WO1999055803A1 - Procede fonde sur la production d'energie a partir de dechets, utilise pour produire du courant, de l'eau et/ou de l'hydrogene et/ou du methanol a partir de biomasse et/ou de dechets organiques - Google Patents

Procede fonde sur la production d'energie a partir de dechets, utilise pour produire du courant, de l'eau et/ou de l'hydrogene et/ou du methanol a partir de biomasse et/ou de dechets organiques Download PDF

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Publication number
WO1999055803A1
WO1999055803A1 PCT/AT1999/000102 AT9900102W WO9955803A1 WO 1999055803 A1 WO1999055803 A1 WO 1999055803A1 AT 9900102 W AT9900102 W AT 9900102W WO 9955803 A1 WO9955803 A1 WO 9955803A1
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WIPO (PCT)
Prior art keywords
module
gas
plant according
filter
hydrogen
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Application number
PCT/AT1999/000102
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German (de)
English (en)
Inventor
Bruno Berger
Gregor Rosinger
Original Assignee
Bruno Berger
Gregor Rosinger
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Filing date
Publication date
Application filed by Bruno Berger, Gregor Rosinger filed Critical Bruno Berger
Priority to AU35123/99A priority Critical patent/AU3512399A/en
Publication of WO1999055803A1 publication Critical patent/WO1999055803A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/463—Gasification of granular or pulverulent flues in suspension in stationary fluidised beds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/04—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content, e.g. water-gas shift [WGS]
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1003—Waste materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/12—Heating the gasifier
    • C10J2300/1261—Heating the gasifier by pulse burners
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • C10J2300/1646—Conversion of synthesis gas to energy integrated with a fuel cell
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1684—Integration of gasification processes with another plant or parts within the plant with electrolysis of water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1869—Heat exchange between at least two process streams with one stream being air, oxygen or ozone
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Definitions

  • Waste to Energy Process for the generation of electricity, water and / or hydrogen and / or methanol from biomass and / or organic waste
  • the invention relates to a plant and a method for recycling biomass and / or organic waste, according to the preamble of claim 1 and claim 21.
  • the invention has for its object to provide a plant for recycling biomass and / or organic waste, with which it is possible to reduce the volume of non-recyclable residues as much as possible.
  • the advantage here is that biomass and / or organic waste, which previously could only be processed with great technical effort, can be easily recycled, which also allows the volume of residual waste to be reduced to such an extent that it can be landfilled the landfills available to a limited extent can be better exploited.
  • this also makes it possible to protect the environment because it can reduce the number of landfills required or it is no longer necessary to create landfills to the extent that is currently customary.
  • it is advantageously possible to prefabricate the system or the various modules to a large extent, so that the assembly effort on site can be kept low, and it is also possible to simplify maintenance work or repair times shorten.
  • an embodiment according to claim 2 is also advantageous, according to which it is possible with simple means to separate the raw fuel gas produced in the gasification of the raw materials into high-purity hydrogen and a so-called lean gas, so that this lean gas can be used, for example, in thermal utilization in the system can and for which hydrogen no additional purification is required
  • An embodiment according to claim 3 is advantageous since the hydrogen contained in the raw fuel gas can easily diffuse through such metal alloys, and on the other hand the filter made of these metal alloys is largely insensitive to, for example, oxidative influences
  • an embodiment according to claim 5 is also advantageous, according to which the reformer module is designed as a fluidized bed reactor, since this enables thorough mixing of the raw materials with the oxidizing agent, and the efficiency of the system 1 can be increased
  • an embodiment according to claim 7 is also advantageous, according to which the heat removed with the raw fuel gas can be recovered from the reformer module and made available to the process again. This advantageously makes it possible to save on primary fuel gases, such as natural gas
  • a steam generator module for evaporation of the oxidizing agent according to claim 8 can advantageously lead to a saving of primary fuels, since it is thus possible to gasify the oxidizing agent already outside the reformer module, for example by the waste heat from the reformer module Increasing the efficiency of the system can be achieved, but it is also possible to keep the temperature fluctuations in the reformer module, which may arise from the introduction of a liquid oxidizing agent, to a minimum
  • an embodiment according to claim 9 is also advantageous, since dust particles entrained in the raw gas are simply separated from the reformer module and can thus be fed back to the gasification process in the event of incomplete implementation. In addition, this makes it possible to protect downstream system parts against possible incrustation or to operate them in a gentle manner.
  • an oxidation module By arranging an oxidation module according to claim 10 it can be achieved that the carbon monoxide formed due to the prevailing reaction conditions, in particular the carbon contained therein, can be further oxidized, and it is thus possible to increase the yield of hydrogen.
  • an energy generation module By arranging an energy generation module according to claim 11, it is also advantageously possible to generate electrical energy in an environmentally friendly manner, since especially when hydrogen is used as raw material for the energy generation module, predominantly chemically pure water is generated. However, this also makes it possible, on the one hand, to produce and make available the oxidizing agent for the process itself, and on the other hand to use any excess, for example as drinking water.
  • raw materials of different compositions can be used in an advantageous manner, and it is possible, for example, to integrate the plant into an overall concept for waste recycling, since this means that non-gasifiable raw material parts, such as metals, sorted out and possible recycling, e.g. a melting process can be supplied.
  • training according to claim 19 is also advantageous, since it makes it possible to compensate for seasonal fluctuations in the quantity of raw materials, and thus, for example, continuous operation of the energy generation module is possible.
  • the object of the invention is also achieved by a method according to claim 21.
  • the advantage of such a procedure is that by setting a partial pressure difference it is possible to control the output of the production of hydrogen and / or methanol and thus to compensate for any fluctuations in the operation of the system.
  • Fig. 1 is a schematic flow diagram of a plant according to the invention
  • FIG. 2 shows a simplified flow diagram of an embodiment variant of a system according to the invention
  • FIG. 1 shows the flow diagram of a system 1 according to the invention.
  • This system 1 is used primarily for the production of hydrogen, water and electrical energy, but of course other products such as carbon monoxide and hydrogen-containing gases such as synthesis gas, methanol, generator gas, water gas, hydrogen sulfide, sulfur, gypsum, heat or the like can be generated become.
  • Raw materials 2 are fed to a reformer module 3 in order to produce the desired products.
  • Mixed or unmixed biomass such as e.g. Various annual or multi-year plant varieties, but also waste of any kind, such as plastic waste, waste from organic material or the like, are used. As described in detail below, it may be necessary to subject the waste to separate processing beforehand. Of course, all raw materials can be mixed together.
  • so-called hazardous waste can also be processed with it. So it is e.g. possible to load the reformer module 3 with hospital waste, which would otherwise have to be disposed of in a landfill.
  • radioactive materials such as, for example, radioactive wood or the like, can be processed in the system 1 according to the invention in such a way that the volume of residual waste to be landfilled can be significantly reduced and thus landfill
  • the reformer module 3 is preferably designed as a fluidized bed reactor 4 and is intended to enable partial gasification and partial oxidation of the raw material 2.
  • the raw materials 2 can be introduced into the reformer module 3 via suitable conveying means known from the prior art, such as, for example, screw conveyors, belt conveyors or the like, and can be subjected to an oxidative treatment under pressure and at elevated temperature.
  • the temperature can be in the range between 500 ° C and 1000 ° C, preferably 600 ° C and 850 ° C.
  • Water vapor can be used as the oxidizing agent, so that essentially the carbon is partially oxidized to carbon monoxide and hydrogen can additionally be formed.
  • the content of carbon monoxide in the resulting raw fuel gas 5 is dependent on the selected pressure and temperature and in particular the ratio of carbon monoxide to carbon dioxide can be predetermined within certain limits, taking into account the Boudard equilibrium.
  • the reaction is chosen so that the fuel raw gas 5 contains a high proportion of carbon monoxide, since this can also be used for hydrogen production in a later process step.
  • fluidized bed reactor 4 instead of the fluidized bed reactor 4, it is possible to use other types of reactors known from the prior art, such as are known, for example, from Koppers-Totzk gasification or Lurgi pressure gasification. Fixed-bed reactors can of course also be used, or it is also possible to use a plurality of reformer modules 3 in combination, in particular in parallel.
  • the reformer module 3 is designed as a fluidized bed reactor 4, it is possible to use the steam required to establish the reaction as a fluidization medium.
  • the reformer module 3 is assigned at least one heat generating device 6, which can be designed as a so-called pulse burner or tube burner.
  • the heat generating device 6 can be designed as a so-called pulse burner or tube burner.
  • other types of burners such as surface burners, as the heat generating device 6, or it is possible to heat or preheat the raw materials 2 by means of electrical energy, for this purpose, for example, infrared burners, to which a particularly ceramic radiation element can be assigned , to use.
  • infrared burners to which a particularly ceramic radiation element can be assigned
  • the preferred design of the heat generating device 6 as a pulse burner or tube burner can solve the problems which arise due to the introduction of the required heat into the reformer module 3, in particular a steam reformer. If the reformer module is designed as a fluidized bed reactor 4, its size is limited by the laws of fluidization of the fluidized bed, and thus also the area that is possibly available for heat generation or transfer. In addition to the use of pulse burners or tube burners, there is of course
  • - 5 also the possibility of preheating the raw materials 2 accordingly or of designing the fluidized bed reactor 4 such that a plurality of communicating fluidized beds are available, a first fluidized bed being able to be used as a heating part and a second as an endothermic part (the reactions taking place in the reformer module 3 are essentially endothermic).
  • this can consist of a combustion chamber and a subsequent resonance tube, the combustion not taking place stationary, but rather a pulsation being established.
  • the frequency of the pulses is determined by the length of the resonance tube and can preferably correspond to just a quarter of the wavelength of the vibration to be formed.
  • the physical effect can be achieved with advantage that the heat transfer in the resonance tube can increase by a factor of 4 to 5 compared to a stationary heating at the same average temperature, and thus the required heating surface in the pulse burner can be reduced to a level that the integration of Heating surface in the fluidized bed of the reformer module 3 allows.
  • a pulse burner or tube burner can produce a sound emission, which advantageously has a comparative effect in the reformer and supports a cross-exchange of solids and gases in the fluidized bed. It is also possible to avoid slagging of the fluidized bed.
  • a heat generating device 6 may be assigned several pulse burners.
  • the expelled and partially oxidized raw fuel gas 5 is preferably drawn off in the upper region of the reformer module 3 and fed to a dedusting module 7.
  • This dedusting module 7 can, for example, as a mass separator, such as. B. as a cyclone, as a dust settling chamber, as a cloth filter, as an electrostatic precipitator or as a wet separator, such as. B. as a Venturi washer.
  • a mass separator such as. B. as a cyclone
  • a dust settling chamber such as a cloth filter
  • electrostatic precipitator such as. B. as a Venturi washer.
  • wet separator such as. B. as a Venturi washer.
  • the dedusting module 7 it is of course also possible for the dedusting module 7 to have its own dust discharge, and the dust components of the raw fuel gas which are separated off in this way can be fed to an aftertreatment.
  • This oxidation module 8 can be designed, for example, as a shift reactor 9 corresponding to the prior art, and is used primarily for the oxidation of the carbon monoxide carried in the raw fuel gas 5. An efficiency which can be in the range between 0.8 and 0.95 is preferably achieved. Water vapor can again be used as the oxidizing agent, so that hydrogen is formed in addition to carbon dioxide and the overall yield of hydrogen can thus be increased. Of course, it is also possible that other oxidizing agents are used to oxidize the carbon in the carbon monoxide.
  • the system is not primarily aimed at generating hydrogen or electrical energy, either to feed this raw fuel gas 5 directly to a combustion, or to refurbish it so that essentially synthesis gas as the end product for a number of possible chemical processes, such as eg the synthesis of methanol is available.
  • the raw fuel gas 5 When leaving the oxidation module 8, the raw fuel gas 5 preferably contains between 50% by volume and 70% by volume, in particular 60% by volume, of hydrogen.
  • This grass cleaning module 10 can comprise a filter 11, in particular a metal membrane filter, which preferably consists of an alloy of Pd-Cu, Pd-Ag or the like and forms palladium as the main alloy component.
  • this filter 11 should be designed in such a way that it is possible that only hydrogen can diffuse through this filter 11 and thus a separation or separation of the hydrogen from the raw fuel gas 5 is possible.
  • the filter 11 is designed as a metal membrane filter, it is also possible to supply the resulting lean gas, which still contains combustible constituents, such as methane, in particular to the reformer module 3, in particular the heat generating device 6, which saves primary fuel, in particular natural gas or can be replaced.
  • the filter 11 can be designed, for example, as a plate filter, tube filter or the like, it being possible in particular to combine a plurality of tubes into a tube bundle and thus to keep the dimensions of the gas cleaning module 10 small.
  • the filter 11, in particular the metal membrane filter, is preferably operated at an elevated temperature, since this allows the diffusion rate to be increased. Heating of the filter 11 can be achieved on the one hand by the raw fuel gas 5 itself, since it carries with it a thermal energy content originating from the reformer module 3, on the other hand it is of course possible to separately heat the gas cleaning module 10, in particular the filter 11, this heating can be electrical or with combustible gases or it is possible to use radiant heat for heating.
  • the resulting separated hydrogen can subsequently be fed to an energy generation module 12 or a storage module 13.
  • a partial stream of hydrogen is used for energy generation and the rest is either stored or fed to an end user.
  • suitable conveyors such. B. pipelines, chemical production plants, such as ammonia producers, the z. B. to work according to the Haber-Bosch process or to integrate a methano production or the like integrated in the WTE system.
  • the plant 1 according to the invention can also be part of petroleum refineries in order to have the necessary hydrogen for cracking the crude oil immediately and in sufficient quantity. Since the possible uses of hydrogen in the chemical industry are innumerable, the examples given should not be understood as limiting.
  • the power generation module 12 can preferably comprise at least one fuel cell for power generation
  • Fuel cells 14, hydrogen and oxygen, which can be used either in pure form or in the form of air, are recombined to form water.
  • the recombination takes place on catalytically active electrodes, thereby reversing the electrolysis of water
  • the energy in the form of direct current is preferably used.
  • Electrodes based on PEM technology polyme electrolyte membrane are preferably used.
  • the water formed in the reaction of the hydrogen with the oxygen is usually chemically pure and can be used as drinking water or the water formed can the process, in particular the reformer module 3 or the oxidation module 8, are supplied, whereby on the one hand the additional amount of water required can be reduced, and on the other hand the amount of auxiliaries, for example desalination chemicals for the supplied primary water, can be reduced and the environment can thus be protected
  • the electrodes of the fuel cell 14 should preferably be designed so that they have a pore structure, which allow the contact of the three phases, ie the fuel gas, the electrolyte and the electrode or the catalyst, for example due to the action of capillary forces, on the other hand, however, an overflow of the Electrolytes in one of the combustion spaces can be prevented
  • the hydrogen gives off the electrons to the anode under oxidation and the oxygen takes up these electrons at the cathode, so that in addition to the electrical current generated by the flowing electrons, water is also generated - direct current is generated assigned to the energy generation module 12, preferably an inverter 15, so that, for example, the resulting electricity can be fed into an energy supply network Based on the high calorific value of hydrogen, around 40-70% of the thermal energy of hydrogen can be converted into electrical energy.
  • the system 1 can also have at least one steam generator module 16 for generating and overheating the steam for the reformer module 3, a further gas cleaning module 10 for separating dust and acidic components of the flue gas, a water treatment module 17, a recooling module 18, various control and / or control devices 19 as well as various safety devices.
  • the water of reaction for the reformer module 3 which is preferably conducted in countercurrent, can be heated to such an extent that it can be introduced into the reformer module 3 as a vaporous oxidizing agent.
  • the air required for the combustion can be preheated, as a result of which valuable primary energy, in particular natural gas, can be saved, which is used by the heat generating device 6 to start up the plant 1 and / or to maintain the reaction in addition to the lean gas contained in the system 1 is generated and separated via the gas cleaning module 10, is supplied.
  • the ash which is discharged from the reformer module 3 via various suitable conveying devices is used discontinuously or continuously to heat the oxidation water.
  • a heat exchanger 20 can also be present in the area of the ash discharge.
  • Oxidation water can additionally be preheated via a heat exchanger 20, which is preferably arranged between the dedusting module 7 and the oxidation module 8.
  • a heat exchanger 20 can be arranged between the gas cleaning module and the energy generation module, if this is necessary. This can achieve 12, for example when this / 0 2 and H 2 with an advantage of protection of the power generation module - fuel cell is performed. With the heat dissipated in this heat exchanger 20, it is possible to preheat water which arises from the oxidation in an energy generation module 12 and in turn feed it to the reformer module 3 and / or the oxidation module 8.
  • a heat exchanger 20 is arranged in this raw fuel gas stream, as shown in dashed lines in Fig. 1. With the help of this heat exchanger 20, water, which is required for the operation of the system 1, can also be preheated.
  • Gas purification module 12 can also regulate the throughput and thus the utilization of the power generation module 12 in a simple manner, and it is thus possible to remove any overproduction.
  • the heat exchangers 20 are preferably designed so that they are made of materials which have a high heat transfer coefficient, e.g. Copper, aluminum, copper alloys or the like. Are corrosive media, such as. B. carried hydrogen sulfide, of course, various heat exchanger parts can be made of corrosion-resistant materials, or they can have corrosion-resistant coatings.
  • the heat exchangers 20 preferably operate according to the countercurrent principle, but all other possible flow profiles, such as, for example, crossflow, crossflow, direct current or the like, are also possible.
  • At least one medium preferably flows through the heat exchanger 20 with a turbulent flow, ie that the Reynold 's number, which is used to distinguish between laminar and turbulent flow can be used, greater than 2320, preferably greater than 10 4 .
  • a turbulent flow ie that the Reynold 's number, which is used to distinguish between laminar and turbulent flow can be used, greater than 2320, preferably greater than 10 4 .
  • the heat exchanger 20 which is arranged in the area of the ash discharge, as a recooling module 18, which enables the ash to be deposited directly.
  • the discharged ash can, of course, also be used for fertilizing purposes, particularly if 2 biomass from agricultural areas is used as raw material, and it is possible to feed the discharged ash to a bag filling device downstream of the heat exchanger 20 or the ash for bulk customers by means of, for example, trucks or to transport railway wagons.
  • conveying devices 22 such as pumps, compressors, blowers or the like, can of course be arranged at suitable points in order to maintain optimal operation of the system 1.
  • Such conveying devices 22 can be arranged, for example, in the primary air stream or in the various oxidant streams, as is indicated in FIG. 1.
  • conveyor devices 22 can be connected to the control and / or regulating device 19 via lines 23, so that, for example, a delivery volume of various process media that is dependent on the respective production quantity can be automatically regulated.
  • Flow meters or the like can be connected, with the help of which, or with the values detected by these sensors and sensors, the automatic regulation and control of the system 1 according to the invention is possible.
  • Such sensors and sensors can be arranged, for example, in the reforming module 3, in the oxidation module 8 or in the areas of the heat exchangers 20, or else in the area of the energy generation module 12. This makes it possible to control the temperature in the reformer module 3, which is necessary, for example, for the optimal reaction, in particular the ratio of carbon monoxide to carbon dioxide generated. On the other hand, it is possible in this way that the flow rate through the heat exchanger 20 is matched to the optimum operating temperature for the system 1 with the aid of temperature sensors.
  • the raw fuel gas 5 and the oxidizing agent as well as the combustion air or the fuel gas for the heat generating device 6 preferably pipes of any cross-section and diameter, which are in particular fluid-tight, are used.
  • pipes of any cross-section and diameter which are in particular fluid-tight
  • raw materials which consist of biomass can preferably be used for raw materials which consist of biomass, it is in particular also possible in the embodiment variant of FIG. 2 for these raw materials 2, as mentioned at the beginning, also secondary raw materials, such as, for. B. plastic waste or the like, or is it possible to also radioactively contaminated biomass or gasifiable biomass, which z. B. comes from so-called C weapons, to be recycled.
  • secondary raw materials such as, for. B. plastic waste or the like, or is it possible to also radioactively contaminated biomass or gasifiable biomass, which z. B. comes from so-called C weapons, to be recycled.
  • a sorting device 24 in front of the reformer module 3, for example. This can be used, for example, for sorting out metallic components from the raw material 2 and can be designed as a magnetic separator or the like.
  • the raw material 2 For non-magnetic components it may be necessary that the raw material 2 must be re-sorted manually. In order to avoid contamination of the staff with various pathogens,
  • a sterilization module 25 can be arranged before or after the sorting device 24.
  • This sterilization module can be formed in part from an electron accelerator, an irradiation device for ⁇ quanta or a device for gassing the raw material 2 with, for example, ethylene oxide.
  • the sterilization module 25 can comprise various conveying means such as conveyor belts, various continuous conveyors or the like to increase the degree of automation of the system 1.
  • the sterilization module 25 can in particular also be connected to the control and regulating device 19, so that automatic operation of the sterilization module 25 is possible, and on the other hand it is possible to monitor the treatment room of the sterilization module with, for example, a video camera, so that the operating personnel can access the Usually only necessary for maintenance work.
  • light guides can also be used as transmission media for electrical signals.
  • the sorting device 24 can further comprise various comminution devices, such as shredders, mills or the like, so that comminution of the raw material 2 to the desired particle size is possible.
  • Comminution devices of this type are advantageously used if the reformer module 3 is designed as a fluidized bed reactor 4, since a certain particle size of the raw material 2 is advantageous for maintaining the fluidized bed.
  • the sorting device 24 is also assigned various screening devices for sorting according to particle sizes and fractions.
  • the sorting device 24 can be appropriate funding for raw materials, such. B. include a belt conveyor, a chain conveyor or the like.
  • the individual parts of the sorting device 24 can of course also be arranged at a suitable other location within the system 1, if this is expedient.
  • the raw materials 2 pretreated in this way can be fed to the reformer module 3.
  • the raw materials 2 can have a different composition, it is possible that these raw materials 2 have sulfur components, e.g. organically bound sulfur.
  • the reformer module e.g. organically bound sulfur.
  • a raw fuel gas 5 is formed which, in addition to the desired proportions, in particular hydrogen and carbon monoxide, also contains undesirable constituents, such as hydrogen sulfide.
  • undesirable constituents such as hydrogen sulfide.
  • a desulfurization module 26 can be used to remove the hydrogen sulfide from the raw fuel gas 5 be arranged. This desulfurization module 26 can be arranged between the energy generation module 12 and the reformer module 3, in particular between the oxidation module 8 and a heat exchanger 20, which may be connected upstream thereof.
  • the desulfurization module 26 For desulfurization, it is possible, for example, for the desulfurization module 26 to work according to the Claus method, after which the hydrogen sulfide is incompletely burned in a combustion chamber with the supply of air, and sulfur dioxide and water vapor are formed in the process.
  • the resulting combustion temperature is approximately 1400 ° C., this heat can be used in a possibly downstream waste heat boiler to generate steam, which can be supplied to the reformer module 3.
  • the desulfurization module 26 is arranged directly after the reformer module 3, in order to keep the conveyance paths for the raw fuel gas 5 between the desulfurization module 26 and the reformer module 3 as short as possible, in order to cool down the raw fuel gas 5 to avoid.
  • the water produced in this process can of course be fed to the reformer module 3 or the oxidation module 8.
  • the sulfur dioxide formed can subsequently be fed to a contact container assigned to the desulfurization module 26 by reducing it to pure sulfur by hydrogen sulfide, the temperature of the reaction gases increasing again, and this temperature increase being able to be partially recovered via a heat exchanger 20 which may be arranged.
  • the resulting sulfur can be discharged from the desulfurization module 26 and used, for example, to generate sulfuric acid.
  • the desulfurization module 26 As, for example, adsorption columns, these adsorption columns, for example, with activated carbon, molecular sieves or the like can be filled. However, it should be ensured that no adsorbents are used as filler material for such adsorption columns, which reduce the content of hydrogen or carbon monoxide in the raw fuel gas 5.
  • lime is used to remove S or H 2 S from the raw fuel gas 5, e.g. B. as a solution in
  • the flue gases before they leave the system 1 via the chimney 21 for example with the Ferrox process, which uses a suspension of iron (III) hydroxide in dilute soda solution, or after the Thylox Processes in which a sodium thioarsenate solution is used as the oxidation cleaner, which can be regenerated by oxidation with air, are desulfurized.
  • raw materials 2 of different compositions can be used in the embodiment variant of system 1 according to FIG. 2, it may be necessary to feed the flue gases, which leave system 1 via chimney 21, to separate cleaning in order to impair the environment to keep it as low as possible.
  • a cleaning module 27 is arranged between the second steam generator module 16 and the chimney 21 according to FIG. 1, which cleaning module may consist, for example, of two absorption columns.
  • One absorption column can be used as a washing tower for acidic constituents and the second absorption column can be used as a washing tower for basic constituents in the flue gas, so that such constituents can be removed from the flue gas.
  • Such washers can be operated batchwise or continuously, and it is possible to use the absorbent in liquid or solid form.
  • Wash towers can also be used, in which the absorbent is distributed over several floors, through which the flue gases are passed.
  • One possible training is, for example, a bubble tray column.
  • so-called spray towers can of course also be used.
  • washing towers of the cleaning module 27 are operated at elevated pressure, so that the acidic and / or basic constituents contained in the flue gas are chemically and / or physically bound, it is possible that the absorbent can be regenerated with a subsequent relaxation.
  • system 1 can include additional storage modules 13 for water, electrical energy, primary fuels, secondary fuels and raw materials 2.
  • the raw materials 2 are after any necessary pretreatment, such as. B. one
  • Raw material components the reformer module 3 fed.
  • the raw materials 2 it is possible for the raw materials 2 to be supplied preheated from the reformer module 3.
  • the raw materials 2 can then be brought to the required reaction temperature in the reformer module 3 with a heat generating device 6, and a pressure required for carrying out the reaction can be set in the reformer module 3.
  • Natural gas, lean gas from the recycling process, mixtures thereof or the like can be fed into the heat generating device 6.
  • Water vapor can be fed into the reformer module 3 as an oxidizing agent at one or more points, this water vapor preferably being generated with heat derived from the recycling process. For this purpose, it is possible to heat the oxidation water with the aid of a number of heat exchangers 20 or steam generation modules 16.
  • the raw fuel gas 5 escaping from the reformer module which contains partially oxidized carbon and hydrogen as main components, and possibly methane, CO 2 , or the like as secondary components, is fed to a dedusting module 7 for the separation of possibly carried dust particles.
  • the solid particles separated off for example with a cyclone, can be fed to the reformer module 3 again.
  • the raw fuel gas 5 leaving the dedusting module 7 is preferably passed through a heat exchanger 20 in countercurrent, with this heat exchanger 20 in turn being able to preheat water of oxidation.
  • the raw fuel gas 5 can subsequently be fed to an oxidation module 8, for example a shift reactor 9, in which the carbon monoxide is oxidized to carbon dioxide with the aid of water as the oxidizing agent, and in turn hydrogen is formed in the process.
  • the efficiency of this reaction is preferably in the range between 0.8 to 0.95.
  • the raw fuel gas 5 removed from the oxidation module 8 is fed to a gas cleaning module 10.
  • the hydrogen is preferably separated off with the aid of a metal membrane filter which is only permeable to hydrogen atoms.
  • the rate of dissociation through this metal membrane filter which can be tubular, for example, and in particular also
  • tubes can be assembled to form a filter unit, or which can also have any other configuration, such as plate-shaped, depends on the partial pressure difference of hydrogen before and after the filter 11, and can thus be controlled or regulated via this partial pressure difference become.
  • the lean gas generated during this gas cleaning which still contains combustible components such as methane, residual amounts of carbon monoxide or the like, is preferably fed to the heat generating device 6 for recycling.
  • the hydrogen gas removed from the gas cleaning module 10 can subsequently be cooled via a heat exchanger 20, which in turn can be used to heat oxidation water, to the extent that either storage in various storage products 13 and / or its use in the energy generation module 12 becomes possible.
  • the hydrogen is oxidized to water.
  • Oxygen serves as the oxidizing agent, which can either be used as pure oxygen or as air.
  • a so-called PEM electrolyte polymer electrolyte membrane
  • the gases flowing along the electrodes are oxidized (hydrogen) or reduced (oxygen) and an electrical current flow is possible due to the electron transfer taking place, so that the energy generated or converted - chemical energy is converted into electrical energy - to an end user or a corresponding storage medium, such as an accumulator.
  • the direct current generated in the fuel cell can be converted into alternating current using an inverter 15.
  • the hydrogen produced is not, or not wholly, emitted, but is, for example, either fed directly to an end user, such as the chemical industry, for example via pipeline, or that this hydrogen is stored in corresponding storage modules 13 for the further consumption can be stored temporarily.
  • These memory modules 13 can of course also be used as buffers for seasonal capacity fluctuations in the system 1.
  • the raw materials 2 can be subjected to sterilization in suitable packaging, such as cardboard boxes, containers or the like. This makes handling in the task area easier. It also proves to be an advantage if the packaging consists of a gasifiable material, so that unpacking is not necessary and the raw materials 2 with their packaging can be fed to the reformer module 3 after any size reduction.
  • Recyclable containers for example made of metal, can also be used as collection containers, in particular for household waste, which enables the establishment of a regional collection network. Under certain circumstances, these collection containers can be subjected to sterilization, which can reduce the risk of possible transmission of germs.
  • the resulting waste heat can of course also be used for preheating the various raw materials.
  • the electrical current required for the operation of the linear accelerator is preferably branched off from the plant 1's own production.
  • the packaging can also be provided with moisture-blocking layers, e.g. PE films must be lined.
  • the raw materials 2 are pelletized in a pelletizing system before they are used in the reformer module 3, whereby the storage or the raw material handling can be facilitated.
  • the system 1 according to the invention can of course also be used to connect petrol stations for vehicles operated with fuel cells.
  • FIGS. 1; 2 shown versions of the

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  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)

Abstract

L'invention concerne une installation pour valoriser de la biomasse et/ou des déchets organiques, qui se caractérise en ce qu'elle comporte un module de reformage auquel est raccordé au moins un dispositif de production de chaleur pour chauffer une matière première et/ou un agent d'oxydation, au moins un dispositif pour acheminer le combustible primaire et/ou le combustible secondaire, ainsi qu'au moins, dans chaque cas, un dispositif pour acheminer la matière première au moins apte à la gazéification partielle et un agent d'oxydation, par ex. de la vapeur d'eau, ou similaire et au moins un dispositif pour enlever un gaz brut combustible et/ou des gaz brûlés et/ou un solide, par ex. des cendres ou similaires, ainsi qu'au moins un module de purification des gaz (10) qui comprend un filtre (11), notamment une membrane métallique.
PCT/AT1999/000102 1998-04-28 1999-04-26 Procede fonde sur la production d'energie a partir de dechets, utilise pour produire du courant, de l'eau et/ou de l'hydrogene et/ou du methanol a partir de biomasse et/ou de dechets organiques WO1999055803A1 (fr)

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AU35123/99A AU3512399A (en) 1998-04-28 1999-04-26 Waste to energy method for producing electricity, water and/or hydrogen and/or methanol from biomass and/or organic waste

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HUP9815295 1998-04-28
HU15295/98 1998-04-28
HU15297/98 1998-04-28
HUP9815297 1998-04-28

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1120844A2 (fr) * 2000-01-24 2001-08-01 Toyota Jidosha Kabushiki Kaisha Système pour production du gaz combustible pour piles à combustible
EP1136542A1 (fr) * 1998-11-05 2001-09-26 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
DE10016847A1 (de) * 2000-04-05 2001-10-18 Zae Bayern Bayerisches Zentrum Fuer Angewandte Energieforschung Ev Vorrichtung zur energetischen Nutzung von kohlenstoffhaltigen Einsatzstoffen
US6572837B1 (en) 2000-07-19 2003-06-03 Ballard Power Systems Inc. Fuel processing system
DE102004006516A1 (de) * 2004-02-10 2005-08-25 Voith Paper Patent Gmbh Verfahren zur Erzeugung von Prozesswärme und/oder elektrischer Energie
EP1601614A2 (fr) * 2002-09-10 2005-12-07 Manufacturing And Technology Conversion International, Inc. Processus et appareil de reformage a la vapeur
DE102009038323A1 (de) * 2009-08-21 2011-02-24 Krones Ag Verfahren und Vorrichtung zur Verwertung von Biomasse
DE102013101368A1 (de) * 2013-02-12 2014-08-14 Thyssenkrupp Uhde Gmbh Wirbelschichtvergaser
WO2015154874A1 (fr) * 2014-04-09 2015-10-15 Michael Niederbacher Procédé et installation d'épuration de friches environnementales contaminées, en particulier de réduction de la charge de rayonnement de friches environnementales contaminées par des substances radioactives

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0081669A1 (fr) * 1981-12-11 1983-06-22 Forschungszentrum Jülich Gmbh Membrane de diffusion pour hydrogène et procédé de diffusion pour séparer de l'hydrogène des mélanges de gaz
FR2580660A1 (fr) * 1985-04-19 1986-10-24 Gau Georges Reacteur multitubulaire pour la gazeification des combustibles solides carbones
EP0292987A1 (fr) * 1987-05-28 1988-11-30 TOGNAZZO, Valerio Procédé et installation pour la transformation de matières de déchets polluants combustibles en énergie propre et produits utilisables
EP0512305A1 (fr) * 1991-05-08 1992-11-11 DANECO DANIELI ECOLOGIA SpA Procédé pour la conversion de combustible dérivé de déchets en un gaz combustible
EP0609802A1 (fr) * 1993-02-02 1994-08-10 JUCH, Helmut Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0081669A1 (fr) * 1981-12-11 1983-06-22 Forschungszentrum Jülich Gmbh Membrane de diffusion pour hydrogène et procédé de diffusion pour séparer de l'hydrogène des mélanges de gaz
FR2580660A1 (fr) * 1985-04-19 1986-10-24 Gau Georges Reacteur multitubulaire pour la gazeification des combustibles solides carbones
EP0292987A1 (fr) * 1987-05-28 1988-11-30 TOGNAZZO, Valerio Procédé et installation pour la transformation de matières de déchets polluants combustibles en énergie propre et produits utilisables
EP0512305A1 (fr) * 1991-05-08 1992-11-11 DANECO DANIELI ECOLOGIA SpA Procédé pour la conversion de combustible dérivé de déchets en un gaz combustible
EP0609802A1 (fr) * 1993-02-02 1994-08-10 JUCH, Helmut Dévolatilisation et/ou gazéification en continu de carburants ou de déchets solides

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1136542A4 (fr) * 1998-11-05 2004-11-24 Ebara Corp Systeme de production d'energie par gazeification d'un materiau combustible
EP1136542A1 (fr) * 1998-11-05 2001-09-26 Ebara Corporation Systeme de production d'energie par gazeification d'un materiau combustible
EP1120844A3 (fr) * 2000-01-24 2008-11-19 Toyota Jidosha Kabushiki Kaisha Système pour production du gaz combustible pour piles à combustible
EP1120844A2 (fr) * 2000-01-24 2001-08-01 Toyota Jidosha Kabushiki Kaisha Système pour production du gaz combustible pour piles à combustible
DE10016847C2 (de) * 2000-04-05 2002-11-14 Zae Bayern Bayerisches Zentrum Fuer Angewandte Energieforschung Ev Vorrichtung zur energetischen Nutzung von kohlenstoffhaltigen Einsatzstoffen
DE10016847A1 (de) * 2000-04-05 2001-10-18 Zae Bayern Bayerisches Zentrum Fuer Angewandte Energieforschung Ev Vorrichtung zur energetischen Nutzung von kohlenstoffhaltigen Einsatzstoffen
US6572837B1 (en) 2000-07-19 2003-06-03 Ballard Power Systems Inc. Fuel processing system
EP1601614A2 (fr) * 2002-09-10 2005-12-07 Manufacturing And Technology Conversion International, Inc. Processus et appareil de reformage a la vapeur
EP1601614A4 (fr) * 2002-09-10 2008-02-13 Mfg & Tech Conversion Int Inc Processus et appareil de reformage a la vapeur
DE102004006516A1 (de) * 2004-02-10 2005-08-25 Voith Paper Patent Gmbh Verfahren zur Erzeugung von Prozesswärme und/oder elektrischer Energie
DE102009038323A1 (de) * 2009-08-21 2011-02-24 Krones Ag Verfahren und Vorrichtung zur Verwertung von Biomasse
DE102013101368A1 (de) * 2013-02-12 2014-08-14 Thyssenkrupp Uhde Gmbh Wirbelschichtvergaser
DE102013101368B4 (de) 2013-02-12 2023-04-27 Gidara Energy B.V. Wirbelschichtvergaser
WO2015154874A1 (fr) * 2014-04-09 2015-10-15 Michael Niederbacher Procédé et installation d'épuration de friches environnementales contaminées, en particulier de réduction de la charge de rayonnement de friches environnementales contaminées par des substances radioactives

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