[go: up one dir, main page]

WO2024218048A2 - Dispositif et procédé de destruction par plasma à haute température de déchets - Google Patents

Dispositif et procédé de destruction par plasma à haute température de déchets Download PDF

Info

Publication number
WO2024218048A2
WO2024218048A2 PCT/EP2024/060206 EP2024060206W WO2024218048A2 WO 2024218048 A2 WO2024218048 A2 WO 2024218048A2 EP 2024060206 W EP2024060206 W EP 2024060206W WO 2024218048 A2 WO2024218048 A2 WO 2024218048A2
Authority
WO
WIPO (PCT)
Prior art keywords
reactor
waste
hydrogen
gas
temperature
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/EP2024/060206
Other languages
English (en)
Other versions
WO2024218048A3 (fr
Inventor
Georg ROYSSBACH
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Quantum Energy d o o
Original Assignee
Quantum Energy d o o
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Quantum Energy d o o filed Critical Quantum Energy d o o
Publication of WO2024218048A2 publication Critical patent/WO2024218048A2/fr
Publication of WO2024218048A3 publication Critical patent/WO2024218048A3/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
    • F23G5/085—High-temperature heating means, e.g. plasma, for partly melting the waste
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed

Definitions

  • the present invention belongs to the field of combustion devices and combustion processes for removal of waste.
  • the invention relates to a device and a method for high-temperature plasma destruction of solid and/or liquid waste.
  • Waste disposal includes the processes and actions required to manage waste from its inception to its final disposal. Waste can be solid, liquid, or gases and each type has different methods of disposal and management. Waste management may have various origins, such as industrial, biological, household, municipal, organic, biomedical, radioactive wastes. Waste can pose a threat to human health, hence safe and efficient treatment and disposal is required.
  • the most promising trend in the development of technology for cleaning up toxic industrial and energy gas emissions, water treatment and disposal of industrial wastewater is the use of high-energy external fields like cold and high-temperature plasma, ultrasonic wave coherence, multiphase coherence, acoustic-plasma discharge with the formation of a high-energy hydroxyl radical group.
  • the energy of the electric field affects the physicochemical characteristics of the processed liquid and gaseous medium and its ionic composition, the structure of dissolved organic substances and the viability of the microorganisms present without any additional introduction of chemical reagents.
  • the technical problem addressed by the present invention is design of a reactor and a method for efficient destruction of various waste materials without the use of atmospheric air and without producing dioxins, furans and other toxic substances.
  • Utility model CN217973078U discloses a composite gasification device based on a filtering combustion mode, and belongs to the technical field of synthesis gas production through solid fuel gasification.
  • the problems of low carbon conversion efficiency, high tar content and low synthesis gas yield are solved.
  • the device comprises a gasifying agent inlet, a preheating section, a reaction section, a reforming section, a synthesis gas outlet and a discharge section, the gasifying agent inlet is communicated with the preheating section, two ends of the reaction section are respectively communicated with the preheating section and the reforming section, the synthesis gas outlet is communicated with the reforming section, the discharge section is communicated with the reaction section, and the reforming section is communicated with the reaction section.
  • the preheating section and the reforming section are both composed of inert porous medium fillers in various forms, the interior of a porous medium accumulation bed layer is provided with complex pore channels, mass transfer and heat transfer are facilitated, and a porous medium can be composed of inert particles such as ceramsite or glass beads and similar substances, metal wire meshes, foamed ceramics and the like; the device is mainly used for high-efficiency gasification of various solid fuels.
  • This solution uses filtration combustion and the adiabatic effect for gasification of solid products, such as coal or other burning fuel.
  • this disclosure is not discussing superheated steam to be split into oxygen, hydrogen and hydroxyl radicals.
  • Patent application WO2018164651 A1 relates to a method for gasification of solid fuel in a gasifier comprising a casing defining a cavity and having a fuel compartment, a reverse gasification zone and a direct gasification zone disposed therein, the method comprising the steps of:
  • the invention aims to provide a device and a method for destructing any type of waste including any possible emission gases, which address the shortcomings as well as complexity of the presently known solutions.
  • the goal of the present invention is to design the device and the method so there is no need for further processing of flue gases emitted during waste processing, as the device itself ensures all potentially toxic gases are destructed too.
  • the technical problem is solved as defined in the independent claims, wherein preferred embodiments of the invention are defined in the dependent claims.
  • This invention is based on the method of superadiabatic filtration combustion, in which there are several active layers of influence on the feedstock, the reaction fluidized bed, the boundary layer and the gasification layer of the fuel feedstock.
  • Filtration combustion is understood as the propagation of exothermic transformation waves in the porous medium of an ionized fluidized bed, when all combustion products, flue gases (synthesis) and condensate are filtered through the fluidized bed until complete oxidation (destruction of matter).
  • the technology makes it possible to destroy the products of gasification of any solid and gaseous fuel. Heating expanding gases moving up the toroid from the boundary layer from the area of heating and gasification, flue gases practically cannot leave the reactor without passing through a high-temperature ionized fluidized bed, which is plentifully purged with oxidizers and radicals of the hydroxyl group obtained from water vapor.
  • the mechanism of propagation of the thermal reaction zone in this system includes layer-by-layer heating of the initial substances (solid fuel) ahead of the combustion front, down from the boundary layer forming a combustion zone (fluidized bed), and up from the boundary layer a gasification zone.
  • a specific element that determines the combustion feature of this system is the filtration of all flue gases (synthesis gas) through a fluidized bed, which acts not only as a participant in a chemical reaction, but also as a coolant that forms the thermal structure of the combustion wave.
  • the device for high-temperature plasma destruction of solid and liquid waste comprises a reactor (incinerator) with an inlet for leading waste material into the intertior of the reactor and an outlet for leading created gas and/or heat towards a device for recovery of the resulting heat into simultaneous production electricity and/or green hydrogen in compliance with environmental requirements for emissions of pollutants into the atmosphere.
  • Said reactor has a reactor shell, lined with a convection tubes for toroidal gas convection, heat exchanger for cooling the reactor bottom, ceramic protection layer and the high temperature shield and thermal insulation provided on the top of the shell provided with the inlet.
  • the reactor On the opposite end from the inlet the reactor is provided with a grate and an ash drip tray.
  • three zones are provided, namely a gasification zone, a high-temperature fluidized bed and a boundary zone inbetween the gasification zone and the fluidized bed.
  • the fluidized bed zone with high temperatures in the range from 1500 and higher, also higher than 2000 °C, is exposed to an outlet of a device for generation of high-temperature reactive gas flow from water vapour (i.e.
  • emission gases are flowing in one direction, which is downwards, so they have to pass through the fluidized bed. Furthermore, the gas streams due to the grate may be recirculated inside the reactor until the complete destruction of any harmful gases.
  • the final processed gases are then led from the reactor towards a user, which may be a steam generator, a hydrogen producing device, etc. Due to leading away the gases, there is no pressure in the combustion chamber in the reactor. Rather, there is a negative pressure, i.e. a vacuum.
  • the device for generation of high-temperature reactive gas flow from water vapour may be any device that ensures that the water as fuel is transformed into the resulting gas flow, which comprises hydrogen, oxygen and hydroxyl radicals, which may be further separated based on needs of users, systems and subsequent processing.
  • All produced heat may be used for the production of water steam, which can be further split into hydrogen and oxygen, thus producing green hydrogen as a commercial product, while the oxygen may be used for optional ozonation of incoming waste material or for operation of the reactor.
  • hot gases from the reactor enter the vortex cyclone through the pipeline.
  • cyclone ash and slag fractions are separated from the exhaust gases, while the heat may be further used with subsequent recovery of the resulting heat into simultaneous production electricity and green hydrogen in compliance with environmental requirements for emissions of pollutants into the atmosphere and bottom ash in accordance with the EPA standard.
  • the gas flow enters a steam boiler, the hot gas recovery boiler generates steam to rotate the turbine, with subsequent recovery and condensation of the exhaust steam through the condenserrecuperator back into the water supply system to the steam boiler.
  • the superheated steam from the steam boiler enters the steam turbine, the turbine rotates the generator, which in turn generates electricity (power transformer).
  • the system allows for the disposal of 30 tons of garbage per day to generate up to 2 MW of electricity.
  • the method for high-temperature plasma destruction of solid and liquid waste comprises at least the following steps: a) Waste in any form is created, preferably hazardous industrial emission or various waste, b) Waste is led to a hopper, where it is combined and shredded c) Optionally waste is treated with ozone d) Waste is led to a reactor, where it is exposed to high-temperatures and highly reactive gases comprising oxygen, hydrogen and hydroxyl radicals, where all waste and flue gases are oxidized and destroyed, e) Optionally heat is recuperated as electricity and/or hydrogen is produced by using the generated heat to produce superheated water steam from which hydrogen can be purified using suitable filters and membranes.
  • the lower part of the grate is active, rotates and is used to remove the lower fluidized bed
  • the reaction zone consists of three layers, the fluidized bed zone, the boundary layer, and the gasification zone.
  • the fluidized bed zone is actively purged with a hydrogen-oxygen mixture, which is produced only from water by splitting water vapor into hydrogen oxygen and OH hydroxyl radicals.
  • the nozzles for forcing the hydrogen-oxygen mixture are located along the entire circumference of the fluidized bed and create a vortex turbulent flow in the area of the fluidized bed.
  • the design of the reactor does not allow flue gases and combustion products to leave the reactor without participating in the processes of thermochemical degradation reactions.
  • the nozzles for introducing superheated steam into the reactor are, by their design, a plasma torch, thereby forming a plasma jet up to 5.000 °C with a sharp thermal wave gradient up to 1 m.
  • a reflector screen made of resistant materials, such as high-temperature tungsten carbide alloys.
  • the upper grate and the active lower grate are made of resistant materials, such as high-temperature alloys of tungsten carbide and titanium oxide.
  • the ash collection area under the grate is protected by a protective screen with a high-temperature ceramic plate lining.
  • the zone of fuel supply to the reactor consists of a sealed sluice, consisting of a hydraulic seal blocking the access of gas from the reactor to the zone of fuel supply.
  • the two-chamber vortex cyclone provides separation of solid slags and bottom ash from emission gases.
  • a specially designed plasma-chemical reactor operating on the principle of resonance of electromagnetic fields and high-voltage corona discharge, produces a high-energy highly reactive hydrogen-oxygen mixture from superheated steam, which creates plasma-chemical processes in the zone of thermochemical reactions and afterburning of exhaust gases.
  • the main principle of the process of high-temperature plasma-chemical destruction of matter is the principle of superadiabatic filtration combustion, resulting in complete combustion of flue gases with subsequent recovery of the resulting heat into simultaneous production electricity and green hydrogen in compliance with environmental requirements for emissions of pollutants into the atmosphere and bottom ash in accordance with the EPA standard.
  • the invention ensures the destruction and removal of 99.99% of all major hazardous components, and for the most hazardous organic components of toxic waste, such as PCDD, PCDF and PCBs, destruction and destruction by 99.9999%.
  • the present invention is suitable for disposal or destruction of solid and liquid municipal waste, sludge from industrial, petrochemical, coal, organic agricultural wastes with a high content of non-combustible components, biological sewage treatment plants, meat processing waste and other solid waste, as well as any vapor-gaseous, liquid hazardous waste, including low-calorie waste in terms of the content of combustible components.
  • the invention ensures utilization of various above-mentioned wastes without an expressed need for grinding them, without limiting them in terms of moisture, without using additional fuel, without environmental restrictions on the use of ash residue.
  • FIG 1 The device for high-temperature plasma destruction of solid and liquid waste with shown zones of treatment
  • FIG. 2 The device for high-temperature plasma destruction of solid and liquid waste
  • FIG. 3 Scheme of a combustion wave with superadiabatic heating.
  • the flow of solid material from top to bottom, the gas flow is fed from the side of the reactor into the fluidized bed.
  • the high-temperature combustion zone is shown with a lighter background colour
  • Figure 4a The device for generation of high-temperature reactive gas flow from water vapour (plasma reactor) according to a first embodiment
  • FIG 4b The device for generation of high-temperature reactive gas flow from water vapour (plasma reactor) according to a second embodiment
  • Figure 5 Schematic diagram of a plasma chemical plant with subsequent generation of electricity and hydrogen
  • the device for high-temperature plasma destruction of solid and liquid waste comprises a reactor with an inlet for leading waste material into the intertior of the reactor and an outlet for leading created gas and/or heat towards a device for recovery of the resulting heat into simultaneous production electricity and/or green hydrogen in compliance with environmental requirements for emissions of pollutants into the atmosphere.
  • the inlet comprises a hopper 1 in its bottom provided with a grinder or a shredder 2 for grinding waste material.
  • a shutter is provided between the hopper 1 and the reactor, wherein the shutter comprises a shutter frame 3, a hydraulic cylinder 4 and a feed hopper shutter 5.
  • a guide cone 6 for leading waste into the reactor is provided below this a guide cone 6 for leading waste into the reactor, wherein the guide cone area is thermally insulated to prevent losing heat in the reactor.
  • the loading to the reactor may have more than one hydraulic pistons, wherein one is driven by a hydraulic drive, while the second counter hydraulic piston actuates a loading hatch, which blocks access to the lock of gas flows from the reactor, ensuring tightness.
  • the raw material loading guide cone 6 has thermal insulation 9, thereby preventing the propagation of a thermal wave in the upper part of the reactor cover, which also serves as thermal reflectors and a swirler for the upper internal gas flows.
  • the shredder 2 may be combined with a pre-ozonation device, which contributes to the partial displacement of atmospheric air from the supply zone to the reactor, and pre-treatment with ozone of the feedstock fed to the reactor.
  • a pre-ozonation device which contributes to the partial displacement of atmospheric air from the supply zone to the reactor, and pre-treatment with ozone of the feedstock fed to the reactor.
  • an additional device for ozone treatment is used, which receives ozone from atmospheric air, or from oxygen obtained by filtering (separating) superheated steam.
  • Ozone is known for its high oxidizing properties; at the preliminary stage of ozonation, it penetrates into the depth of the crushed raw materials. Ozone is a heavier gas, displacing atmospheric air upwards, filling with it the piston feed zone into the reactor
  • Said reactor has a reactor shell 7, lined with a convection tubes 8 for toroidal gas convection, a heat exchanger 10 for cooling the reactor bottom, ceramic protection layer 12 and the high temperature shield 11 made from high-temperature alloy (tungsten carbide, titanium oxide) and thermal insulation 9 provided on the top of the shell where the guide cone 6 is installed.
  • a grate comprising an upper static part 14 and a rotatable lower part 13, which facilitates discharge of the lower fluidized bed 7, wherein the lower grate 13 is movable due to a shaft 17 of the grate, a motor 16, preferably a reduction ger motor for lower grate shaft rotation, and upper and lower bearings 18, 19 for supporting the shaft of the grate.
  • the bottom of the reactor is provide an ash drip tray 15.
  • the lower part 13 of the grate is movable, it rotates around its axis, dropping the spent as part of the fluidized bed into the ash tray 15, thereby ensuring the movement of all processed fuel (garbage) down the process, this makes it possible to systematically regulate the processes occurring in the boiling zone 22.
  • three zones are provided, namely a gasification zone, a high-temperature fluidized bed 22 and a boundary zone inbetween the gasification zone and the fluidized bed.
  • the fluidized bed zone with high temperatures in the range from 1500 and higher, also higher than 2000 °C, is exposed to an outlet of a device for generation of high-temperature reactive gas flow from water vapour (i.e.
  • Figure 3 shows a scheme of a combustion wave with superadiabatic heating.
  • the flow of solid material from top to bottom, the gas flow is fed from the side of the reactor into the fluidized bed.
  • the high-temperature combustion zone is shown with a lighter background colour. Due to the fact that almost any fuel initially contains chemically inert impurities (for example, ash as a product of combustion), the porous medium before the reaction zone is generally a mixture of condensed fuel with an inert material. Behind the combustion front, a porous residue containing ballast and condensed combustion products remains.
  • the heat released in the reaction is transferred to the unreacted layers of the reactor with a lower temperature and initiates its own heat release in them, resulting in a self-sustaining process of propagation of the reaction wave.
  • the device for generation of high-temperature reactive gas flow from water vapour is divided into four stages (sections, sectors) of water vapor treatment, wherein the main reagent is water and water vapor and wherein the resulting gas flow comprises hydrogen, oxygen and hydroxyl radicals, which may be further separated based on needs of users, systems and subsequent processing.
  • the plasma reactor comprises:
  • a first sector comprising at least: o a vaporization device, preferably comprising a reservoir for water, a high- pressure compressor and an ultrasonic nozzle for vaporization of said water, o a pipe, preferably a pipe twisted by a bifilar winding method of a spiral from titanium or tungsten carbide, for leading the water vapor, and o a heater to heat the water vapor and obtain superheated water vapor at temperature higher than 400 °C, wherein said heater is an inductor or a burner burning natural gas,
  • the second sector comprising a device for generating turbulent flow, preferably a swirler to create a swirling flow of superheated water vapor,
  • a third sector comprising a plasma-chemical flow reactor comprising multilayer electrodes, i.e. , cathodes and anodes, wherein preferably the cathode has a 2-3 mm thick quartz glass or ceramic insulation and the anode is a metal string or a metal plate made of stainless-steel, titanium or nichrome with jagged protrusions of a special geometry, and a power supply arranged to apply high-voltage direct impulse current of 18.000-60.000 kilovolts to the cathode and anode, that causes splitting of water vapor into hydrogen, oxygen and hydroxyl radicals,
  • the third sector of the device can be arranged to allow the gas mixture to be filtered using suitable filters in order to obtain pure hydrogen and oxygen gases stored in separate tanks.
  • the pipelines installed downstream of said filters may be provided with compressors to control the intensity of the gas flow.
  • the first and fourth sector may be combined to form a joint sector.
  • the method for generation of high-temperature reactive gas flow from water vapour with the plasma reactor comprises the following steps: a) supplying water to a vaporization device to create water vapor, b) generation of a superheated water vapor with a temperature higher than 400 °C by heating c) leading the superheated water vapor to a device for generating turbulent flow, preferably a swirler to create a swirling flow of superheated water vapor, d) leading the turbulent flow of superheated water vapor to a plasma-chemical flow reactor comprising several layers of cathodes and anodes, e) applying high-voltage direct impulse current of 18.000-60.000 kilovolts to the cathodes and anodes to cause an avalanche corona discharge, said avalanche corona discharge also causing at least one inductive coil to create an electromagnetic filed, f) creating a high-energy, high-temperature highly reactive gas mixture comprising hydrogen, oxygen and hydroxyl radicals due to splitting of the water molecules under the influence
  • the method also allows a step in which the gas mixture is separated into hydrogen and oxygen by separation through membrane filters.
  • the filtration may be performed with selective membranes made of alloys based on palladium (Pd), preferably obtained by rolling. Efficient membranes with an ultrathin layer of palladium coated with ruthenium or silver may be used to filter hydrogen due to their improved hydrogen permeability.
  • steps a and b may be combined to perform vaporization and heating together in one step.
  • a branch pipe may be provided for the removal of the gas stream split into hydrogen and oxygen, which is directed to the active membrane separator, in which separation takes place gas flow into hydrogen and oxygen with a hydrogen purity of 99.999%.
  • the method in addition or instead of step g) further comprises the following steps: h) the membrane with high hydrogen permeability is first heated by passing a pulsed electric current through it at a certain frequency, i) heating of the gas mixture to increase the diffusion capacity of the gas is performed, wherein due to the heating of the membrane element containing the catalyst with superheated steam, upon contact with the gas mixture, hydrogen molecules H2 are split and H atoms pass through the crystal lattice of the membrane, followed by the formation (recombination) of H2 molecules, j) pumping the hydrogen through a nozzle by a compressor into a suitable storage tank, wherein the remaining oxygen is also pumped through a second nozzle by a second compressor in a second storage tank.
  • an ultrasonic wave may be created inside the membrane filter chamber at the resonance frequency of the water molecule, which additionally creates an excited environment and significantly contributes to the intensification of the process.
  • emission gases are flowing in one direction, which is downwards, so they have to pass through the fluidized bed. Furthermore, the gas streams due to the grate may be recirculated inside the reactor until the complete destruction of any harmful gases.
  • the final processed gases are then led from the reactor towards a user, which may be a steam generator, a hydrogen producing device, etc. Due to leading away the gases, there is no pressure in the combustion chamber in the reactor. Rather, there is a negative pressure, i.e. a vacuum.
  • the entire movement of the gas mission is allowed by the operation of a thermal pump 25, which creates a rarefied medium in the reactor and determines a given forced flow of emission gases.
  • the intensity of plasma-chemical combustion processes is controlled by the supply of an oxidizers originating from the superheated steam that has been processed in the plasma reactor 23, and optionally by the supply of additional oxygen obtained as a result of the separation of superheated steam through a special membrane 24.
  • the flows of oxygen gases and the treated superheated steam are mixed in an injection mixer equipped with a special valve that prevents ignition of the vapor-gas mixture supplied inside the pipeline and is equipped with a nozzle 26 for supplying the step mixture into the reaction zone of the fluidized bed 22 along the grate at an angle of 30°.
  • Said nozzles are directed tangentially along the body, which creates a circular vortex flow (which additionally creates electrostatic discharges around the grate.
  • Said nozzles are made of a high-temperature alloy, they act as a purge of the combustion zone of the fluidized bed with a hydrogen-oxygen mixture.
  • the temperature may therefore reach 3.000° C (combustion temperature of HHO gas) and more.
  • This mode is used to dispose of the most hazardous waste.
  • a softer mode is provided by adjusting the intensity of dissociation of water vapor into hydrogen and oxygen in the plasmachemical reactor 23, there are several options for supplying gas to the fuel mixture.
  • an ionized vapor-gas mixture saturated with hydrogen, oxygen, ozone, and radicals of the hydroxyl group OH ° 100 % is sold into the reaction (combustion) zone derived from water.
  • the gas flow enters a steam boiler 31 , the hot gas recovery boiler generates steam to rotate the turbine, with subsequent recovery and condensation of the exhaust steam through the condenser-recuperator back into the water supply system to the steam boiler.
  • the superheated steam from the steam boiler 31 enters the steam turbine 32, the turbine rotates the generator 33, which in turn generates electricity (power transformer) 34.
  • the system allows for the disposal of 30 tons of garbage per day to generate up to 2 MW of electricity.
  • FIG. 5 shows a schematic diagram of a plasma chemical plant with subsequent generation of electricity and hydrogen.
  • the plant further comprises a PEM proton exchange membrane oxygen and hydrogen separation membranes 24, 25 provided downstream of the plasma reactor.
  • Vortex cyclone 26 is used for collection and granulation of ash residue, which is collected in the collector 29.
  • a steam boiler 31 with a secondary after burning system of reactor combustion products with hydrogenoxygen mixture is connected to the pipeline leading from the cyclone 26, wherein a nozzle 30 is provided for leading hydrogen-oxygen mixture to the steam boiler.
  • a steam turbine 32 is connected to the steam boiler 31 , followed by an alternator 33, a power transformer 34.
  • Hydrogen may be supplied to the plant also from additional reservoirs 36 and/or hydrogen compressor 35.
  • a vacuum pump 37 installed at the outlet is provided to provide vacuum conditions for the combustion.
  • Figure 6 shows temperature (T) and concentration profiles (Soh - gaseous oxidizer, Cf - solid propellant) of the filtration combustion wave in the case of equal heat capacity of the counter fluxes of solid and gas phases.
  • the arrow indicates the direction of gas flow.
  • the resulting hydrogen, oxygen and OH ° radicals act independently; under conditions of strong ionization and high temperature, the radicals exhibit special oxidizing properties.
  • the radicals of the hydroxyl group exhibit the highest chemical reactive oxidative activity. They enter into oxidative reactions with products of combustion and gasification, thereby splitting the molecules of matter in the course of the reaction, creating chain avalanche reactions, forming irreversible oxidative destructive processes. As a result, dioxins, furans, and other dangerous toxic gases are destroyed.
  • the membrane element is first heated by passing a pulsed electric current through it at a certain frequency. Heating of the gas mixture (to increase the diffusion capacity of the gas) is not required, because in this system we have a large amount of superheated steam and the reactor cooling system 10. Due to the heating of the membrane element containing the catalyst with superheated steam, upon contact with the gas mixture, hydrogen molecules are split, and H atoms pass through the crystal lattice of the membrane element, followed by the formation (recombination) of hydrogen molecules. To prevent sticking of oxygen molecules and atoms on the inner working surface of the membrane filter, an ultrasonic wave is created inside the membrane filter chamber at the resonance frequency of the water molecule, which additionally creates an excited environment and significantly contributes to the intensification of the process.
  • the method of waste destruction with the device as described above is the following. From the moment the reactor enters the operating mode, thermodynamic equilibrium is instantly established in the reaction zone. Thus, it happens that the products of gaseous emission leave the reaction zone at the maximum combustion temperature. This is extremely important from the point of view of the subsequent generation of hydrogen and electricity. To create a highly efficient superadiabatic filtration reactor, it is necessary to create a highly effective thermal insulation of the reactor walls, in which case the heat loss through the reactor walls will be insignificant relative to the thermal power generated in the plasma-chemical reaction zone, heat losses through the reactor walls can be neglected. The removal of heat from the reactor occurs due to the forced flow of hot reaction products. There is no conductive heat removal from the ends of the reactor.
  • the thickness of the thermochemical reaction zone can be considered small compared to the total thickness of the heated layer including the gasification zone, so the reaction zone is a break in the fluidized bed with infinite rates of chemical reaction and heat transfer, limited by the upper boundary layer separating the fluidized bed and the gasification zone.
  • a gaseous oxidizing agent hydrogen, oxygen, OH° radicals
  • water vapor it reacts with the carbon surface at a high temperature above 800 °C.
  • the product is enriched with hydrogen and carbon monoxide, the efficiency tends to the maximum value.
  • Adding carbon dioxide to a gaseous oxidizer works similarly. Thus, endothermic reactions most effectively create a thermal wave gradient locally, which reduces the thermal stress of the structure.
  • the efficiency of the general thermal front in the zone of chemical reactions the efficiency of gasification approaches 100%.
  • the reagents are completely consumed, complete burnout of the fuel from the condensed phase and complete consumption of the oxidizer supplied in excess, supplied with the gasifying agent.
  • the formation of CH4 during carbon gasification can be neglected, since it is important mainly during gasification at a pressure above atmospheric pressure.
  • the efficiency of recuperation can be as high as possible, and it is precisely in the presence of a sufficiently large amount of inert material (creating a fluidized bed) in the solid fuel and a sufficiently high content of the inert component in the gaseous oxidizer.
  • the inert components of the system are a very effective heat carrier, due to which both the fuel and the oxidizer can be heated with maximum efficiency before entering the chemical reaction zone.
  • the solid fuel is heated from the gaseous products of combustion, and the gaseous oxidizer is heated from the ash residue and the solid inert component, which is systematically removed mechanically by the lower grate 13.
  • nitrogen-containing organic compounds are partially decomposed in an oxygen-free environment (above the boundary layer), due to which the content of nitrogen oxides in flue gases is minimal.
  • flue gases contain extremely little CO and residual hydrocarbons, including carcinogenic polyaromatic ones.
  • OH 0 hydroxyl radicals the formation of dioxins, polychlorinated dibenzodioxins and dibenzofurans, is sharply reduced, since, even in the presence of chlorine in a preliminary diffuse flame, OH 0 radicals suppress the appearance of soot particles and aromatic compounds in flue gases predecessors dioxins and provides a low content of dust particles of catalysts for the formation of dioxins in flue gases.
  • the ash unloaded from the reactor has a low temperature and does not contain unburned carbon and organic substances, it is well granulated and can be used for construction purposes.

Landscapes

  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Plasma & Fusion (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Gasification And Melting Of Waste (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Le dispositif de destruction par plasma à haute température de déchets solides et liquides selon l'invention comprend un réacteur comprenant une entrée pour diriger des déchets à l'intérieur du réacteur et une sortie pour diriger un gaz et/ou de la chaleur créé(e) vers un dispositif de récupération de la chaleur résultante afin de simultanément produire de l'électricité et/ou de l'hydrogène vert conformément à des exigences environnementales relatives aux émissions de polluants dans l'atmosphère. Le principe de base du processus de destruction chimique par plasma à haute température de matière est le principe de la combustion par filtration superadiabatique. Ledit réacteur comporte trois zones : une zone de gazéification, un lit fluidisé à haute température et une zone de limite entre la zone de gazéification et le lit fluidisé, ce dernier étant exposé à des radicaux hydrogènes, oxygènes et hydroxyles produits par un réacteur à plasma, conduisant ainsi à l'oxydation et par conséquent à la destruction de déchets ainsi que de tout composé potentiellement toxique, vapeur, gaz ou sous-produit.
PCT/EP2024/060206 2023-04-18 2024-04-15 Dispositif et procédé de destruction par plasma à haute température de déchets Pending WO2024218048A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP23168619.7 2023-04-18
EP23168619.7A EP4450871A1 (fr) 2023-04-18 2023-04-18 Dispositif et procede de destruction de dechets par plasma a haute temperature

Publications (2)

Publication Number Publication Date
WO2024218048A2 true WO2024218048A2 (fr) 2024-10-24
WO2024218048A3 WO2024218048A3 (fr) 2024-12-05

Family

ID=86095664

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2024/060206 Pending WO2024218048A2 (fr) 2023-04-18 2024-04-15 Dispositif et procédé de destruction par plasma à haute température de déchets

Country Status (2)

Country Link
EP (1) EP4450871A1 (fr)
WO (1) WO2024218048A2 (fr)

Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018164651A1 (fr) 2017-03-07 2018-09-13 Fedorov Saveliy Dmitrovych Procédé et gazéifieur de combustible solide combiné pour la gazéification de combustible solide
CN217973078U (zh) 2022-02-22 2022-12-06 哈尔滨工业大学 一种基于过滤燃烧模式的复合气化装置

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7832344B2 (en) * 2006-02-28 2010-11-16 Peat International, Inc. Method and apparatus of treating waste
CN101560401B (zh) * 2008-11-09 2012-12-26 周开根 一种垃圾生物质气化炉
EP2571962B1 (fr) * 2010-05-19 2018-10-10 Green Energy And Technology Sdn. Bhd. Procédé et système pour produire de l'énergie à partir de déchets

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2018164651A1 (fr) 2017-03-07 2018-09-13 Fedorov Saveliy Dmitrovych Procédé et gazéifieur de combustible solide combiné pour la gazéification de combustible solide
CN217973078U (zh) 2022-02-22 2022-12-06 哈尔滨工业大学 一种基于过滤燃烧模式的复合气化装置

Also Published As

Publication number Publication date
WO2024218048A3 (fr) 2024-12-05
EP4450871A1 (fr) 2024-10-23

Similar Documents

Publication Publication Date Title
JP6130837B2 (ja) 高分子物質の効率的でクリーンな燃焼方法及び装置
US9410095B2 (en) Method of gasification of biomass using gasification island
US20070204512A1 (en) Steam reformation system
EA024852B1 (ru) Способ и устройство для сжигания топлива при высокой температуре и высоком давлении и соответствующие система и средства
WO1994004631A1 (fr) Procede d'elimination de dechets solides urbains
RU2424277C2 (ru) Способ парового риформинга углеродистого материала
US20050070751A1 (en) Method and apparatus for treating liquid waste
CN102317687A (zh) 用于处理固体废弃物的方法和设备
EP4450871A1 (fr) Dispositif et procede de destruction de dechets par plasma a haute temperature
WO2006075978A1 (fr) Procede de traitement par plasma thermique d'un combustible organique, et installation permettant sa mise en oeuvre
RU2729301C1 (ru) Утилизатор бытовых отходов
JPH02501326A (ja) 廃棄物のクリーン焼却法
RU2218378C1 (ru) Способ утилизации нефтяных шламов и плазмокаталитический реактор для его осуществления
EP3498665B1 (fr) Appareil de production de gaz de synthèse
CN110184095A (zh) 一种固体废弃物热解气化合成气净化处理方法及装置
JP2011522200A (ja) マテリアル酸化プロセスおよび関連装置
RU2716652C1 (ru) Топка для утилизации ТКО
KR102364211B1 (ko) 가스화 디바이스 및 가스화 디바이스의 마이크로파 플라즈마 지연 시스템을 구비한 플라즈마 셔터
EP0687862A1 (fr) Procédé et dispositif pour l'élimination des déchets municipaux solides par gazéification et scorification
CN106190315A (zh) 一种垃圾、固体废物气化系统
CN113578921B (zh) 一种城镇生活垃圾高温热裂解工艺
CN112094661A (zh) 有机固体废弃物处理方法和处理装置
KR20210053536A (ko) 과열증기 생성장치
JP6574183B2 (ja) 固体、液体、または気体炭化水素（ｈｃ）原材料の熱機関での燃焼のプロセス、炭化水素（ｈｃ）材料からエネルギーを作り出す熱機関およびシステム
HU225373B1 (en) Method and apparatus for the prevention of global warming, through elimination of hazardous exhaust gases of waste and/or fuel burners