Method for obtaining a synthesis gas from waste products via a gasification reaction in conjunction with a reforming reaction with thermal energy recirculation

Abstract

The present invention relates to a method and apparatus for obtaining synthesis gas from one or more wastes by combining a reforming reaction and a gasification reaction under thermal energy recirculation. The above method comprises step s1 of introducing a feedstock and a first and / or second oxidizing agent into a gasification reactor, wherein the feedstock comprises, in particular, at least one solid, liquid and / or gaseous waste. Additionally, the above method comprises step s2 of gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct within the gasification reactor while supplying thermal energy using the first and / or second oxidizing agent, wherein the byproduct comprises, in particular, bottom ash and / or fly ash. Additionally, the above method comprises step s3 of supplying the hydrocarbon gas mixture from the gasification reactor to a reformer unit, and step s4 of treating the hydrocarbon gas mixture into a raw synthesis gas within the reformer unit while supplying the first and / or second oxidizing agent, wherein at least a portion of the thermal energy released in step s4 is recirculated to the gasification reactor to provide at least a portion of the thermal energy supplied in step s2.

Description

Technology Field

[0001] The present invention relates to a method and apparatus for obtaining synthesis gas from waste through a combination of a reforming reaction and a gasification reaction accompanied by thermal energy recirculation. Background Technology

[0002] Currently, large-scale production of fossil-based synthesis gas is carried out through energy-intensive processes such as natural gas reforming or coal gasification. In this specification, synthesis gas is defined as a mixture of carbon monoxide (CO) and hydrogen (H2). However, various novel processes for obtaining synthesis gas still face several problems.

[0003] For example, in biogas reforming, syngas is produced in a decentralized manner, resulting in high costs associated with small-scale plants, high investment and operating expenses, and logistical inefficiencies. Consequently, the price of syngas becomes significantly higher than that of natural gas.

[0004] Processes combining electrolysis with the water gas shift reaction or co-electrolysis consume very high electrical energy and have low energy efficiency, resulting in higher synthesis gas prices.

[0005] In a thermally operated waste-to-syngas process, a portion of the waste feedstock is oxidized or combusted to supply the energy required for thermal reforming to produce syngas. This results in the release of large amounts of carbon dioxide, which cannot be efficiently utilized in subsequent processes.

[0006] In thermal processes for obtaining synthesis gas from waste, it is known that carbon-containing waste is converted into synthesis gas under the supply of an oxidizing agent, such as oxygen or steam, with gasification occurring first. The gaseous fractions generated during gasification have varying chain lengths, and some are condensed and distributed as crude oil substitutes. After gasification, the gaseous fractions can be used for heat and electricity production. However, due to the very high requirements for individual fractions and the composition of the waste used in terms of economic feasibility for industrial applications, existing gasification plants are specialized according to the type or purity of the waste, and their scope of application is limited. Furthermore, useful byproducts of gasification, such as various forms of ash including bottom ash, fly ash, and pond ash, are not recycled. In addition, potential fluctuations in the waste supply volume are detrimental to the safe and smooth operation of the gasification reactor. It also makes it difficult to guarantee a continuous supply of the hydrocarbon mixture product stream.

[0007] In addition, a process for purifying unrefined raw gas through reforming, which converts a hydrocarbon-containing gas mixture into hydrogen-rich synthesis gas from which contaminants have been removed, is known; however, recycling of already used materials is not performed in waste management. In the known reforming process, a hydrocarbon mixture such as natural gas, light gasoline, methanol, or biomass is reformed into synthesis gas as a starting material with an oxidizing agent, such as steam, under a supply of heat.

[0008] Overall, the disclosed processes entail high energy consumption throughout the entire process chain from primary energy sources to final products, which can make electrification uneconomical. This is attributed, for example, to waste heat loss, unused feedstocks, or unused oxidizers. Non-electric processes utilizing waste generate carbon dioxide by using oxygen or air as an oxidizer, and the continuous emission of this pollutant eventually leads to a degradation of the synthesis gas quality. The problem to be solved

[0009] Based on the disclosed prior art, the object of the present invention is to provide an improved process for obtaining synthesis gas from waste through a combination of a reforming reaction and a gasification reaction under thermal energy recirculation, and a corresponding apparatus.

[0010] In particular, the focus is on improving energy efficiency and minimizing by-products. Accordingly, one of the objectives of the present invention is to provide an improved process and system for obtaining synthesis gas from waste, which aims for the efficient utilization of waste and the minimization of energy consumption. means of solving the problem

[0011] The above problem is solved by the method according to claim 1. Advantageous additional embodiments are derived from the dependent claims, description, and drawings.

[0012] Accordingly, a method for obtaining synthesis gas from at least one waste is proposed through a combination of a reforming reaction and a gasification reaction under thermal energy recirculation. The method comprises a first step (S1) of introducing a feedstock and a first and / or second oxidizing agent into a gasification reactor, wherein the feedstock comprises, in particular, at least one solid, liquid and / or gaseous waste. Additionally, the method comprises a second step (S2) of gasifying the feedstock into a hydrocarbon gas mixture within the gasification reactor while supplying thermal energy using the first and / or second oxidizing agent, wherein at least one byproduct is produced, wherein the byproduct comprises, in particular, bottom ash and / or fly ash. Additionally, the method comprises a third step (S3) of supplying a hydrocarbon gas mixture from a gasification reactor to a reformer unit, and a fourth step (S4) of treating the hydrocarbon gas mixture into a raw synthesis gas within the reformer unit while supplying a first and / or second oxidizer, wherein at least a portion of the thermal energy generated in step S4 is recirculated to the gasification reactor to provide at least a portion of the thermal energy supplied in step S2.

[0013] In this specification, "waste product" refers to a reactant of a process for obtaining synthesis gas. Typically, suitable reactants are those produced as waste in a previous process. However, this is not a mandatory requirement for the suitability of the synthesis gas acquisition process. Accordingly, in this specification, "waste" also includes reactants that are specially produced but are not actually obtained from waste.

[0014] Here, waste is understood to be, in particular, carbon-containing materials, in particular methane, propane, biogas, plastics, residual waste, wood waste, biomass, lignin and / or paper waste, or mixtures containing said materials, which are, among other things, generated as residues, by-products and / or co-products from prior processes such as cracking, recycling and / or Fischer-Tropsch synthesis.

[0015] By combining a reformer unit with an upstream gasification reactor, it becomes possible to produce high-quality syngas from various wastes. The utilization of waste promotes a sustainable circular economy and reduces the demand for valuable hydrocarbon-containing feedstocks for syngas production. The use of waste as a feedstock contributes to reducing landfill waste and supports sustainable resource utilization. At the same time, the demand for fossil resources decreases. Feedstocks can be supplied from specialized waste material containers, which serve as intermediate storage to compensate for supply bottlenecks or fluctuations. This ensures the smooth operation of the plant and the continuous production of high-quality syngas. As a result, continuous plant utilization and a constant syngas flow can be guaranteed. Additionally, liquid and / or gaseous materials can be added to the process. If only liquid materials are used, an evaporator can be utilized instead of a gasification reactor. Separating syngas production into four stages lowers the requirements for feedstock while expanding the range of applications for the syngas. Another advantage is that solid plastic waste can be introduced into the process as a feedstock, whereas otherwise it would have to be treated separately during the waste disposal process due to interfering chemical properties. The use of a first oxidizer and / or a second oxidizer supplied to the gasification reactor at variable mixing ratios enables precise control of gasification conditions, such as reaction temperature and products. This allows for specific adjustment of the composition of the synthesis gas. Furthermore, gasification and reforming conditions can be precisely controlled. This improves the process's adaptability to various feedstock and product requirements. In step S2, gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct represents the initial step of producing synthesis gas from the feedstock. Gasification is an endothermic reaction.During gasification, the carbon-containing energy feedstock is converted into a gaseous hydrocarbon gas mixture and byproducts through chemical conversion via the supply of thermal energy. Gasification is carried out particularly at temperatures between 400°C and 650°C. Recirculation of thermal energy from the reformer unit to the gasification reactor reduces the external energy requirements for gasification in the S2 stage and increases the overall energy efficiency of the process. As a result, a cost-effective and sustainable process design becomes possible. In addition, thermal energy feedback enables a uniform supply of thermal energy to the gasification reactor, minimizing fluctuations in energy input and enabling stable synthesis gas production.

[0016] To obtain raw synthesis gas, a hydrocarbon gas mixture is fed to a reformer unit in step S3. In step S4, subsequent processing of the hydrocarbon gas mixture within the reformer unit produces raw synthesis gas through the supply of additional first and / or second oxidizers. The synthesis gas obtained in step S4 has a purity suitable for various applications, such as chemical synthesis.

[0017] In the fourth step (S4), a portion of the thermal energy present in the crude synthesis gas is removed and returned to the gasification reactor. This returned thermal energy provides a portion of the thermal energy required in the second step (S2), which in turn improves the energy efficiency of the process.

[0018] In an alternative embodiment, the process comprises a first step (S1) of substantially or entirely supplying a gaseous feedstock to a reformer unit, wherein the gaseous feedstock comprises a hydrocarbon gas mixture. The process also comprises a subsequent step (S4) of substantially or entirely converting the gaseous feedstock into crude synthesis gas in the reformer unit with the supply of a first and / or second oxidizer, wherein at least a portion of the thermal energy released in step S4 is recycled.

[0019] In a further preferred embodiment of the method, the step (S4) of processing a hydrocarbon gas mixture in a reformer unit comprises, in addition to reforming the hydrocarbon gas mixture into a crude synthesis gas in a plasma reformer, at least one step from cooling the crude synthesis gas (S44), controlling the temperature of the crude synthesis gas in a thermal residence chamber to increase the reaction yield (S444), and quenching the crude synthesis gas in a cooling zone (S4444).

[0020] In step S44, the synthesis gas can be cooled by a heat exchanger, which can return thermal energy to the entire system through a heat transfer medium. By utilizing the thermal energy released during the cooling of the crude synthesis gas, the energy efficiency of the process can be improved. By placing a heat exchanger between the heat retention chamber and the cooling zone, the waste heat from the adjacent plasma reformer and the thermal energy of the generated synthesis gas can be utilized to the fullest extent without interfering with reactions within the process. Temperature control in the heat retention chamber in step S444 contributes to improved reaction yield, the decomposition of contaminants in the gas, and the control of the product composition of the crude synthesis gas. Only a small amount of thermal energy is required to maintain the temperature of the crude synthesis gas in the heat retention chamber. In step S4444, quenching of the crude synthesis gas in the cooling zone allows for the rapid reduction of the temperature of the high-temperature crude synthesis gas. This enables the rapid removal of existing thermal energy from the crude synthesis gas. This prevents unwanted additional reactions from occurring within the gas. Water cooling by injection is a cost-effective method for this purpose. Water cooling has the additional advantage of not degrading the quality of the synthesis gas.

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

[0022] Process efficiency can be significantly improved by target-orientedly recirculating the energy released in the S4 stage back to the gasification reactor through the first and / or second oxidizers. This integration enables the optimal utilization of thermal energy, further reducing external energy requirements. Recirculation through the oxidizers also contributes to more flexible control of the gasification process, as it allows for precise regulation and uniform distribution of input energy. This design not only enhances process stability but also enables fine-tuning of reaction conditions, contributing to the continuous production of high-quality synthesis gas.

[0023] In a further preferred embodiment of the process, the first and / or second oxidizer being recirculated for the recirculation of thermal energy is heated through a heat exchanger located between the heat retention chamber and the cooling zone, in particular a radiant heat exchanger or a ceramic heat exchanger.

[0024] Post-treatment of the recirculated first and / or second oxidizer via a heat exchanger enables efficient post-treatment of the recirculated oxidizer, which has the advantage of optimizing its quality and reactivity in the gasification process. For example, the use of evaporator-type heat exchangers, such as radiative heat exchangers or ceramic heat exchangers, ensures effective heat transfer from the heat retention chamber or cooling zone. This allows for the meaningful recycling of thermal energy in the process, thereby improving energy efficiency and reducing the overall energy requirements of the process. Furthermore, post-treatment in the heat exchanger ensures homogeneous conditioning of the oxidizer, enabling a stable and controllable reaction in the gasification reactor. This contributes to improved process stability, consistent synthesis gas quality, and an extended service life of process components.

[0025] In an additional embodiment of the process, thermal energy is returned through a heat exchanger between a heat retention chamber and a cooling zone, said heat exchanger heats a medium in an intermediate circuit, said medium then transfers heat to at least one heat sink through at least one second heat exchanger, said at least one heat sink comprises a heat sink having a stream of a first and / or second oxidizing agent.

[0026] Transferring waste heat from a plasma reformer to an oxidant stream using an intermediate circuit filled with a heat transfer medium has the advantage of reducing losses when the waste heat circuit and the oxidant circuit are far apart. Additionally, the risk of contamination between the two circuits is low. The temperature levels of the oxidant and waste heat circuits can be freely controlled by the intermediate circuit. This prevents damage to the heat exchanger caused by excessive temperatures. Furthermore, process heat can be transferred to other destinations.

[0027] In an additional embodiment of the process, 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 and / or second oxidizer can be further heated, particularly to 650°C, thereby further increasing the heat input of the first and / or second oxidizer into the gasification reactor. This reduces the primary energy requirement of the gasification reactor and improves the efficiency of the entire process. In addition, the use of at least one superheater serves to control the amount and composition of the hydrocarbon gas mixture produced by controlling the gasification conditions.

[0029] In a further preferred embodiment of the process, at least a portion of the post-treated first and / or second oxidizing agent facilitates the process step (S2).

[0030] The targeted use of treated first and / or second oxidizers increases the reaction rate and efficiency of the gasification process, achieving a faster and more complete conversion of the feedstock into a hydrocarbon gas mixture. This is attributed to the rapid removal of reaction products from the gasification reactor, in addition to heat input. This improves not only process productivity but also energy utilization and the consistency of synthesis gas quality. Furthermore, accelerated reactions enable reduced residence times in the gasification reactor, leading to increased throughput and the efficient utilization of plant resources.

[0031] In a further preferred embodiment, the process comprises separating bottom ash generated during gasification in step S2 and at least partially separating fly ash generated during conversion and carried by the hydrocarbon gas mixture and returning it to the gasification reactor, wherein the separation preferably further comprises separating bottom ash through an ash discharge system, and the separation and return step preferably comprises separating fly ash present in the hydrocarbon gas mixture after gasification through an ash trap, in particular a cyclone.

[0032] In the gasification process, ash-type byproducts, such as bottom ash or fly ash, are generated. Due to the high reaction temperatures within the gasification reactor, these byproducts also possess a high average temperature; separating and returning them to the reactor contributes to maintaining high temperature levels during gasification. The separation and recirculation of these high-temperature byproducts contribute to improving the purity of the final gasification product and enhancing the energy efficiency of the overall process.

[0033] The ash discharge system for bottom ash separation ensures the continuous and smooth operation of the gasification reactor by preventing sedimentation and clogging. By enabling the efficient and controlled removal of byproducts, the system maintains stable operating conditions and extends the plant's service life. Furthermore, the separate separation of bottom ash facilitates recycling or environmentally friendly disposal. This contributes to enhancing the sustainability of the entire process by allowing for the recovery of valuable resources or the proper treatment of waste. Additionally, this ash discharge system allows the separated bottom ash to be transported back to the gasification reactor, enabling the recycling of high-temperature ash generated during gasification.

[0034] Fly ash particles generated during gasification can be removed from the final product of the hydrocarbon gas mixture using ash collectors, such as cyclones, or other filtration methods. Efficient removal of fly ash increases the purity of the hydrocarbon gas mixture, thereby improving the quality of the resulting synthesis gas. This ensures the purity of the hydrocarbon gas mixture for further processing on one hand, while enabling the additional utilization of undesirable byproducts on the other. The use of cyclones enhances process stability by enabling reliable and mechanically robust particle separation even at high temperatures and flow rates. Furthermore, targeted separation and recirculation of fly ash prevents deposits on downstream components, reducing maintenance requirements and extending the plant's service life. Fly ash recirculation enables the additional utilization of residual materials, increasing process resource efficiency and contributing to waste minimization. Additionally, the separation and recirculation of fly ash contained in the hydrocarbon gas mixture upstream of the plasma reformer improves the overall process energy efficiency by recirculating byproducts. The high temperature of the fly ash inside the gasification reactor is utilized to reduce the high energy consumption required to heat it to the temperature necessary for the reaction.

[0035] In a further preferred embodiment of the process, the ratio of hydrogen (H2) and carbon monoxide (CO) components in the synthesis gas is controlled through the mixing ratio of the first oxidizer and the second oxidizer.

[0036] The ratio of hydrogen and carbon monoxide in the synthesis gas, i.e., the synthesis gas ratio, is controlled by adjusting the mixing ratio of the oxidant supplied to the gasification reactor and the reformer unit. The synthesis gas ratio can be controlled through the mixing ratio of water vapor and carbon dioxide. This allows for variable adjustment of the composition and quality of the synthesis gas, while also ensuring consistent product quality. A constant mixing ratio of oxidants hinders the system's ability to adapt to variations in the feedstock composition. In conventional processes, the mixing ratio of carbon monoxide and hydrogen is adjusted via the water gas shift reaction. In this process, such adjustment is unnecessary, which saves resources and improves the energy efficiency of the overall system. Control of the synthesis gas ratio by the mixing ratio of oxidants is made possible by the use of non-catalytic, i.e., thermal or plasma-based, reforming in the S4 stage.

[0037] In an additional preferred embodiment of the process, the process includes a step of cooling the crude synthesis gas in a condenser unit while separating the condensate after step S4.

[0038] This cooling stage in the condenser unit processes the crude synthesis gas to separate residual fly ash particles, salts, volatile heavy metals, and residual steam from the crude synthesis gas stream. The separated substances are subsequently removed from the synthesis gas stream by condensate to obtain pure synthesis gas. Furthermore, the targeted temperature reduction optimally prepares the synthesis gas for subsequent process steps, increasing process efficiency and flexibility. The separation of condensate also enables the removal of unwanted concomitant substances, such as moisture or condensable compounds, thereby improving the purity and quality of the synthesis gas. Additionally, the condenser unit contributes to effective heat recirculation by extracting excess heat from the gas stream, thereby increasing the energy efficiency of the overall process. This integration also minimizes the effort required for downstream gas purification.

[0039] In a further preferred embodiment of the process, the operating pressure of the gasification reactor and the operating pressure of the plasma reformer are an absolute pressure of 1 bar to 20 bar, preferably 1.5 bar to 4 bar.

[0040] The required operating pressure of the process within the reactor is an absolute pressure of 1 to 20 bar to obtain a high reaction yield of synthesis gas and enable the reaction stages of gasification and reforming. Additionally, the operating pressure of the process within the reactor can be set to an absolute pressure of 1.5 to 4 bar. Furthermore, the process stages are inherently isobaric. This also means that the compressor needs to operate less, which is reflected in lower energy consumption. Moreover, within this optimal pressure range, low-pressure pipes, which are cheaper than high-pressure pipes, can be used. This reduces mechanical stress on the reactor walls and components, extending the service life of the plant and reducing maintenance costs. Selecting an operating pressure in a lower range also reduces the requirements for the plasma reformer used in stage S4, as high gas pressure makes stable operation of the plasma reformer difficult.

[0041] In a further preferred embodiment of the method, the step of controlling 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 1,200°C, for at least 2 seconds.

[0042] Maintaining crude synthesis gas at a temperature of at least 850°C, preferably 1,200°C, for 2 seconds ensures combustion conditions for a waste incineration plant that comply with §6 of the 17th Decree (BImSchV) for the implementation of the Federal Pollution Control Act (Bundes-Immissionsschutzgesetz). This ensures compliance with specific pollutant emission limits. In addition, maintaining the temperature can increase the yield of the reforming reaction.

[0043] In a further preferred embodiment of the process, 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 reaction partners and oxidizers in gasification and reforming. As oxidizers, steam and carbon dioxide are supplied to the entire system in adjustable mixing ratios when participating in the reaction, and these ratios may consist solely of pure substances. They have a significant impact on reaction temperature and product composition. As oxidizers, steam and carbon dioxide have been technically proven multiple times, require only limited safety precautions, and are available at low cost. In the case of carbon dioxide, this effectively constitutes the recycling of pollutants. Steam contributes to increasing the hydrogen content in synthesis gas by supplying hydrogen to the reforming reaction, thereby providing high-quality, versatile products. At the same time, carbon dioxide, acting as a secondary oxidizer, enables the utilization of potential waste or byproducts from other processes, contributing to the promotion of the circular economy and the reduction of carbon dioxide emissions. The combination of the two oxidizers allows for precise control of gasification and reforming conditions, as it enables flexible adjustment of reaction temperature and product composition. Furthermore, the simultaneous use of steam and carbon dioxide achieves effective feedstock conversion during gasification, thereby increasing process efficiency and reducing the demand for external resources. Overall, this embodiment leads to more sustainable, cost-effective, and environmentally friendly synthesis gas production.

[0045] In a further preferred embodiment where gasification in the S2 stage is performed in a fluidized bed gasifier, a fixed bed gasifier, a screw gasifier, or an evaporator, using fluidized bed gasification in the gasification reactor accelerates the gasification process by having the superheated oxidizer act as a fluidizer for the solid layer within the gasification reactor. This is achieved by the high average temperature of the superheated oxidizer. Gasification in a fluidized bed gasifier offers the advantage of high variability of the feedstock. Additionally, there is excellent controllability over the feedstock and gas input within the reactor, as well as excellent scalability over a wide power range. In screw gasification, a reactor with a rotating screw designed with a special geometry is used. This ensures optimal heat transfer from the feedstock to the reactor wall and excellent mixing. Additionally, a similar gasification process can be used.

[0046] In a further preferred embodiment of the process, a material, in particular a metal carbonate, a metal oxide, a metal hydroxide, or a hydrogen carbonate, is added to the gasification of step S2 to combine the generated acidic gas.

[0047] Adding materials such as metal carbonates, metal oxides, metal hydroxides, or bicarbonates to the gasification reactor is intended to bind acidic gases that may be generated during the gasification reaction. In particular, when using materials containing polyvinyl chloride, acidic gases, especially hydrogen chloride or hydrogen fluoride, may be generated, which can cause corrosion problems in subsequent process steps.

[0048] In a further preferred embodiment of the process, an arc discharge is additionally performed in a plasma reformer during processing.

[0049] Arc discharge generates high-energy plasma, enabling the efficient activation and decomposition of molecules, particularly stable compounds that are difficult to convert within hydrocarbon gas mixtures. This leads to improved reaction efficiency and higher yields of valuable synthesis gas components such as hydrogen and carbon monoxide. Furthermore, the use of plasma reactions allows for the targeted stimulation of specific reaction pathways, enabling precise control of product composition. Additionally, the high temperature and energy of the plasma help optimize the conversion of residues and byproducts, thereby enhancing the overall economic efficiency and sustainability of the process.

[0050] In a further preferred embodiment, the process comprises separating impurity gases present in the synthesis gas by condensation and returning them to a reformer unit, wherein the impurity gases preferably include carbon dioxide, and the carbon dioxide preferably forms a second oxidizer for recirculating the thermal energy generated in step S4.

[0051] The purity requirements for synthesis gas are achieved by separating impurity gases that may be present in the synthesis gas stream. In particular, while carbon dioxide occurs as an impurity gas, other gases may also be present in the synthesis gas product stream. The separation of impurity gases can be performed using various techniques such as scrubbing, membrane separation, or pressure or temperature swing adsorption. The separation technique selected depends on the purity requirements of possible subsequent processes. For example, if synthesis gas is used in the phosgene route, carbon dioxide must be almost completely separated, as it may only be acceptable in the ppm range.

[0052] In a further preferred embodiment, the feedstock supplied in step S1 comprises substantially or entirely at least one gaseous waste, and step S2, which gasifies the feedstock, is omitted.

[0053] In this embodiment, the feedstock supplied in step S1 comprises substantially or entirely at least one gaseous waste. As a result, since the feedstock is already in a gaseous state, a subsequent step S2 to gasify the feedstock is not required. This means that the high primary energy actually required in step S2 is not needed, and the energy requirements of the process are reduced.

[0054] Accordingly, an apparatus is proposed for obtaining synthesis gas from at least one waste through a combination of a reforming reaction and a gasification reaction under thermal energy recirculation. The apparatus comprises a storage facility for a feedstock and a first and / or second oxidizer, wherein the feedstock comprises, in particular, at least one solid, liquid and / or gaseous waste. Additionally, the apparatus comprises a gasification reactor for gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct through the supply of the first and / or second oxidizer and thermal energy, wherein the byproduct comprises, in particular, bottom ash and / or fly ash. Additionally, the apparatus comprises a reformer unit for treating the hydrocarbon gas mixture into crude synthesis gas while supplying the first and / or second oxidizer, and a cooling device for cooling the crude synthesis gas, wherein at least a portion of the thermal energy released from the reformer unit is recirculated to the gasification reactor to provide at least a portion of the thermal energy supplied to the gasification reactor.

[0055] The device supplies waste stored in a waste storage container to a gasification reactor in a solid state, which may also be in a liquid or gaseous state. A process step is performed in the gasification reactor to gasify the feedstock and oxidizer into a hydrocarbon gas mixture and byproducts. In addition to the heat generated, bottom ash and / or fly ash are also formed as byproducts; however, for energy efficiency, these are removed from the hydrocarbon gas mixture stream and recirculated to the gasification reactor to recycle the residual heat of the material after gasification. The hydrocarbon stream is then supplied to a reformer unit, where the hydrocarbon stream and oxidizer are reformed into crude synthesis gas. Additionally, a step is performed to process the crude synthesis gas in the reformer unit to finally obtain synthesis gas.

[0056] In a preferred embodiment, the device is configured to perform a process according to one of the previous embodiments.

[0057] In addition, the process according to step S4 may include a step of scrubbing acidic synthesis gas with a scrubbing solution, in particular Selexol and / or Rectisol, in a scrubbing column to provide synthesis gas.

[0058] By cleaning acidic synthesis gas with cleaning solutions such as Selexol and / or Rectisol, the gas is effectively purified from unwanted impurities, such as carbon dioxide, hydrogen sulfide, and other acidic gases, to obtain high-purity synthesis gas. This improves not only the quality of the synthesis gas but also its versatility for downstream applications, such as the chemical industry or energy production. Using Selexol and Rectisol as cleaning solutions enables 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 hazardous or corrosive gases within the synthesis gas. Overall, this leads to better product quality above all else.

[0059] After the step of washing the acidic synthesis gas with synthesis gas, the process may include the steps of initially separating impurity gases, storing the synthesis gas in a storage tank, and preferably compressing the synthesis gas.

[0060] Storing synthesis gas in storage tanks allows for buffering the product stream. Buffering facilitates responding to fluctuating demand for synthesis gas. Additionally, it can compensate for variations in synthesis gas production. Compressing synthesis gas not only reduces the volume required for storage but also makes it possible to supply it directly to gas networks and pipelines at regulated pressure levels. Effects of the invention

[0061] The method and apparatus according to the present invention provide a sustainable process capable of improving energy efficiency, minimizing by-products, and producing high-quality synthetic gas from various wastes. Brief explanation of the drawing

[0062] Preferred additional embodiments of the invention are described in more detail in the following description of the drawings. The drawings represent the following: Figures 1a and 1b schematically show the flowchart of a process for obtaining synthesis gas from waste using thermal energy recirculation. Figure 2a schematically illustrates a process for obtaining synthesis gas from waste using thermal energy recirculation. Figure 2b schematically illustrates a process for obtaining synthesis gas from waste through thermal energy recirculation using an intermediate circuit. Figure 3 schematically shows the post-treatment of synthesis gas. Figure 4 schematically illustrates the process of obtaining synthesis gas from waste and the post-treatment of the synthesis gas. Specific details for implementing the invention

[0063] FIGS. 1a and 1b illustrate a process for obtaining synthesis gas from waste in an exemplary flowchart. The flowchart shows four steps (S1 to S4). The first step (S1) involves the input of a feedstock, the second step (S2) involves the gasification of the feedstock, the third step (S3) involves supplying a hydrocarbon gas mixture to a reformer unit, and the fourth step (S4) involves the treatment of the hydrocarbon gas mixture in the reformer unit.

[0064] In the first step (S1), both the feedstock and the oxidant stream are supplied to the gasification reactor. The oxidant stream may consist of a first oxidant and a second oxidant in a controllable mixing ratio. Since the mixing ratio can be changed in both directions, both the pure substance of the first or second oxidant and a mixture of the first and second oxidants may be present. In the example presented, the oxidant stream is understood to be a mixture of water vapor and carbon dioxide. Additionally, the first and second oxidants may be carbon monoxide (CO), oxygen (O2), or hydrogen (H2). The feedstock may consist of solid, liquid, and / or gaseous waste. For example, the waste may include solid plastic waste. Additionally, carbon sources within the system, such as carbon dioxide, or organic waste, such as biomass or sorting residues, may be used as waste. The feedstock (S1) and the oxidant stream are supplied by a feed system. The supply system is implemented, for example, as a screw conveyor, and all types of supply systems such as belt conveyors, inclined conveyors, or industrial trucks can be used.

[0065] In the second stage (S2), the feedstock supplied in the first stage is gasified by an oxidant stream in a gasification reactor. Due to the endothermic nature of the gasification reaction in the second stage, a supply of thermal energy is required. The reaction products are a mixture of hydrocarbon gases and at least one byproduct. Additionally, two, three, four, or any number of byproducts may be produced, with various types of ash being the most common byproduct. Bottom ash and fly ash are produced as byproducts. In the second stage, the supply of external thermal energy is required to provide the high process temperature necessary for gasification. In the example shown in Fig. 1, thermal energy is provided by an electric heater and the recirculation of a high-temperature oxidant. Additionally, thermal energy can be provided by heating or recirculating any form of thermal energy within the system. In the example shown in Fig. 1, a fluidized bed gasifier is used as the gasification reactor. Additionally, an entrained flow gasifier or a fixed bed gasifier may 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 the S2 stage is deposited at the bottom of the reactor from the hydrocarbon gas mixture within the gasification reactor. The deposited bottom ash is separated from the gasification reactor through an ash discharge system.

[0067] The fly ash generated during gasification in the fluidized bed gasifier of the second stage (S2) is discharged at the top of the reactor along with the hydrocarbon gas mixture. The fly ash constitutes only a small amount of the material stream. After the gasification reactor, the material stream passes through an ash collector to separate the fly ash from the hydrocarbon gas mixture. The ash collector is formed as a cyclone. Additionally, the ash collector can be formed as any separation system, such as a filter or adsorption.

[0068] In the third step (S3), the ash-removed hydrocarbon gas mixture is fed from the gasification reactor to the reformer unit. The hydrocarbon gas mixture is fed directly to the reformer unit, for example, via a pipeline, and further processed into synthesis gas. In the third step (S3), the gasification reaction of step S2 and the reforming reaction of step S4 are combined through the gasified medium. Additionally, it is possible to incorporate intermediate stages, such as a filter unit or a transfer unit for the medium, into the combination.

[0069] In the fourth step (S4), the hydrocarbon gas mixture is processed into crude synthesis gas in the reformer unit. An oxidant stream is added to the reformer unit to enable the reaction. The oxidant stream consists of first and second oxidants in a controllable mixing ratio. The mixing ratio can be changed in both directions, allowing for the presence of pure substances. The oxidants in the oxidant stream of step S4 correspond to the first and / or second oxidants of the first step (S1), and the mixing ratio may differ from that of the first step (S1). In the example shown, water vapor is used as the first oxidant and carbon dioxide as the second oxidant. After the oxidant stream is added to the plasma reformer within the reformer unit, a reforming reaction is carried out to produce crude synthesis gas. Alternatively, a steam reformer may be used instead of a plasma reformer. The plasma reformer is driven by plasma drivers. This provides the thermal energy required for the high reaction temperature. Due to the high temperature requirement, the medium outlet temperature of the plasma reformer is between 1,100°C and 1,600°C. In the plasma reformer, a hydrocarbon gas mixture and an oxidant stream are mixed to generate a non-thermal plasma. The non-thermal plasma then reforms the hydrocarbon gas mixture and the oxidant stream into a crude synthesis gas. The plasma reformer can perform the reforming in the form of an arc discharge. The synthesis gas generated in the plasma reformer consists of carbon monoxide and hydrogen, and their mixing ratio can be controlled by the mixing ratio of the oxidant stream. The absolute pressure during the reaction within the plasma reformer is 1 bar to 20 bar. Additionally, an operating pressure of 1.5 bar to 4 bar is also possible.

[0070] As shown in FIG. 1a, the heat exchanger can return the thermal energy released from the reformer unit to stage S2. This thermal energy can be used again for gasification in stage S2. As shown in FIG. 1b, the treatment of the hydrocarbon gas mixture in stage S4 may include additional steps such as cooling of the crude synthesis gas (S44), temperature control of the crude synthesis gas in a heat retention chamber to increase the reaction yield (S444), and quenching of the crude synthesis gas in a cooling zone (S4444).

[0071] In step S44, the cooling of the crude synthesis gas provides thermal energy, which can be recirculated back to step S2. In the cooling step, a portion of the thermal energy transferred from the plasma reformer to the crude synthesis gas in step S4 is transferred to a heat exchanger. In the example shown, the heat exchanger is a ceramic radiation heat exchanger. Heat exchangers made of other materials, such as iron or stainless steel, may also be used. The heat exchanger transfers the thermal energy of the synthesis gas to the oxidant stream. The oxidant stream is supplied separately or separated from the product stream of the synthesis gas by condensation and returned. The oxidant stream is fed to the heat exchanger. The oxidant stream is evaporated and superheated by the heat exchanger. It is also possible to evaporate only the oxidant stream. In this design, the heat exchanger is used as an evaporator. Alternatively, in step S4, the heat exchanger can first transfer the thermal energy released from the plasma reformer to an intermediate circuit filled with a heat transfer medium. Thermal oil is used as the heat transfer medium, but any heat transfer medium such as molten salts, liquid metal, water, alcohol-water solutions, or salt-water solutions can be used. The heat transfer medium then transfers thermal energy to the oxidant stream through another heat exchanger. This causes the oxidant stream to evaporate, and the oxidant stream may also evaporate and superheat. The thermal energy of the oxidant stream is then transferred to the gasification reactor in step S2. Increasing the thermal energy of the oxidant stream and recirculating the oxidant stream facilitates process step S2. This can again provide part of the thermal energy required in step S2.

[0072] In the additional step of the hydrocarbon gas mixture treatment of step S4, the temperature of the crude synthesis gas in the thermal residence chamber of the reformer unit is controlled in step S444. This control is achieved by maintaining the temperature at 850°C for at least 2 seconds. Additionally, control may be achieved at a temperature of 850°C or higher for a time longer than 2 seconds.

[0073] In an additional step of the treatment of the hydrocarbon gas mixture S4, the quenching of the crude synthesis gas in the cooling zone takes place in step S4444. Here, the crude synthesis gas passes through the cooling zone before being discharged from the reformer unit. Water is used for quenching, but oil or gas may be used as alternatives. 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 a schematic diagram of the first stage of the process for obtaining synthesis gas from waste.

[0075] FIG. 2a shows a waste storage container (10) in which a feedstock is stored. Solid plastic waste is used as the feedstock. The feedstock is transported to a gasification reactor (30) via a supply system (20). The supply system (20) is designed as a screw conveyor. In the example shown in FIG. 2a, the gasification reactor (30) is designed as a vortex gasifier. Additionally, an oxidizing agent stream is supplied to the gasification reactor (30). The oxidizing agent stream used here is a mixture of a first oxidizing agent (e.g., water vapor) and a second oxidizing agent (e.g., carbon dioxide). In the gasification reactor (30), the feedstock is gasified together with the oxidizing agent stream. In addition to the hydrocarbon gas mixture, ash of the form of bottom ash and fly ash is generated during this process. The bottom ash generated in the gasification reactor is deposited at the bottom of the reactor after the reaction. The bottom ash is separated from the gasification reactor (30) by an ash discharge system (32). Fly ash is discharged along with a stream of hydrocarbon gas mixture at one end of the gasification reactor (30). The stream of hydrocarbon gas mixture and fly ash passes through an ash collector (34), which is designed as a cyclone in a later example. 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, purified from the fly ash, is fed to a reformer unit (40) after the ash collector (34).

[0076] The reformer unit (40) includes a plasma reformer (42). A hydrocarbon gas mixture and a first and / or second oxidizer are supplied to the plasma reformer (42) via an oxidizer stream. The same oxidizer used in the gasification reactor (30) is used as the oxidizer stream, but the mixing ratio may differ from the mixing ratio of the oxidizer stream in the gasification reactor (30). The oxidizers used here are water vapor and carbon dioxide. After the oxidizer stream is added to the plasma reformer (42), a reforming reaction takes place in the reformer unit to produce crude synthesis gas. The temperature of the crude synthesis gas is controlled in the heat retention chamber (44) of the reformer unit (40) after the plasma reformer (42). The temperature is controlled by maintaining 850°C for 2 seconds. The crude synthesis gas also undergoes a multi-stage cooling process. In one stage of the cooling process, the crude synthesis gas transfers some of its thermal energy to a heat exchanger (46). The heat exchanger (46) is a ceramic radiation heat exchanger. The heat exchanger (46) transfers a portion of the thermal energy of the crude synthesis gas to an oxidant stream, which is supplied separately or separated from the product stream of the synthesis gas by condensation by a gas separator (90) and returned. The oxidant stream is evaporated, and the oxidant stream can also be evaporated and superheated. In this embodiment, the heat exchanger (46) is an evaporator.

[0077] An oxidant stream with increased thermal energy is supplied to a gasification reactor (30). Gasification in the gasification reactor (30) is promoted by increasing the thermal energy of the oxidant stream and recirculating the oxidant stream. This provides some of the thermal energy required in the gasification reactor (30). Additionally, the synthesis gas produced from the hydrocarbon gas mixture is processed by quenching the crude synthesis gas in a cooling zone (48). The crude synthesis gas passes through the cooling zone (48) before being discharged from the reformer unit (40). Water is used for quenching. The crude synthesis gas is cooled to a temperature level supplied from the reformer unit (40) to the condenser unit (50).

[0078] As shown in FIG. 2b, the heat exchanger (46) can alternatively first transfer the thermal energy released by the plasma reformer (42) into the crude synthesis gas to an intermediate circuit (47) filled with a heat transfer medium. Thermal oil is used as the heat transfer medium. There are two heat exchangers in the intermediate circuit (47). In the first heat exchanger, the thermal energy transferred from the heat exchanger (46) is absorbed and transferred to the intermediate circuit. In the second heat exchanger, the thermal energy of the intermediate circuit (47) is transferred to the oxidant stream. In this process, the oxidant stream evaporates, and the oxidant stream can also evaporate and superheat. In this embodiment, the intermediate circuit acts as an evaporator.

[0079] An oxidizing agent stream heated to increase thermal energy is supplied to a gasification reactor (30). Gasification in the gasification reactor (30) is promoted by increasing the thermal energy of the oxidizing agent stream and recirculating the oxidizing agent stream. This provides a portion of the thermal energy required in the gasification reactor (30).

[0080] Additionally, the hydrocarbon gas mixture is treated by quenching the crude synthesis gas in the cooling zone (48). The crude synthesis gas passes through the cooling zone (48) before being discharged from the reformer unit (40). Water is used for quenching. The crude synthesis gas is cooled to a temperature level at which it can be discharged from the reformer unit (40).

[0081] FIG. 3 shows a schematic diagram of the second stage of producing synthesis gas from waste. The crude synthesis gas discharged from the reformer unit is supplied to the condenser unit (50). In the condenser unit, the crude synthesis gas is condensed and cooled. Condensate is separated, and the condensate is separated from the crude synthesis gas at the bottom of the condenser unit (50). This produces acidic synthesis gas, which is supplied to the scrubbing tower.

[0082] In the scrubbing tower (60), contaminants such as halogen acids and other acidic gases transported along with the acidic synthesis gas are combined in a scrubbing process using a pure scrubbing solution. The pure scrubbing solution is supplied to the scrubbing tower (60). Here, potassium bicarbonate is used as the scrubbing solution. Additionally, Selexol scrubbing or Lectizol scrubbing may also be used as the scrubbing process, in which case polyethylene glycol or methanol may be used as the scrubbing solution. The contaminants originate from compounds of plastic waste. The contaminants are combined with the pure scrubbing solution and separated from the synthesis gas. This results in the production of a scrubbing solution contaminated with synthesis gas and contaminants. The synthesis gas is transferred to a storage tank (70), and the contaminated scrubbing solution containing contaminants is fed into a separate circuit. In this circuit, the scrubbing solution contaminated with contaminants is treated, the contaminants are separated from the scrubbing solution, and the pure scrubbing solution is returned to the scrubbing tower (60).

[0083] The product stream of the crude synthesis gas is stored in a storage tank (70). The storage tank is designed as a vessel, and any type of storage tank, such as a cavern storage tank or an absorptive storage tank, can be used. This compensates for fluctuations in synthesis gas production. The synthesis gas is transferred from the storage tank (70) to a compressor station (80).

[0084] A compressor station (80) compresses the synthesis gas to a higher pressure level so that it can be supplied to a pipeline, gas network, or additional process. The compressor station (80) achieves this by using compressors. One, two, three, four, or any number of compressors may be used. Additional processes include, for example, chemical synthesis, fuel production, hydrogen production, or power production.

[0085] After the compressor station (80), impurity gas is separated from the synthesis gas by condensation in the gas separator (90) and returned to the heat exchanger (46). The oxidant stream of carbon dioxide is understood as impurity gas, and other impurity gases can also be removed from the synthesis gas by the gas separator (90).

[0086] FIG. 4 shows a schematic diagram of a process for obtaining synthesis gas from waste. This represents a combination of sections of FIG. 2a and FIG. 3. The feedstock is stored in a waste storage container (10). Solid plastic waste is used as the feedstock. The feedstock is transported to a gasification reactor (30) through a supply system (20). The supply system (20) is designed as a screw conveyor. The gasification reactor (30) is a vortex gasifier. Additionally, an oxidizing agent stream is supplied to the gasification reactor (30). A mixture of water vapor and carbon dioxide is used as the oxidizing agent stream. The feedstock is gasified together with the oxidizing agent stream in the gasification reactor (30). In addition to the hydrocarbon gas mixture, ash in the form of bottom ash and fly ash is produced during this process. The bottom ash produced in the gasification reactor is deposited at the bottom of the reactor after the reaction. The bottom ash is separated from the gasification reactor (30) by an ash discharge system (32). Fly ash is discharged along with a stream of hydrocarbon gas mixture at one end of the gasification reactor (30). The stream of hydrocarbon gas mixture and fly ash then passes through an ash collector (34), in this case a cyclone, downstream of the gasification reactor (30). 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, purified from the fly ash, is supplied to a reformer unit (40) after the ash collector (34).

[0087] The reformer unit (40) includes a plasma reformer (42). A hydrocarbon gas mixture and an oxidant stream are supplied to the plasma reformer (42). The first and / or second oxidant of the supplied oxidant stream corresponds to the first and / or second oxidant of the gasification reactor (30), and the mixing ratio may differ from the mixing ratio of the oxidant stream of the gasification reactor (30). Here, water vapor and carbon dioxide are used as oxidants. In the reformer unit (40), a reforming reaction is carried out to produce crude synthesis gas in the plasma reformer (42) after the oxidant stream is added. The temperature of the crude synthesis gas is controlled in the heat retention chamber (44) of the reformer unit (40) after the plasma reformer (42). The temperature is controlled by maintaining 850°C for 2 seconds. The crude synthesis gas also undergoes a multi-stage cooling process. In one stage of the cooling process, the crude synthesis gas transfers some of its thermal energy to a heat exchanger (46). The heat exchanger (46) is a ceramic radiative heat exchanger. The heat exchanger (46) transfers a portion of the thermal energy of the crude synthesis gas to an oxidant stream, which is supplied separately or separated from the product stream of the synthesis gas by condensation by a gas separator (90) and returned. The oxidant stream is evaporated, and the oxidant stream can also be evaporated and superheated. In this embodiment, the heat exchanger (46) is an evaporator.

[0088] An oxidant stream with increased thermal energy is supplied to a gasification reactor (30). Gasification in the gasification reactor (30) is promoted by increasing the thermal energy of the oxidant stream and recirculating the oxidant stream. This provides some of the thermal energy required in the gasification reactor (30). Additionally, the synthesis gas produced from the hydrocarbon gas mixture is processed by quenching the crude synthesis gas in a cooling zone (48). The crude synthesis gas passes through the cooling zone (48) before being discharged from the reformer unit (40). Water is used for quenching. The crude synthesis gas is cooled to a temperature level supplied from the reformer unit (40) to the condenser unit (50).

[0089] In the condenser unit (50), the crude synthetic gas is condensed and cooled. During this process, condensate is separated, and the condensate is separated from the crude synthetic gas at the bottom of the condenser unit (50). This generates acidic synthetic gas, which is supplied to the scrubbing tower (60).

[0090] In the scrubbing tower (60), contaminants such as halogen acids and other acidic gases, which are transported along with the acidic synthesis gas, are combined in a scrubbing process using a pure scrubbing solution. The pure scrubbing solution is supplied to the scrubbing tower (60). Here, potassium bicarbonate is used as the scrubbing solution. The contaminants originate from compounds of plastic waste. The contaminants are combined with the pure scrubbing solution and separated from the synthesis gas. This results in the production of a scrubbing solution contaminated with synthesis gas and contaminants. The synthesis gas is transferred to a storage tank (70), and the contaminated scrubbing solution containing contaminants is fed into a separate circuit. In this circuit, the scrubbing solution contaminated with contaminants is treated, the contaminants are separated from the scrubbing solution, and the pure scrubbing solution is returned to the scrubbing tower (60).

[0091] The product stream of the crude synthesis gas is stored in a storage tank (70). The storage tank is designed as a vessel. This compensates for fluctuations in synthesis gas production. The synthesis gas is transferred from the storage tank (70) to a compressor station (80).

[0092] The compressor station (80) compresses the synthesis gas to a higher pressure level so that it can be supplied to a pipeline, gas network, or additional process. The compressor station (80) achieves this by using a compressor.

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

[0094] Where applicable, all individual features shown in the embodiments may be combined and / or exchanged with one another without departing from the scope of the invention. Explanation of the symbols

[0095] 1 device 10 waste storage containers 20 supply system 30 gasification reactors 32 discharge systems 34th collector 40 reformer units 42 Plasma reformer 44 heat retention chambers 46 heat exchangers 47 Intermediate Circuit 48 cooling zones 50 condenser units 60 scrubbing towers 70 storage tanks 80 Compressor Stations 90 gas separator S1 Input of feedstock S2 Gasification of feedstock Supply of S3 hydrocarbon gas mixture S4 Treatment of hydrocarbon gas mixtures S44 Cooling of raw synthesis gas S444 Temperature control of synthesis gas S4444 Rapid cooling of synthesis gas

Claims

Claim 1 A method for obtaining synthesis gas from at least one waste by combining a reforming reaction and a gasification reaction under thermal energy recirculation, comprising: a step (S1) of introducing a feedstock and a first and / or second oxidizing agent into a gasification reactor (30), wherein the feedstock comprises, in particular, at least one solid, liquid and / or gaseous waste; a step (S2) of gasifying the feedstock into a hydrocarbon gas mixture while supplying thermal energy using the first and / or second oxidizing agent within the gasification reactor (30), wherein at least one byproduct is generated, wherein the byproduct comprises, in particular, bottom ash and / or fly ash; a step (S3) of supplying the hydrocarbon gas mixture from the gasification reactor (30) to a reformer unit (40); and a step (S4) of treating the hydrocarbon gas mixture into a raw synthesis gas while supplying an additional first and / or second oxidizing agent within the reformer unit (40); wherein the thermal energy released in step S4 A method for obtaining synthesis gas, characterized by recirculating at least a portion to the gasification reactor (30) to provide at least a portion of the heat energy supplied in the S2 step. Claim 2 In claim 1, the step (S4) of processing the hydrocarbon gas mixture in the reformer unit (40) comprises, in addition to the step of reforming the hydrocarbon gas mixture into a crude synthesis gas in a plasma reformer (42), at least one of the following steps: a step of cooling the crude synthesis gas (S44); a step of controlling the temperature of the crude synthesis gas in a heat retention chamber (44) to increase the reaction yield (S444); and a step of rapidly cooling the crude synthesis gas in a cooling zone (48) (S4444). Claim 3 A method for obtaining synthesis gas according to claim 1 or 2, wherein a portion of the thermal energy released in step S4 is recirculated to the gasification reactor (30) through the first and / or second oxidizer. Claim 4 A method for obtaining synthetic gas, wherein the first and / or second oxidizer for recovering thermal energy is heated through a heat exchanger (46), particularly a radiative heat exchanger or a ceramic heat exchanger, located between the heat retention chamber (44) and the cooling zone (48). Claim 5 A method for obtaining a synthesis gas, wherein, in paragraph 3, the thermal energy is recirculated through a heat exchanger (46) located between the heat retention chamber (44) and the cooling zone (48), the heat exchanger (46) heats a medium in an intermediate circuit, and the medium then transfers heat to at least one heat absorber through at least one second heat exchanger (47), wherein the at least one heat absorber comprises a heat absorber having a flow of a first and / or second oxidizing agent. Claim 6 A method for obtaining synthesis gas according to paragraph 3, wherein at least one superheater is included between the heat exchanger (46) and the gasification reactor (30). Claim 7 A method for obtaining synthesis gas according to any one of claims 3 to 6, wherein at least a portion of the heated first and / or second oxidizing agent promotes the S2 step. Claim 8 A method for obtaining synthesis gas, wherein in any one of the preceding claims, the S2 step comprises separating bottom ash generated during gasification and at least partially separating fly ash generated during gasification and carried by the hydrocarbon gas mixture and returning it to the gasification reactor (30), wherein the separation preferably further comprises separating bottom ash through an ash discharge system (32), and the separation and return step preferably comprises separating fly ash present in the hydrocarbon gas mixture after gasification through an ash collector (34), particularly a cyclone. Claim 9 A method for obtaining a synthesis gas, wherein, in any one of the preceding claims, the ratio of hydrogen (H2) and carbon monoxide (CO) components in the synthesis gas is controlled through the mixing ratio of the first oxidizing agent and the second oxidizing agent. Claim 10 A method for obtaining synthesis gas, wherein in any one of the preceding claims, the method comprises the step of cooling the crude synthesis gas in a condenser unit (50) while separating the condensate after step S4. Claim 11 A method for obtaining synthesis gas, wherein, in any one of the preceding claims, the operating pressure of the gasification reactor (30) and the operating pressure of the plasma reformer (42) are an absolute pressure of 1 bar to 20 bar, preferably 1.5 bar to 4 bar. Claim 12 A method for obtaining a synthesis gas according to any one of claims 2 to 11, wherein the step of controlling the temperature of the crude synthesis gas in the heat retention chamber (44) comprises maintaining the temperature of the crude synthesis gas at least 850°C, preferably 1,200°C, for at least 2 seconds. Claim 13 A method for obtaining synthesis gas, wherein, in any one of the preceding claims, the first oxidizing agent comprises water vapor (H2O) and the second oxidizing agent comprises carbon dioxide (CO2). Claim 14 A method for obtaining synthesis gas, wherein in any one of the preceding claims, the gasification in step S2 is performed in a fluidized bed gasifier, a fixed bed gasifier, a screw gasifier, or an evaporator. Claim 15 A method for obtaining synthesis gas, wherein, in any one of the preceding claims, a material, in particular a metal carbonate, a metal oxide, a metal hydroxide, or a bicarbonate is added to the gasification of step S2 to combine the generated acidic gas. Claim 16 A method for obtaining a synthetic gas, wherein, in any one of claims 2 to 15, an arc discharge is additionally performed in the plasma reformer (42) during processing. Claim 17 A method for obtaining a synthesis gas according to any one of claims 3 to 16, wherein the method comprises separating an impurity gas present in the synthesis gas by condensation and returning it to the reformer unit (40), wherein the impurity gas preferably comprises carbon dioxide, and the carbon dioxide preferably forms a second oxidizing agent for recirculating the thermal energy generated in step S4. Claim 18 A method for obtaining synthesis gas according to claim 1, wherein the feedstock input in step S1 comprises at least one gaseous waste. Claim 19 An apparatus (1) for obtaining synthesis gas from at least one waste through a combination of a reforming reaction and a gasification reaction under thermal energy recirculation, comprising: (a) a storage facility for a feedstock and a first and / or second oxidizer, wherein the feedstock comprises, in particular, at least one solid, liquid and / or gaseous waste; (b) a gasification reactor (30) for gasifying the feedstock into a hydrocarbon gas mixture and at least one byproduct through the supply of a first and / or second oxidizer and thermal energy, wherein the byproduct comprises, in particular, bottom ash and / or fly ash; and (c) a reformer unit (40) for treating the hydrocarbon gas mixture into a raw synthesis gas while supplying the first and / or second oxidizer. and (d) a cooling device for cooling the synthetic gas, wherein at least a portion of the thermal energy released from the reformer unit (40) is recirculated to the gasification reactor (30) to provide at least a portion of the thermal energy supplied to the gasification reactor (30), a device for obtaining synthetic gas. Claim 20 In claim 19, the above device (1) is configured to perform a method according to any one of claims 1 to 18.

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