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WO2016040969A1 - Procédé et dispositif de production d'un gaz de synthèse à partir de déchets carbonés - Google Patents

Procédé et dispositif de production d'un gaz de synthèse à partir de déchets carbonés Download PDF

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Publication number
WO2016040969A1
WO2016040969A1 PCT/AT2015/000116 AT2015000116W WO2016040969A1 WO 2016040969 A1 WO2016040969 A1 WO 2016040969A1 AT 2015000116 W AT2015000116 W AT 2015000116W WO 2016040969 A1 WO2016040969 A1 WO 2016040969A1
Authority
WO
WIPO (PCT)
Prior art keywords
section
reaction chamber
synthesis gas
conveyor
waste materials
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.)
Ceased
Application number
PCT/AT2015/000116
Other languages
German (de)
English (en)
Inventor
Markus Primavesi
Paul Primavesi
Jean Jacques WEILAND
Pierre Holzschuh
Faker LEVIEV
Johannes Stari
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.)
Ame Handelsgesellschaft MBH
Original Assignee
Ame Handelsgesellschaft MBH
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 Ame Handelsgesellschaft MBH filed Critical Ame Handelsgesellschaft MBH
Publication of WO2016040969A1 publication Critical patent/WO2016040969A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/18—Continuous processes using electricity
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/087—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • B01J19/088—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/18—Stationary reactors having moving elements inside
    • B01J19/20—Stationary reactors having moving elements inside in the form of helices, e.g. screw reactors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
    • 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
    • C10J3/002—Horizontal gasifiers, e.g. belt-type gasifiers
    • 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
    • C10J3/007—Screw type gasifiers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00389—Controlling the temperature using electric heating or cooling elements
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/123—Heating the gasifier by electromagnetic waves, e.g. microwaves
    • C10J2300/1238—Heating the gasifier by electromagnetic waves, e.g. microwaves by plasma
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2203/00—Furnace arrangements
    • F23G2203/80—Furnaces with other means for moving the waste through the combustion zone
    • F23G2203/801—Furnaces with other means for moving the waste through the combustion zone using conveyors
    • F23G2203/8013—Screw conveyors

Definitions

  • the invention relates to a method and a device for producing synthesis gas from carbonaceous waste materials, in which the carbonaceous waste materials are fed to a reaction chamber in which the waste materials, optionally with external energy supply, are subjected to pyrolysis at temperatures of 600-1,300 ° C. wherein the resulting syngas and the solid residues are discharged from the reaction chamber.
  • pyrolysis or synthesis gases produced by such processes can be burnt off after discharge, in particular used as engine gas in a gas engine, used as synthesis gases for the chemical industry or in the metal-producing industry, liquefied, used for gas turbines or as natural gas substitution.
  • the synthesis gas consists mainly of CH 4 .
  • Anoxic conditions are understood here as conditions in which free oxygen is not added. Anoxic conditions are thus characterized by the fact that hot air or oxygen does not enter the reactor in which the gasification is carried out.
  • oxygen compounds such as water vapor
  • CO2 are well implemented in such a gasification process, wherein in the case of CO2 in the presence of carbon at correspondingly high temperatures, the equilibrium is quantitatively on the side of carbon monoxide and when injecting water on the side of synthesis gas, namely carbon monoxide and hydrogen.
  • the present invention includes both autothermal high temperature gasification processes in which pyrolysis is independent of external heat input because the glowing waste supplies the energy for gasification, as well as allothermal gasification processes which require external energy input.
  • a disadvantage of autothermal gasification processes is that high demands are placed on the calorific value of the waste materials used.
  • the invention is based on a pyrolysis process in which the thermal decomposition of the starting materials takes place at temperatures of 600-1,300 ° C. Such temperatures are in allothermal gasification processes by combustion of primary energy sources in the reaction chamber or by an external heat input, such. achievable by electrical heating of the reaction chamber.
  • biomass and various carbonaceous wastes including e.g. contaminated soils, sewage sludge, cellulose slurries, filter residues and the like. , proposed.
  • the synthesis gas may still contain unwanted substances such as toxic substances (eg tars, dioxins, furans) and / or minerals in conventional gasification processes.
  • toxic substances eg tars, dioxins, furans
  • the solid residues usually contain carbon that has not been converted. The present invention therefore aims to develop a method and a device of the type mentioned in that the disadvantages mentioned above can be at least partially avoided.
  • the invention provides in a method of the type mentioned above, that the solid residues and / or the synthesis gas for further decomposition or decomposition are exposed to a plasma.
  • a plasma the residual carbon contained in the solid residues can be converted to CO, so that the calorific value of the resulting synthesis gas can be increased.
  • the mineral components which may be contained in the synthesis gas can thereby be vitrified and discharged as slag. In the slag possibly existing heavy metals and other substances such. Sulfur are bound.
  • plasma it is possible to crack open the undesired substances contained in the synthesis gas so that synthesis gas which has been freed of pollutants can be made available.
  • temperatures are significantly higher than in the first stage. Preference is given to proceeding in such a way that the solid residues and, if appropriate, the synthesis gas in the reaction zone of the plasma are brought to at least 1500 ° C., preferably at least 2400 ° C., preferably at least 4000 ° C. In this case, temperatures of up to 15,000 ° C. prevail in the reaction zone.
  • the organic constituents of the residual substances remaining from the first stage, in particular the residual carbon, are thereby completely converted and mineral and metallic constituents of the residues left over from the first stage sinter into a glassy ash.
  • the plasma is preferably generated by application of electrostatic fields.
  • the procedure is such that a sufficiently high electrical DC voltage is applied between two electrodes, with a suitable combination of voltage, electrode spacing and gas pressure causing a flashover and the ignition of a discharge between the electrodes.
  • a gas is passed through which is ionized to a plasma.
  • the recombination of the ionized atoms occurs and thus a considerable increase in temperature. through the also inert compounds obtained for a complete implementation activation energy.
  • plasma gas in this case can air, 0 2 , H0, C0 2 od. Like. to be used.
  • a plasma injector suitable for the preparation of a cantilevered plasma is characterized in that it manages without counter electrode.
  • a Plasmain ector is characterized in that it manages without counter electrode.
  • the thermal decomposition of the waste materials in the reaction chamber preferably takes place in such a way that the reaction chamber comprises a first section and a second section connected thereto, wherein the waste passes through the first section under anoxic conditions and is pyrolyzed there, then into The second section is spent and that in the second section substoichiometric oxygen, water vapor and / or C0 2 is introduced to ensure a conversion of the residual carbon to CO or CH 4 .
  • the actual pyrolysis, ie the thermal decomposition with exclusion of oxygen thus occurs only in said first section, whereas in the second section a substoichiometric oxygen, C0 2 and / or water vapor introduction takes place.
  • the pyro ⁇ lysis causes a splitting of the water content contained in the waste materials in 0 2 and H 2 .
  • the 0 2 portion reacts with part of the carbon contained in the waste to CO.
  • the substoichiometric blowing of 0 2 causes a conversion of remaining in the waste residual carbon in CO. If alternatively or additionally superheated steam is injected, the remainder of the carbon in CO and CH 4 implemented.
  • CO2 When CO2 is injected, it is split into CO and O, with the free oxygen oxidizing with the residual carbon of the waste to CO (C0 2 + C -> 2C0).
  • the reaction chamber comprises a heatable conveying device, in particular a screw conveyor, with which the waste materials in the reaction chamber, in particular by this, are transported.
  • the conveyor is thus responsible for both the transport of the starting materials and for the heat input.
  • a particularly preferred embodiment provides that the first section and optionally the second section of the reaction chamber is formed by the heatable conveyor, in particular the screw conveyor.
  • the reaction space is thus cylindrical, wherein the cylinder is penetrated in the axial direction of the screw conveyor.
  • the auger ensures a continuous transport and at the same time a constant circulation of the feed material. When the auger itself is heated, this also causes the constant renewal of the material in contact with the heated surface.
  • the conveyor is electrically heated, in particular inductive, conductive or capacitive. With such heating, the atmosphere in the first section of the reaction chamber can be kept reliably anoxic.
  • the heating of the conveyor does not have to extend over the entire length of the conveyor, but can also concern only a subarea.
  • the heating may be restricted to the first section of the reaction chamber in which the pyrolysis is carried out.
  • the following second section may be waived due to the possibly exiting exothermic oxidation reactions to a heating under certain circumstances.
  • the inductive heating of the conveyor is advantageous not only in the case of a screw conveyor, but also in differently designed conveyors with metallic entrainment elements, because the energy can be introduced directly into those elements of the conveyor, which is in contact with the feed, so that an efficient heat transfer can take place ,
  • the contactless heat input can also be realized independently of the conveyor.
  • an inductively heated bed of elements which can be excited to inductive coupling in particular steel balls
  • the inductive heating by lumpy elements, such as steel balls, which couple to an induction field applied to the outside of the reaction chamber, ensures a particularly uniform heat input in the entire cross section of the reaction chamber.
  • the process is preferably carried out so that the waste in the first section of the reaction chamber are heated to a temperature of 500-1,000 ° C.
  • the waste materials are preferably brought to a higher temperature than the first section, in particular to a temperature of 800-1,200 ° C.
  • the procedure according to the invention can be such that a partial amount of the synthesis gas produced is burned in the reaction chamber to achieve the gasification temperature. As a result, the temperature in the reaction chamber can be increased.
  • the solution of the problem underlying the invention is also a device for the production of synthesis gas from carbonaceous waste materials comprising a heatable reaction onshunt to subject the carbonaceous waste under external energy pyrolysis, with at least one discharge opening for discharging the resulting synthesis gas and the solid residues , which is characterized in that the at least one discharge opening is connected to a plasma reactor, in which the solid residues and / or the synthesis gas for further decomposition or decomposition can be acted upon by a plasma.
  • the device is particularly suitable for carrying out the method according to the invention.
  • the fact that the reaction chamber is connected to the plasma reactor via a discharge opening does not necessarily mean that the plasma reactor is spatially separated from or separate from the reaction chamber. It is also conceivable that the plasma reactor is formed in a separate section of the reaction chamber.
  • a preferred embodiment provides that the inventionskam ⁇ mer a heatable conveyor, in particular a Screw conveyor, comprises, with which the waste materials in the reaction chamber, in particular by these, are transportable.
  • reaction chamber comprises a first section and a second section connected thereto, wherein the first section forms a pyrolysis chamber and at least one line for introducing oxygen and / or water vapor opens into the second section.
  • the first section and possibly the second section of the reaction chamber can be formed by the heatable conveyor, in particular a screw conveyor.
  • the second section directly adjoins the first section of the reaction chamber.
  • the conveyor to an electric heating, in particular for inductive, conductive or capacitive heating of the conveyor.
  • the invention is suitable for the utilization of biomass, plastic waste, waste from the paper industry (cellulose sludge), sewage sludge, hospital waste, waste from the pharmaceutical industry, pharmacy waste, contaminated railway sleepers, waste from the oil / gas industry and the like.
  • FIG. 1 shows a first embodiment of the device according to the invention
  • FIG. 2 shows a modified one Training
  • Fig. 3 shows a further modified embodiment of the device.
  • Fig. 1 shows a cylindrical reactor 1 with a funnel-shaped Materialaufgäbe 2.
  • the cylindrical wall of the reactor 1 forms together with a coaxial with the wall conveyor screw 3 from a screw conveyor, the material discontinued on the material 2 material in the direction of arrow 4 by the reaction chamber 5 transports.
  • a coil 6 which can be connected to a power source surrounds the reactor jacket and forms an inductive heater for the screw conveyor 3.
  • the screw conveyor is therefore formed from a stimulable for inductive coupling material, in particular steel.
  • the reactor shell does not consist of a stimulable for inductive coupling material.
  • a feed line 9 opens in the interior of the reactor 1, via which reaction gases, such as air, 0 2 / C0 2 and / or H 2 0 can be introduced.
  • the screw conveyor 3 extends through both the first section 7 and the second section 8 of the reactor 1.
  • a discharge line 10 flows through the bottom, via which the reaction products are discharged from the reactor 1 and be introduced into a plasma reactor 11.
  • a För ⁇ Dersch corner 12 is disposed, with which the on Abzugslei- tung 10 material coming one plasma injector is supplied.
  • an upward-directed synthesis gas outlet 14 and in the bottom an ash / slag discharge 15 are provided.
  • the temperature in the reactor 1 can, however, be ⁇ vorzugt to about 1,000 ° C are limited, with higher temperature ⁇ temperatures (> 1500 ° C) until the following plasma reactor 11 be ⁇ sets.
  • the higher temperatures increase the conversion rate and allow the thermal decomposition of any undesirable substances present in the feedstock, such as tar-forming compounds and toxic substances, which is ensured only in this temperature range.
  • Fig. 2 is a comparison with the Fig. 1 modified embodiment is shown, wherein the same reference numerals are used for the same or corresponding parts as in Fig. 1.
  • the plasma reactor 11 is not a structurally separate unit but is formed in an end portion of the reaction chamber 5.
  • the training corresponds substantially to the embodiment of FIG. 1, wherein the drive of the screw 3 of the screw conveyor is denoted by 16.
  • the induction coil 6 in the embodiment according to FIG. 2 extends only over the first section 7 of the reaction chamber 5.
  • the induction coil 6 is not in this case Outside of the reactor 1 arranged, but on the inner wall.
  • the reaction chamber 1 together with the integrated plasma reactor 11 is designed as a stationary fall reactor with a rotary grate 19 arranged in the floor area (rotary grate actuator).
  • the feedstock is fed via the Materialaufgäbe 2 with a gas-tight rotary valve 17 and will expand due to the gravity effect in downwards ⁇ moves the reactor down.
  • the reactor wall and the material are heated inductively, wherein the induction coil is again denoted by 6.
  • the induction coil is again denoted by 6.
  • the lower third of the reactor opens a blowing device 9 in the reactor, with which Reak ⁇ tion gases, such as O2, water vapor and / or C0 2 are introduced into the second section 8 of the reactor.
  • a plasma in ⁇ ector 13 is arranged so that in the lower region of the reactor that is above the rotary grate 19, a plasma reactor 11 is formed directly.
  • the solid residues falling through the rotary lattice 19 are removed via an ash / slag outlet 15 provided with a screw conveyor 21. carried.
  • the synthesis gas is discharged upwards via the line 14.
  • the fill level of the reactor 1 can be detected with the aid of level sensors 20, wherein the measured values of the level meter 20 are fed to a control device (not shown) with which the material input is controlled as a function of the fill level.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Toxicology (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

Procédé et dispositif de production de gaz de synthèse à partir de déchets carboné. Selon ce procédé, les résidus carbonés sont chargés dans une chambre de réaction (5), dans laquelle ils sont soumis à une pyrolyse à des températures de 600-1300°C, avec un apport éventuel d'énergie externe, le gaz de synthèse résultant et les résidus solides étant évacués de la chambre de réaction (5). Les résidus solides et/ou le gaz de synthèse sont ensuite exposés à un plasma en vue d'une transformation ou d'une décomposition additionnelle.
PCT/AT2015/000116 2014-09-16 2015-09-03 Procédé et dispositif de production d'un gaz de synthèse à partir de déchets carbonés Ceased WO2016040969A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
ATA707/2014 2014-09-16
ATA707/2014A AT516178B1 (de) 2014-09-16 2014-09-16 Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen

Publications (1)

Publication Number Publication Date
WO2016040969A1 true WO2016040969A1 (fr) 2016-03-24

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AT (1) AT516178B1 (fr)
WO (1) WO2016040969A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT518474A1 (de) * 2016-04-12 2017-10-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
EP3498665A1 (fr) 2017-12-18 2019-06-19 Clariant International Ltd Appareil de production de gaz de synthèse
AT527982A1 (de) * 2024-02-05 2025-08-15 Jenascent Gmbh Reaktor zur Erzeugung von Kohle und Synthesegas aus Biomasse

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT518754A2 (de) * 2016-06-13 2017-12-15 Gs Gruber-Schmidt Gmbh Vergasung biogener Stoffe in einem Doppelschneckenreaktor mit Hilfe von Mikrowellen Plasma

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0184405A2 (fr) * 1984-12-03 1986-06-11 Canadian Patents & Development Ltd. Procédé et appareil pour la réduction de minerais par fusion
WO2001005910A1 (fr) * 1999-07-19 2001-01-25 Nuova Meccanica S.R.L. Procede et dispositif de production de gaz combustible a partir de dechets carbones
WO2007065202A1 (fr) * 2005-12-05 2007-06-14 Struan Glen Robertson Dispositif de traitement de matieres
WO2008130260A1 (fr) * 2007-04-18 2008-10-30 Sgc Energia Sgps, S.A. Système de raffinage déchets en hydrocarbure liquide
AT507629A1 (de) 2008-12-05 2010-06-15 New Plasma Gmbh & Co Keg Vorrichtung zur erzeugung von plasma
US20120217150A1 (en) * 2006-11-06 2012-08-30 Kostek Sr Stanislaw Methods and apparatus for pyrolyzing material

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102006007457B4 (de) * 2006-02-17 2007-12-27 Native Power Solutions Gmbh & Co. Kg Verfahren und Vorrichtung zum Erzeugen von Gas aus kohlenstoffhaltigem Material
ES2670801T3 (es) * 2010-05-10 2018-06-01 Indian Oil Corporation Limited Generador de gas de dos etapas para generar gas de síntesis
CN101906325B (zh) * 2010-07-20 2013-09-04 阳光凯迪新能源集团有限公司 生物质低温裂解高温气化工艺及其设备

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0184405A2 (fr) * 1984-12-03 1986-06-11 Canadian Patents & Development Ltd. Procédé et appareil pour la réduction de minerais par fusion
WO2001005910A1 (fr) * 1999-07-19 2001-01-25 Nuova Meccanica S.R.L. Procede et dispositif de production de gaz combustible a partir de dechets carbones
WO2007065202A1 (fr) * 2005-12-05 2007-06-14 Struan Glen Robertson Dispositif de traitement de matieres
US20120217150A1 (en) * 2006-11-06 2012-08-30 Kostek Sr Stanislaw Methods and apparatus for pyrolyzing material
WO2008130260A1 (fr) * 2007-04-18 2008-10-30 Sgc Energia Sgps, S.A. Système de raffinage déchets en hydrocarbure liquide
AT507629A1 (de) 2008-12-05 2010-06-15 New Plasma Gmbh & Co Keg Vorrichtung zur erzeugung von plasma

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT518474A1 (de) * 2016-04-12 2017-10-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
AT518474B1 (de) * 2016-04-12 2020-08-15 Ame Handelsgesellschaft M B H Verfahren zur Erzeugung von Synthesegas aus kohlenstoffhaltigen Abfallstoffen
EP3498665A1 (fr) 2017-12-18 2019-06-19 Clariant International Ltd Appareil de production de gaz de synthèse
WO2019121312A1 (fr) 2017-12-18 2019-06-27 Clariant International Ltd Procédé de production d'un gaz de synthèse
AT527982A1 (de) * 2024-02-05 2025-08-15 Jenascent Gmbh Reaktor zur Erzeugung von Kohle und Synthesegas aus Biomasse

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AT516178B1 (de) 2016-03-15

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