thereby achieving faster and more complete conversion of the feed material into the hydrocarbon gas mixture. This is because, in addition to heat input, the discharge of reaction products from the gasification reactor is accelerated. This improves not only the productivity of the method, but also the energy utilization rate and the uniformity of syngas quality. Furthermore, acceleration of the reaction enables a reduction in residence time in the gasification reactor, which leads to higher throughput and more efficient utilization of plant resources.

[0031] In another preferred embodiment, the method includes isolating (Absonderung) the bottom ash generated during gasification in S2 and at least partially separating (Abscheidung) the fly ash generated during conversion and carried by the hydrocarbon gas mixture back to the gasification reactor, preferably the isolating further includes isolating the bottom ash via an ash discharge system, and preferably the separating and returning step includes separating the fly ash present in the hydrocarbon gas mixture after gasification by an ash trap, particularly a cyclone.

[0032] Ashes such as bottom ash and fly ash are generated as by-products in the gasification process. Due to the high reaction temperature in the gasification reactor, the medium temperature of these by-products is also high, and this medium temperature contributes to maintaining the high temperature level during gasification when they are separated and returned to the reactor. Separating and returning these high-temperature by-products contributes to the high purity of the final gasification product and the high energy efficiency of the overall process.

[0033] The ash removal system for isolating bottom ash prevents sedimentation and clogging, ensuring continuous and uninterrupted operation of the gasification reactor. The ash removal system enables efficient and controlled discharge of by-products, thereby maintaining stable operating conditions and extending the plant's service life. Furthermore, isolating bottom ash facilitates its effective utilization or environmentally friendly disposal. This contributes to improved overall process sustainability by enabling the recovery of valuable resources or specialized waste treatment. Additionally, this ash removal system allows the isolated bottom ash to be returned to the gasification reactor for reuse of the high temperature levels of the ash during gasification.

[0034] Fly ash particles generated during gasification are removed from the final hydrocarbon gas mixture using ash traps such as cyclones or other filtering methods. Efficiently removing fly ash increases the purity of the hydrocarbon gas mixture, improving the quality of the resulting synthesis gas. This is beneficial on the one hand for further processing of the hydrocarbon gas mixture, and on the other hand for further utilization of undesirable by-products. The use of cyclones enables reliable and mechanically robust particle separation even at high temperatures and flow rates, thereby improving process stability. Furthermore, accurately separating and returning fly ash prevents potential accumulation in downstream components, reducing maintenance effort and extending the plant's lifespan. In addition, returning fly ash allows for further utilization of residual materials, thereby increasing the resource efficiency of the method and minimizing waste. Moreover, isolating and returning fly ash present in the hydrocarbon gas mixture flow upstream of the plasma reformer helps in utilizing by-products to improve the overall energy efficiency of the process. In that case, a high temperature level of fly ash is used in the gasification reactor to reduce the large energy consumption required to heat it to the necessary reaction temperature.

[0035] In another preferred embodiment of the method, the component ratio of hydrogen H2 to carbon monoxide CO in the synthesis gas is controlled by the mixing ratio of the first oxidizing agent and the second oxidizing agent.

[0036] The ratio of hydrogen to carbon monoxide in the synthesis gas, also known as the synthesis ratio, is controlled by controlling the mixing ratio of the oxidizer supplied to the gasification reactor and reformer units. In this case, the synthesis ratio can be controlled by the mixing ratio of water vapor to carbon dioxide. This allows for variable adaptation of the synthesis gas composition and quality, thereby ensuring a consistent product quality of the synthesis gas. If the mixing ratio of the oxidizers is constant, system adaptation due to fluctuations in the composition of the supplied materials is prevented. In existing processes, the mixing ratio of carbon monoxide to hydrogen is adjusted by a water-gas shift reaction. This is not necessary here, which also saves resources and contributes to the overall energy efficiency of the system. Control of the synthesis ratio by the mixing ratio of the oxidizers is made possible by the use of non-catalytic, i.e., thermal or plasma-based, reforming in step S4.

[0037] In another preferred embodiment of the method, the method according to step S4 includes cooling the crude synthesis gas in a condenser unit under condensate separation.

[0038] This cooling process in the condenser unit is used to process the crude synthesis gas and separate any airborne dust particles, salts, and volatile heavy metals and residual vapors that may still be present in the crude synthesis gas flow. The separated substances are ultimately removed from the synthesis gas flow by condensation, resulting in pure synthesis gas. Furthermore, precisely lowering the temperature allows for optimal processing of the synthesis gas for subsequent process steps, which also enhances the efficiency and flexibility of the method. In addition, the separation of condensate allows for the removal of undesirable associated substances such as water and condensable compounds, thereby improving the purity and quality of the synthesis gas. Moreover, the condenser unit contributes to effective heat recovery by removing excess heat from the gas flow, which improves the overall energy efficiency of the process. This integration also minimizes the effort required for downstream gas purification.

[0039] In another preferred embodiment of this method, the operating pressure of the gasification reactor and the operating pressure of the plasma reactor are absolute pressures of 1 bar to 20 bar, preferably 1.5 to 4 bar.

[0040] The operating pressure of the reactor required to achieve a high reaction yield of synthesis gas and enable the gasification and reforming reaction steps is an absolute pressure of 1 bar to 20 bar. Furthermore, the operating pressure of the reactor can be adjusted to an absolute pressure of 1.5 to 4 bar. Moreover, the process steps are substantially isobaric. In this case, less work needs to be done by the compressor, which is reflected in a reduction in energy consumption. Furthermore, in this intermediate pressure range, low-pressure piping, which has a lower cost factor than high-pressure piping, can be used. This pressure range reduces the mechanical load on the reactor walls and components, extends the life of the plant, and reduces maintenance effort. In addition, high gas pressure makes stable operation of the plasma reactor difficult, so selecting an operating pressure in the low-pressure range lowers the requirements for the plasma reactor used in step S4.

[0041] In another preferred embodiment of the method, the step of adjusting the temperature of the crude synthesis gas in the heat retention chamber includes maintaining the temperature of the crude synthesis gas at least 850°C, preferably 1200°C, for at least 2 seconds.

[0042] Maintaining the crude synthesis gas at a minimum temperature of 850°C, preferably 1200°C, for 2 seconds ensures combustion conditions in waste incineration facilities that comply with the standards of Section 6 of Section 17 of the Federal Emissions Control Act. This guarantees specific limits on the emission of hazardous substances. Furthermore, maintaining the temperature can increase the yield of the reforming reaction.

[0043] In another preferred embodiment of the method, the first oxidizing agent comprises water vapor (H2O) and the second oxidizing agent comprises carbon dioxide (CO2).

[0044] Steam and carbon dioxide are used as reactants and oxidizers in gasification and reforming. The oxidizers, steam and carbon dioxide, are added in adjustable mixing ratios when they are involved in the reaction throughout the system, and the mixing ratio can also consist of pure substances. In this case, they have a decisive influence on the reaction temperature and product composition. The oxidizers steam and carbon dioxide have already been proven in the technical sector, require only limited safety measures, and are inexpensive and readily available. Furthermore, in the case of carbon dioxide, an inherently hazardous substance is utilized. Steam contributes to increasing the hydrogen content in the synthesis gas by providing hydrogen during the reforming reaction, thereby yielding a high-quality, widely usable product. Simultaneously, carbon dioxide, as a second oxidizer, enables the utilization of waste or by-products that may arise from other processes, contributing to the promotion of a circular economy and the reduction of carbon dioxide emissions. Combining the two oxidizers allows for flexible adaptation of both the reaction temperature and the composition of the resulting products, enabling precise control of gasification and reforming conditions. Furthermore, the simultaneous use of steam and carbon dioxide achieves effective conversion of feedstock during gasification, thereby improving process efficiency and reducing the need for external resources. Overall, this embodiment leads to a more sustainable, cost-effective, and environmentally friendly synthesis gas production method.

[0045] In another preferred embodiment of the method, the gasification in step S2 is carried out by fluidized bed gasification, fixed bed gasification, screw gasification, or evaporator.

[0046] Superheated oxidizers are used as liquefaction agents for the solid bed in a gasification reactor when using fluidized bed gasification, thereby accelerating the gasification process. This is due to the high medium temperature of the superheated oxidizer. Gasification in fluidized bed gasification has the advantage of high variability of the feed material. Furthermore, it offers good control over the introduction of feed materials and gas into the reactor and good scalability over a wide coverage area. Screw gasification uses a reactor equipped with a rotating screw, which is designed with a special shape. This ensures optimal heat transfer and good mixing of the feed materials at the reactor wall. Furthermore, equivalent gasification methods can be used.

[0047] In another preferred embodiment of the method, a substance, particularly a metal carbonate, metal oxide, metal hydride, or bicarbonate, is supplied to the gasification in step S2 in order to absorb and remove the resulting acidic gas.

[0048] The supply of materials, particularly metal carbonates, metal oxides, metal hydrides, or bicarbonates, to the gasification reactor helps absorb and remove acidic gases that may be generated during the gasification reaction. When using materials, especially those containing polyvinyl chloride, acidic gases, particularly hydrogen chloride or hydrogen fluoride, may be generated, which can cause corrosion problems in subsequent process steps.

[0049] In another preferred embodiment of the method, an arc discharge is further performed in the plasma modifier during processing.

[0050] Arc discharge generates a high-energy plasma that enables the efficient activation and decomposition of molecules in hydrocarbon gas mixtures, particularly unreactive or stable compounds. This improves reaction efficiency and increases the yield of valuable synthesis gas components such as hydrogen and carbon monoxide. The use of plasma reactions also allows for precise stimulation of specific reaction pathways, thereby enabling precise control of product composition. Furthermore, the high temperature and high energy of the plasma contribute to optimizing the conversion of residues and by-products, thereby improving the overall economics and sustainability of the method.

[0051] In a more preferred embodiment, the method includes separating interfering gases present in the synthesis gas by condensation and returning them to a reformer unit, wherein the interfering gases preferably include carbon dioxide, and the carbon dioxide preferably forms a second oxidizing agent for returning the thermal energy generated in step S4.

[0052] The required purity for synthesis gas is achieved by separating any interfering gases that may be present in the synthesis gas flow. These interfering gases include carbon dioxide in particular, but other gases may also be present in the synthesis gas production flow. Separation of interfering gases can be performed using various techniques, such as washing, membrane separation, and pressure or temperature swing adsorption. The selected separation technique is tailored to the purity requirements of any subsequent processes. For example, if the synthesis gas is then used in a phosgene route, carbon dioxide must be separated almost completely, as only ppm levels are acceptable.

[0053] In another preferred embodiment, the feed material supplied in step S1 substantially or exclusively includes at least one gaseous waste, and the step S2 for gasifying the feed material is omitted.

[0054] In this embodiment, the feed material supplied in step S1 substantially or exclusively includes at least one gaseous waste. As a result, since the feed material is already in a gaseous condensation state, there is no need for step S2 to gasify the feed material. This eliminates the need for the high primary energy that would otherwise be required in step S2, and reduces the energy requirements of the method.

[0055] Therefore, an apparatus is proposed for obtaining synthesis gas from at least one waste material via a gasification reaction combined with a reforming reaction, by returning thermal energy. The apparatus comprises a feed material comprising a feed material comprising at least one solid, liquid, and / or gaseous waste material and a reservoir for a first oxidizer and / or a second oxidizer. Furthermore, the apparatus comprises a gasification reactor for gasifying the feed material with the first and / or second oxidizer under the supply of thermal energy to a hydrocarbon gas mixture and at least one by-product comprising at least bottom ash and / or fly ash. The apparatus further comprises a reformer unit for further adding the first and / or second oxidizer to treat the hydrocarbon gas mixture into crude synthesis gas, and a cooling device for cooling the crude synthesis gas, wherein at least a portion of the thermal energy released in the reformer unit is returned to the gasification reactor to provide at least a portion of the thermal energy supplied to the gasification reactor.

[0056] In this case, the apparatus supplies the waste, which is a solid stored in a waste container but may also exist in liquid or gaseous form, to the gasification reactor. Subsequently, a process is carried out in the gasification reactor in which the feed material and oxidizer are gasified into a hydrocarbon gas mixture and by-products. In addition to the heat generated, bottom ash and / or fly ash are also produced as by-products, but for energy efficiency reasons, these are removed from the hydrocarbon gas mixture flow to reuse the residual heat of the gasified material and are supplied back to the gasification reactor. Next, the hydrocarbon flow is supplied to a reformer unit, where the hydrocarbon flow and oxidizer are reformed into crude synthesis gas. Furthermore, in the reformer unit, a process is carried out to process the crude synthesis gas in order to obtain the final synthesis gas.

[0057] In a preferred embodiment, the apparatus is configured to perform the method according to any of the embodiments described above.

[0058] Furthermore, the method may include, after step S4, a step of washing the acidic synthesis gas in a washing tower using a washing solution, particularly Selexol and / or Rectisol, in order to provide the synthesis gas.

[0059] The cleaning process of acidic synthesis gas using cleaning solutions such as Selexol and / or Rectisol effectively removes undesirable impurities such as carbon dioxide, hydrogen sulfide, and other acidic gases from the acidic synthesis gas, producing high-purity synthesis gas. This not only improves the quality of the synthesis gas but also enhances its versatility for subsequent applications, such as in the chemical industry or energy production. Using Selexol and / or Rectisol as the cleaning solution allows for the selective absorption of acidic components and precise control of the cleaning process. This reduces the need for additional purification steps and lowers operating costs. Furthermore, the cleaning process contributes to improved plant safety by minimizing the concentration of harmful or corrosive gases in the synthesis gas. Overall, this leads to improved product quality, among other things.

[0060] Following the washing step of acidic synthesis gas into synthesis gas, the method first includes separating the interfering gas and storing the synthesis gas in a storage tank, and preferably compressing the synthesis gas.

[0061] Storing synthesis gas in storage tanks allows for buffering of the product flow. This buffering better accommodates fluctuating synthesis gas demand. Furthermore, it can compensate for variations in synthesis gas production. Compressing synthesis gas, in addition to reducing the volume required for storage, allows for direct introduction into gas networks and generally pipelines at controlled pressure levels. Other preferred embodiments of the present invention will be described in more detail below with reference to the drawings. [Brief explanation of the drawing]

[0062] [Figure 1a] This diagram schematically shows a flowchart of a method for obtaining synthesis gas from waste by returning thermal energy. [Figure 1b] This diagram schematically shows a flowchart of a method for obtaining synthesis gas from waste by returning thermal energy. [Figure 2a] This diagram schematically illustrates a method for obtaining synthesis gas from waste by returning thermal energy. [Figure 2b] This diagram schematically illustrates a method for obtaining synthesis gas from waste by using an intermediate circuit to return thermal energy. [Figure 3] This diagram schematically illustrates the post-treatment of synthesis gas. [Figure 4] This diagram schematically illustrates a method for obtaining synthesis gas from waste and for post-treatment of the synthesis gas. [Modes for carrying out the invention]

[0063] Figures 1a and 1b show an illustrative flowchart of a method for obtaining synthesis gas from waste. The flowchart shows four steps S1 to S4. In this case, the first step S1 shows the supply of the feed material, the second step S2 shows the gasification of the feed material, the third step S3 shows the supply of the hydrocarbon gas mixture to the reformer unit, and the fourth step S4 shows the processing of the hydrocarbon gas mixture in the reformer unit.

[0064] In the first step S1, both the feed material and the oxidizer stream are supplied to the gasification reactor. In this case, the oxidizer stream may consist of a first oxidizer and a second oxidizer in a controllable mixing ratio. The mixing ratio can be changed in both material directions, thereby allowing both pure substances of the first or second oxidizer and mixtures of the first and second oxidizers to exist. In the above-described embodiment, the mixing ratio of water vapor and carbon dioxide is understood here as the oxidizer stream. Furthermore, the first and second oxidizers can be formed as carbon monoxide (CO), oxygen (O2), or hydrogen (H2). The feed material may consist of solid, liquid, and / or gaseous waste. For example, the waste may include solid plastic waste. Furthermore, organic waste such as a carbon source from a system of carbon dioxide, or biomass or sorting residues can also be used as waste. The supply of the feed material and the supply of the oxidizer stream S1 is made possible by a feed system. The supply system is implemented as, for example, a screw conveyor, but any type of supply system can be used, such as a belt conveyor, an inclined conveyor, or a cargo handling vehicle.

[0065] In the second step S2, the feed material supplied in step S1 is gasified in the gasification reactor by an oxidizing agent flow. Since the gasification reaction in S2 is endothermic, thermal energy must be supplied. The reaction products are a hydrocarbon gas mixture and at least one by-product. Additionally, two, three, four, or any number of by-products may be produced, the most common being various types of ash. In this case, bottom ash and fly ash are produced as by-products. External supply of thermal energy is necessary in step S2 to provide a high process temperature for gasification. In the example shown in Figure 1, thermal energy is provided by an electric heater, and thus by returning the oxidizing agent to a high temperature. Furthermore, thermal energy can be provided by heating or returning thermal energy in any form within the system. In the example shown in Figure 1, a fluidized bed gasifier is used as the gasification reactor. Furthermore, a jet bed gasifier or a fixed bed gasifier can also be used. The absolute pressure during the reaction in the gasification reactor is 1 bar to 20 bar.

[0066] The bottom ash generated during gasification in S2 accumulates at the bottom of the gasification reactor, separated from the hydrocarbon gas mixture. The accumulated bottom ash is further isolated from the gasification reactor via an ash removal system.

[0067] The fly ash generated during gasification in the second step S2 is discharged from the fluidized bed gasifier along with the hydrocarbon gas mixture at the front of the reactor. In this case, the proportion of fly ash is only a small amount of the material flow. After the gasification reactor, the material flow passes through an ash trap to separate the fly ash from the hydrocarbon gas mixture. In this case, the ash trap is formed by a cyclone. Furthermore, the ash trap can be formed by any isolation system, such as a filter or adsorption.

[0068] In the third step S3, the hydrocarbon gas mixture from which the ash has been removed is sent from the gasification reactor to the reformer unit. The hydrocarbon gas mixture is sent directly to the reformer unit, for example, through piping, and further processed into synthesis gas. Thus, in the third step S3, the gasification reaction from step S2 and the reforming reaction in step S4 are combined via the gasified medium. Furthermore, it is conceivable to introduce intermediate steps, such as a filter unit or a medium transfer unit, into the combination.

[0069] In the fourth step, S4, the hydrocarbon gas mixture is treated into crude synthesis gas in the reformer unit. To enable the reaction, an oxidizer stream is added to the reformer unit. The oxidizer stream consists of a first and second oxidizer in a controllable mixing ratio. The mixing ratio can be changed in both material directions, allowing for the presence of pure substances. The oxidizers in the oxidizer stream in S4 correspond to the first and / or second oxidizers in the first step, S1, and their mixing ratios can differ from those in the first step, S1. In the example shown, steam is used as the first oxidizer and carbon dioxide as the second oxidizer. After the oxidizer stream is added to the reformer unit, the reforming reaction into crude synthesis gas takes place in the plasma reformer. Furthermore, a steam reformer can be used instead of the plasma reformer. In this case, the plasma reformer is driven by a plasma driver, which provides the thermal energy necessary for the high reaction temperature. In this case, high temperatures are required, so the medium outlet temperature of the plasma reformer is 1100°C to 1600°C. In the plasma reformer, the hydrocarbon gas mixture and the oxidizer stream are mixed to generate a non-thermal plasma. Next, the non-thermal plasma reforms the hydrocarbon gas mixture and oxidizer stream into a crude synthesis gas. The plasma reformer can perform the reforming in the form of an arc discharge. The synthesis gas produced in the plasma reformer consists of carbon monoxide and hydrogen, and its mixing ratio can be controlled by the mixing ratio of the oxidizer stream. The absolute pressure during the reaction in the plasma reformer is 1 bar to 20 bar. Furthermore, an operating pressure of 1.5 bar to 4 bar is possible.

[0070] As shown in Figure 1a, the heat exchanger can return the thermal energy released in the reformer unit to step S2. This thermal energy can also be used for gasification in step S2. As shown in Figure 1b, the processing of the hydrocarbon gas mixture in step S4 may include further steps S44: cooling the crude synthesis gas, S444: adjusting the temperature of the crude synthesis gas in the heat retention chamber to increase the reaction yield, and S4444: rapidly cooling the crude synthesis gas in the cooling zone.

[0071] In step S44, thermal energy is provided by the cooling of the crude synthesis gas, and this thermal energy can also be returned to step S2. During the cooling stage, a portion of the thermal energy released from the plasma reformer into the crude synthesis gas in step S4 is transferred to a heat exchanger. In the example shown, the heat exchanger is a ceramic radiant heat exchanger. Furthermore, heat exchangers made from other materials, such as iron or stainless steel, can also be used. In that case, the heat exchanger transfers the thermal energy of the synthesis gas to an oxidizer stream. The oxidizer stream is supplied separately and / or separated from the synthesis gas production stream by condensation and returned. The oxidizer stream is supplied to the heat exchanger. In that case, the oxidizer stream is evaporated and superheated by the heat exchanger. Furthermore, it is also possible to simply evaporate the oxidizer stream. In this embodiment, the heat exchanger is used as an evaporator. Alternatively, the heat exchanger can first transfer the thermal energy released from the plasma reformer in step S4 to an intermediate circuit filled with a heat transfer medium. In this case, hot oil is used as the heat transfer medium, but any other heat transfer medium can also be used, such as molten salt, liquid metal, water, aqueous alcohol solution, or aqueous salt solution. Next, the heat transfer medium releases thermal energy to the oxidizer flow via another heat exchanger. In this case as well, the oxidizer flow is evaporated, but it is also possible for the oxidizer flow to be evaporated and superheated. Next, the thermal energy of the oxidizer flow is transferred to the gasification reactor in step S2. Step S2 of the method is accelerated by the increase in the thermal energy of the oxidizer flow and the return of the oxidizer flow. In this case as well, it can provide some of the thermal energy required in step S2.

[0072] In another step S4 of the processing of the hydrocarbon gas mixture, the temperature of the crude synthesis gas in the reformer unit is adjusted in the heat retention chamber of step S444. In this case, the adjustment is performed by maintaining the temperature at 850°C for at least 2 seconds. Furthermore, the adjustment may be performed at a temperature above 850°C for longer than 2 seconds.

[0073] In another step S4 processing the hydrocarbon gas mixture, the crude synthesis gas is quenched in a cooling zone in step S4444. In this case, the crude synthesis gas passes through the cooling zone before being discharged from the reformer unit. In this case, water is used for quenching, but oil or gas can also be used as an alternative. In this case, the crude synthesis gas is cooled to a temperature level at which it can be discharged from the reformer unit.

[0074] Figures 2a and 2b show schematic diagrams of the first section of the method for obtaining synthesis gas from waste.

[0075] Figure 2a shows a waste container 10 where the feed material is stored. Solid plastic waste is used as the feed material. The feed material is transferred to the gasification reactor 30 via a feed system 20. The feed system 20 is designed here as a screw conveyor. In the example shown in Figure 2a, the gasification reactor 30 is designed as a fluidized bed gasifier. Furthermore, an oxidizer stream is supplied to the gasification reactor 30. The oxidizer stream used here is a mixture of a first oxidizer, e.g., water vapor, and a second oxidizer, e.g., carbon dioxide. In the gasification reactor 30, the feed material is gasified using the oxidizer stream. In addition to the hydrocarbon gas mixture, ash such as bottom ash and fly ash is produced. The bottom ash generated in the gasification reactor accumulates at the bottom of the reactor after the reaction. The bottom ash is isolated from the gasification reactor 30 by an ash discharge system 32. The fly ash is discharged at the front of the gasification reactor 30 along with the hydrocarbon gas mixture stream. The hydrocarbon gas mixture and fly ash flow through the gasification reactor 30, followed by an ash trap 34, which in this example is designed as a cyclone. The ash trap 34 separates the fly ash present in the flow and returns this fly ash back to the gasification reactor 30. The hydrocarbon gas mixture, from which the fly ash has been removed, is then transferred after the ash trap 34 to a reformer unit 40.

[0076] The reformer unit 40 contains a plasma reformer 42. The plasma reformer 42 is supplied with a hydrocarbon gas mixture and a first oxidizer and / or a second oxidizer via an oxidizer stream. The same oxidizer used in the oxidizer stream of the gasification reactor 30 is used as the oxidizer stream, but the mixing ratio can differ from that of the oxidizer stream of the gasification reactor 30. Here, water vapor and carbon dioxide are used as oxidizers. In this case, after the oxidizer stream is added in the reformer unit, a reforming reaction to crude synthesis gas occurs in the plasma reformer 42. The temperature of the crude synthesis gas is controlled in the reformer unit 40 in a heat retention chamber 44 after the plasma reformer 42. In this case, the control is performed by maintaining the temperature at 850°C for 2 seconds. Furthermore, the crude synthesis gas is sent through a multi-stage cooling process. In one stage of cooling, the crude synthesis gas releases some of its thermal energy into a heat exchanger 46. In this case, the heat exchanger 46 is a ceramic radiant heat exchanger. The heat exchanger 46 releases some of the thermal energy of the crude synthesis gas into an oxidizer stream, which is supplied separately and / or separated from the synthesis gas production stream by condensation and returned. In this case, the oxidizer stream is evaporated, although it is also possible for the oxidizer stream to be evaporated and superheated. In this embodiment, the heat exchanger 46 is an evaporator.

[0077] As shown in Figure 2b, the heat exchanger 46 can alternatively first send the thermal energy released from the plasma reformer 42 to the crude synthesis gas to an intermediate circuit 47 filled with a heat transfer medium. In this case, hot oil is used as the heat transfer medium. The intermediate circuit 47 has two heat exchangers. In the first heat exchanger, the thermal energy sent from the heat exchanger 46 is received and transferred to the intermediate circuit. In the second heat exchanger, the thermal energy from the intermediate circuit 47 is released into the oxidizer flow. In this case as well, the oxidizer flow is evaporated, but it is also possible for the oxidizer flow to be evaporated and superheated. In this embodiment, the intermediate circuit is used as an evaporator.

[0078] The oxidizer stream, with its increased thermal energy, is supplied to the gasification reactor 30. The increase in the thermal energy of the oxidizer stream, and its return, accelerate gasification in the gasification reactor 30. In this case, a portion of the thermal energy required in the gasification reactor 30 is provided.

[0079] Furthermore, the hydrocarbon gas mixture is treated by quenching the crude synthesis gas in a cooling zone 48. In this case, the crude synthesis gas passes through the cooling zone 48 before being discharged from the reformer unit 40. In this case, water is used for quenching. In this case, the crude synthesis gas is cooled to a temperature level that allows it to be discharged from the reformer unit 40.

[0080] Figure 3 shows a schematic diagram of the second section of obtaining synthesis gas from waste. In this case, the crude synthesis gas discharged from the reformer unit is sent to the condenser unit 50. In the condenser unit, the crude synthesis gas is condensed and cooled. In this case, the condensate is separated and isolated from the crude synthesis gas at the bottom of the condenser unit 50. This generates acidic synthesis gas, which is then transferred to the scrubbing tower.

[0081] In the scrubbing tower 60, hazardous substances, such as halogen acids and other acidic gases, transported along with the acidic synthesis gas, are combined with a pure scrubbing solution in the scrubbing method. The pure scrubbing solution is supplied to the scrubbing tower 60. Potassium bicarbonate is used as the scrubbing solution here. Furthermore, Selexol scrubbing or Rectisol scrubbing can also be performed as the scrubbing method, in which case polyethylene glycol or methanol can be used as the scrubbing solution. The hazardous substances are generated from compounds of plastic waste. In this case, the hazardous substances are combined with the pure scrubbing solution and separated from the synthesis gas. This results in synthesis gas and a scrubbing solution contaminated with hazardous substances. The synthesis gas is transferred to a storage tank 70, and the contaminated scrubbing solution containing hazardous substances enters another circuit. In this case, the scrubbing solution contaminated with hazardous substances is treated, the hazardous substances are isolated from the scrubbing solution, and the pure scrubbing solution is supplied back to the scrubbing tower 60.

[0082] The storage tank 70 stores the production logistics of crude synthesis gas. In this case, the storage container is designed as a vessel, and any type of storage container can be used, such as a cavity storage container (Kavernenspeicher) or an adsorption storage container. In this case, fluctuations in the increase or decrease of synthesis gas production are compensated for. The synthesis gas is transferred from the storage tank 70 to the compressor station 80.

[0083] The compressor station 80 compresses the synthesis gas to a higher pressure level, allowing it to be sent to pipelines, gas networks, or further processes. The compressor station 80 enables this through compressors. In this case, one, two, three, four, or any number of compressors can be used. Further processes may include, for example, chemical synthesis, fuel production, hydrogen production, or power generation.

[0084] After the compressor station 80, the interfering gas is separated from the synthesis gas by condensation in the gas separator 90 and returned to the heat exchanger 46. The oxidizing agent stream consisting of carbon dioxide is understood as the interfering gas, and other interfering gases can also be removed from the synthesis gas by the gas separator 90.

[0085] Figure 4 shows a schematic diagram of a method for obtaining synthesis gas from waste. This combines several sections from Figures 2a and 3. The feed material is stored in a waste container 10. Solid plastic waste is used as the feed material. The feed material is transferred to the gasification reactor 30 via a feed system 20. The feed system 20 is designed here as a screw conveyor. The gasification reactor 30 is a fluidized bed gasifier. Furthermore, an oxidizer stream is supplied to the gasification reactor 30. Here, a mixture ratio of water vapor and carbon dioxide is used as the oxidizer stream. In the gasification reactor 30, the feed material is gasified using the oxidizer stream. In addition to the hydrocarbon gas mixture, ash such as bottom ash and fly ash is produced. The bottom ash generated in the gasification reactor accumulates at the bottom of the reactor after the reaction. The bottom ash is isolated from the gasification reactor 30 by an ash discharge system 32. The fly ash is discharged at the front of the gasification reactor 30 along with the flow of the hydrocarbon gas mixture. The hydrocarbon gas mixture and fly ash flow proceeds to the gasification reactor 30, where it passes through an ash trap 34, which is a cyclone. The ash trap 34 separates the fly ash present in the flow and returns this fly ash back to the gasification reactor 30. The hydrocarbon gas mixture, from which the fly ash has been removed, is transferred after the ash trap 34 to the reformer unit 40.

[0086] A plasma reformer 42 is present in the reformer unit 40. A hydrocarbon gas mixture and an oxidizer stream are supplied to the plasma reformer 42. The first and / or second oxidizers in the supplied oxidizer stream correspond to the first and / or second oxidizers in the gasification reactor 30, and their mixing ratio can differ from that of the oxidizer stream in the gasification reactor 30. Here, water vapor and carbon dioxide are used as oxidizers. In this case, after the oxidizer stream is added in the reformer unit, a reforming reaction to crude synthesis gas occurs in the plasma reformer 42. The temperature of the crude synthesis gas is controlled in the reformer unit 40 in a heat retention chamber 44 after the plasma reformer 42. In this case, the control is performed by maintaining the temperature at 850°C for 2 seconds. Furthermore, the crude synthesis gas is sent through a multi-stage cooling process. In one stage of cooling, the crude synthesis gas releases some of its thermal energy into a heat exchanger 46. In this case, the heat exchanger 46 is a ceramic radiant heat exchanger. The heat exchanger 46 releases some of the thermal energy of the crude synthesis gas into an oxidizer stream, which is separately supplied and / or removed from the synthesis gas production stream by condensation and returned by a gas separator 90. In this case, the oxidizer stream is evaporated, although it is also possible for the oxidizer stream to be evaporated and superheated. In this embodiment, the heat exchanger 46 is an evaporator.

[0087] The oxidizer stream, with its increased thermal energy, is supplied to the gasification reactor 30. The increase in the thermal energy of the oxidizer stream, and its return, accelerates gasification in the gasification reactor 30. In this case, a portion of the thermal energy required in the gasification reactor 30 is provided. Furthermore, the synthesis gas generated from the hydrocarbon gas mixture is treated by quenching the crude synthesis gas in the cooling zone 48. In this case, the crude synthesis gas passes through the cooling zone 48 before being discharged from the reformer unit 40. In this case, water is used for quenching. In this case, the crude synthesis gas is cooled to a temperature level to which it is sent from the reformer unit 40 to the condenser unit 50.

[0088] In the condenser unit 50, the crude synthesis gas is condensed and cooled. In this process, the condensate is separated and isolated from the crude synthesis gas at the bottom of the condenser unit 50. This generates acidic synthesis gas, which is then transferred to the scrubbing tower 60.

[0089] In the scrubbing tower 60, hazardous substances, such as halogen acids and other acidic gases, which are transported along with the acidic synthesis gas, are combined with a pure cleaning solution in the scrubbing process. The pure cleaning solution is introduced into the scrubbing tower 60. Potassium bicarbonate is used as the cleaning solution here. The hazardous substances are generated from compounds of plastic waste. In this case, the hazardous substances are combined with the pure cleaning solution and separated from the synthesis gas. This results in synthesis gas and a cleaning solution contaminated with hazardous substances. The synthesis gas is transferred to a storage tank 70, and the contaminated cleaning solution containing hazardous substances enters another circuit. In this case, the cleaning solution contaminated with hazardous substances is treated, the hazardous substances are isolated from the cleaning solution, and the pure cleaning solution is supplied back to the scrubbing tower 60.

[0090] The raw materials for the production of crude synthesis gas are stored in the storage tank 70. In this case, the storage container is designed as a vessel. In this case, fluctuations in the increase or decrease of synthesis gas production are compensated for. The synthesis gas is transferred from the storage tank 70 to the compressor station 80.

[0091] Compressor Station 80 compresses synthesis gas to a higher pressure level, allowing it to be sent to pipelines, gas networks, or further processes. Compressor Station 80 makes this possible through its compressors.

[0092] After the compressor station 80, the interfering gas is removed from the synthesis gas by condensation in the gas separator 90 and returned to the heat exchanger 46. Carbon dioxide, in particular, is understood as an interfering gas as an oxidizing agent, and the gas separator 90 can also remove other interfering gases from the synthesis gas.

[0093] Where applicable, all individual features shown in the embodiments can be combined with and / or substituted for one another without departing from the scope of the invention. [Explanation of symbols]

[0094] 1 device 10 Waste containers 20 Supply System 30 Gasification reactor 32 Ash Discharge System 34 Ashtrap 40 Reformer Unit 42 Plasma modifier 44 Heat retention chamber 46 Heat exchanger 47 Intermediate circuit 48 cooling zones 50 Condenser Units 60 Washing Tower 70 storage tanks 80 Compressor Stations 90 Gas separator S1 supplies materials. S2 Gasifies the supply material. S3 Supply the hydrocarbon gas mixture S4 Processing of hydrocarbon gas mixtures S44 Cooling the crude synthesis gas. S444 Adjusting the temperature of crude synthesis gas S4444 Rapid cooling of crude synthesis gas

Claims

1. A method for obtaining synthesis gas from at least one waste by a gasification reaction combined with a reforming reaction by returning thermal energy, comprising the following steps: S1: supplying a supply material, particularly containing at least one solid, liquid, and / or gaseous waste, and a first oxidizing agent and / or a second oxidizing agent to a gasification reactor (30); S2: gasifying the supply material into a hydrocarbon gas mixture in the gasification reactor (30) in the presence of the first oxidizing agent and / or the second oxidizing agent under the supply of thermal energy, wherein at least one by-product is generated, the by-product particularly containing bottom ash and / or fly ash; S3: supplying the hydrocarbon gas mixture from the gasification reactor (30) to a reformer unit (40); and S4: processing the hydrocarbon gas mixture into crude synthesis gas in the reformer unit (40) by adding the first oxidizing agent and / or the second oxidizing agent. A method wherein at least a portion of the thermal energy generated in step S4 is returned to the gasification reactor (30) in order to provide at least a portion of the thermal energy supplied in step S2.

2. Step S4, which processes the hydrocarbon gas mixture in the reformer unit (40), includes, in addition to reforming the hydrocarbon gas mixture into crude synthesis gas in the plasma reformer (42), -S44: a step of cooling the crude synthesis gas, -S444: a step of adjusting the temperature of the crude synthesis gas in the heat retention chamber (44) to improve the reaction yield, and -S4444: a step of rapidly cooling the crude synthesis gas in the cooling zone (48). A method for obtaining the synthesis gas according to claim 1, comprising at least one of the steps.

3. A method for obtaining synthesis gas according to claim 1, wherein a portion of the thermal energy generated in step S4 is returned to the gasification reactor (30) via a first oxidizing agent and / or a second oxidizing agent.

4. A method for obtaining a synthesis gas according to claim 3, wherein the first oxidizing agent and / or the second oxidizing agent are heated by a heat exchanger (46), particularly a radiant heat exchanger or a ceramic heat exchanger, between the heat retention chamber (44) and the cooling zone (48) in order to return thermal energy.

5. The method for obtaining synthesis gas according to claim 3, characterized in that the return of the thermal energy is performed via a heat exchanger (46) between the heat retention chamber (44) and the cooling zone (48), the heat exchanger (46) heats a medium in an intermediate circuit, the medium then releases this heat to at least one heat sink through at least one second heat exchanger (47), the at least one heat sink includes a heat sink through a flow of a first oxidizer and / or a second oxidizer.

6. A method for obtaining synthesis gas according to claim 3, wherein at least one superheater is included between the heat exchanger (46) and the gasification reactor (30).

7. A method for obtaining synthesis gas according to claim 3, wherein at least a portion of the heated first oxidizing agent and / or second oxidizing agent accelerates step S2.

8. Step S2 includes isolating the bottom ash generated during the gasification and separating at least partially the fly ash generated during the gasification and carried by the hydrocarbon gas mixture and returning it to the gasification reactor (30), preferably the isolating further includes isolating the bottom ash via an ash discharge system (32), and preferably the separating and returning step includes separating the fly ash present in the hydrocarbon gas mixture after the gasification by an ash trap (34), particularly a cyclone, the method for obtaining synthesis gas according to claim 1.

9. A method for obtaining the synthesis gas according to claim 1, wherein the component ratio of hydrogen H2 and carbon monoxide CO in the synthesis gas is controlled by the mixing ratio of the first oxidizing agent and the second oxidizing agent.

10. The method for obtaining the synthesis gas according to claim 1, further comprising cooling the crude synthesis gas in a condenser unit (50) under separation of condensates after step S4.

11. The method for obtaining synthesis gas according to claim 1, wherein the operating pressure of the gasification reactor (30) and the operating pressure of the plasma reactor (42) are absolute pressures of 1 bar to 20 bar, preferably 1.5 to 4 bar.

12. The method for obtaining the synthesis gas according to claim 2, wherein the step of adjusting the temperature of the crude synthesis gas in the heat retention chamber (44) includes maintaining the temperature of the crude synthesis gas at least 850°C, preferably 1200°C, for at least 2 seconds.

13. A method for obtaining synthesis gas according to claim 1, wherein the first oxidizing agent comprises water vapor H2O and the second oxidizing agent comprises carbon dioxide CO2.

14. The method for obtaining the synthesis gas according to claim 1, wherein the gasification in step S2 is carried out by fluidized bed gasification, fixed bed gasification, screw gasification, or evaporator.

15. A method for obtaining synthesis gas according to claim 1, wherein a substance for absorbing and removing the generated acidic gas, particularly a metal carbonate, metal oxide, metal hydroxide, or bicarbonate, is supplied to the gasification in step S2.

16. A method for obtaining a synthesis gas according to claim 2, wherein, during the process, an arc discharge is further performed in the plasma modifier (42).

17. The method for obtaining the synthesis gas according to claim 3, comprising separating the interfering gas present in the synthesis gas by condensation and returning it to the reformer unit (40), wherein the interfering gas preferably includes carbon dioxide, and the carbon dioxide preferably forms a second oxidizing agent for returning the thermal energy generated in step S4.

18. A method for obtaining synthesis gas according to claim 1, wherein the supply material supplied in step S1 includes at least one gaseous waste.

19. An apparatus for obtaining synthesis gas from at least one type of waste by returning thermal energy and combining it with a reforming reaction in a gasification reaction, a. A supply material comprising, in particular, at least one solid, liquid and / or gaseous waste, and a storage container for a first oxidizer and / or a second oxidizer, b. A gasification reactor (30) for gasifying the supply material into a hydrocarbon gas mixture and at least one by-product, particularly bottom ash and / or fly ash, using the first oxidizing agent and / or second oxidizing agent under the supply of thermal energy, c. A reformer unit (40) for further adding the first oxidizing agent and / or the second oxidizing agent to treat the hydrocarbon gas mixture into crude synthesis gas, d. A cooling device for cooling the crude synthesis gas, An apparatus in which at least a portion of the thermal energy released in the reformer unit (40) is returned to the gasification reactor (30) in order to provide at least a portion of the thermal energy supplied to the gasification reactor (30).

20. The apparatus (1) according to claim 19, wherein the apparatus (1) is configured to perform the method described in claim 1.

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