EP1218471B1 - Verfahren und vorrichtung zum gewinnen heizwertreicher brenngase - Google Patents
Verfahren und vorrichtung zum gewinnen heizwertreicher brenngase Download PDFInfo
- Publication number
- EP1218471B1 EP1218471B1 EP00969430A EP00969430A EP1218471B1 EP 1218471 B1 EP1218471 B1 EP 1218471B1 EP 00969430 A EP00969430 A EP 00969430A EP 00969430 A EP00969430 A EP 00969430A EP 1218471 B1 EP1218471 B1 EP 1218471B1
- Authority
- EP
- European Patent Office
- Prior art keywords
- solid particles
- bed
- heating
- reaction zone
- gasification
- 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.)
- Expired - Lifetime
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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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- 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
- C10J3/48—Apparatus; Plants
- C10J3/482—Gasifiers with stationary fluidised bed
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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
- C10J2200/00—Details of gasification apparatus
- C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
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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
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—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
- C10J2300/12—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
Definitions
- the invention relates to a method for recovering high-calorie fuel gases and a device for carrying out the method.
- Substantial advantage of the gasification compared to the combustion is that in the Starting substance contained pollutants in a reducing atmosphere in components or converted into relatively simple chemical compounds.
- the gas volumes are significantly smaller compared to the combustion, so that a gas cleaning at Gasification compared to combustion with the same objective easier and less expensive can be done.
- the allothermal water vapor gasification of solid, pasty or liquid fuels usually finds in one to ensure uniform reaction conditions Fluidized bed instead.
- This is a bed of small solid particles from below with Steam streamed. The flow velocity is so great that the solid particles at least held in suspense.
- One speaks of a stationary one Fluidized bed when the solid particles have a well-defined surface with ascending Form gas bubbles, while in a circulating fluidized bed, the essential Part of the solid particles discharged with the gas stream from the fluidized bed reactor, separated from the gas stream and then over a fall distance again the the lower part of the actual fluidized bed reactor is supplied.
- the solid particles may be inert, e.g. quartz sand, limestone, dolomite, corundum or similar; she However, they can also consist of the ashes of the fuel.
- the solid particles can accelerate the gasification reactions by catalytic properties.
- a fluidized bed is a proven and widely used technology for many years. Areas of application are e.g. the drying and combustion of solids or from muds. Basis of each fluidized bed process is a reactor in which a Solid inventory is loosened by flow from the bottom so far that the individual particles begin to float in the air, the solid inventory is fluidized.
- the method according to the invention and the invention Device no heating device in the reaction chamber.
- inventive Method and the inventive device are not limited to special heaters, but allow the use of any heating devices, in particular tubular heat exchanger.
- no fuel particles get out of the reducing into an oxidizing zone.
- the embodiment of the reaction space be made regardless of the geometric specifications for the heating, so that the size of the device according to the invention can be optimized.
- the descending first bed by injection of a gas loosened or slightly fluidized, causing advantageously prevents undesirable agglomeration of the solid particles and the transport of the bed material is supported.
- the heating medium in the heat release to pulsate on the descending first bed in the heat exchanger.
- the heat transfer from the heat exchanger to the descending first Bed improved.
- the gasification can take place under pressure or under atmospheric conditions.
- the carbonaceous substances may consist of liquid, pasty or solid substances, especially from coke, petroleum, biomass or waste materials. advantageously, thus, the inventive method allows the processing of a variety of carbonaceous substances.
- water vapor is used as a gasifying agent.
- the Heating area and the reaction area by a different fluidization of the Be separated fluidized bed wherein the different fluidization a circulation of the Bed material caused by one or more substantially horizontal axis.
- the im Essential horizontal axes can be closed annularly.
- These Embodiment of the device according to the invention is particularly characterized a compact design.
- Device are the heating area and the reaction area through a wall separated. Furthermore, the heating area and the reaction area can each be in one own reactor to be formed. These two embodiments offer the advantage a safe separation of the heating area from the reaction area by constructive Activities.
- the device for the transfer of the heated solid particles may be a wall opening or a pipe. Furthermore, this facility can be used for the transfer of the heated solid particles in a lower region of the heating be provided. In a preferred embodiment, this device a nozzle bottom, with the help of a slight fluidization of the solid particles can be done in the heating.
- the indirect Heat supply device at least one of a heating medium flowed through Heat exchanger, which is provided in or on the heating area.
- Heat exchanger as a heat supply device simplifies the construction of the reactor.
- the heat exchanger may have at least one resonance tube, in which the heating medium in the heat transfer to the heating pulsating flows.
- the resonance tube can resonant with a Combustion chamber be connected.
- the generation of the desired resonance can also with the help of an acoustic vibrator, which is separate from the combustion chamber is arranged.
- the means for generating the ascending, fluidizing fluidized bed a in a lower region of the reaction area provided nozzle bottom.
- a nozzle bottom offers the advantage of being even inject the fluidizing medium into the reaction zone.
- the device for separating the gases produced during the gasification from the solid particles can be a cyclone.
- a device for the transfer the solid particles from the reaction area provided in the heating area be. This device may be a wall opening or a pipe. preferably, this device is provided in an upper region of the reaction region.
- the supply area for the carbonaceous substances can open into the heating area.
- a supply device for the carbonaceous substances also in open the reaction area.
- the embodiment of the device according to the invention shown in FIG. 1 comprises a reaction zone 3 in which carbonaceous substances are gasified.
- the carbonaceous Substances are located in an ascending, fluidized fluidized bed 2, which is generated by means of the device 4 in the reaction region 3.
- These in the bottom Provided area of the reaction region 3 means 4, for example, a open or closed nozzle bottom, through which the fluidizing medium Steam is injected.
- the water vapor can be mixed with gases.
- the Nozzle bottom 15 delimits the reaction region 3, in which the fluidized bed 2 is formed is.
- Trigger from which e.g. Bedding, impurities from the fuel, ashes and Unreacted fuel components can be deducted.
- the embodiment shown further comprises a heating region 6, which from the reaction region 3 through a device 9 is separated.
- a heating region 6 which from the reaction region 3 through a device 9 is separated.
- a nozzle bottom 22 may be arranged, flows through the steam, the to Improving the transport of material that loosens up the bed material of the heating zone or slightly fluidized.
- a device 8 for the indirect Heat supply arranged in the heating region 6, in the heating region 6, a device 8 for the indirect Heat supply arranged.
- This heat supply device 8 for example, a or more heat exchangers.
- the present invention is not limited to the specific arrangement of the heat exchanger 12 shown in FIG. 1 is limited, but that other arrangements, for example, on the wall of the heating area 6, are also conceivable.
- a planar heat exchanger for example, in the wall the heating area 6 is integrated, are used.
- the provided in the heating heat exchanger 12 may partially from resonance tubes 13 exist in which the heating medium in the heat dissipation in the heating 6 pulsating flows.
- the resonance tubes 13 are for generating the resonance vibration with a combustion chamber, not shown, or other resonant generator connected.
- the heating of the heating medium takes place directly by combustion a combustible substance with oxygen-containing gas.
- the heating of the solid particles thus takes place separately from the taking place in the reaction chamber 3 gasification. Due to the weak fluidization of the heating area forms there a slow descending bed 1, while due to the strong fluidization of the reaction region 3 there is a fast ascending fluidized bed 2 forms.
- the heat exchanger 12 in the slow descending bed 1 is the strong mechanical abrasion of the Heat exchanger, which previously took place in the prior art, reduced. Furthermore is the heat exchanger 12 in the heating less severe corrosion effects exposed in the reaction region 6. This means that the reactor thereby a longer Life has.
- the heating area 6 is connected to the reaction area 3 via a device 7, with their help the heated in the heating area 6 solid particles in the reaction area 3 are transferred.
- this device 7 as Wall opening 10 is formed.
- This device 7 can also be, for example, as Be formed pipe.
- the device 7 have a nozzle bottom 11 for the transfer of the heated solid particles. With the help of this nozzle bottom 11, the solid particles can be loosened or light be fluidized.
- the nozzle bottom 11 can for generating the ascending, fluidized Fluid bed 2 used nozzle bottom 15 are used, taking into account must be that in the reaction area 3 a greater fluidization than in the heating 6 takes place.
- This device 16 can, as in Fig. 1 shows a wall opening 17 his. It is also conceivable, this device 16 to train as a pipeline.
- the device 5 for the separation of the resulting in the gasification Gases from the solid particles and for the discharge of these gases are in the In Fig. 1 embodiment shown internals 18 and 19.
- the internals 18 and 19 cause a sharp deflection of the flow, which does not follow the solid particles can. Gas flow and solid particle flow thus separate at the internals.
- the Gas flow is removed via the gas path 20 through which the internals 18 and 19 are separated.
- the solid particle stream rains in the heating area 6, which is below the internals 18 and 19 is located.
- a feed device 21 opens for the carbonaceous substances in the Aufflower Scheme 6.
- the fuel can either Pressed in the area of the bed 1 or dropped from the top of the bed 1 become.
- a further supply device which opens into the reaction region 3.
- the bed material is in a cyclone separated from the gas stream and the descending bed 1 again the lower Area of the ascending bed 2 supplied.
- the gas stream flows over in this case the tube 23 tangentially into the separator 5 formed as a cyclone.
Description
- DE 28 36 531:
- Ein stationäres Wirbelschichtverfahren, bei dem mittels Einbau einer Trennwand Bereiche unterschiedlicher Fluidisierung ausgebildet werden, so daß sich in einem stationären Bett eine Zirkulation von Bettmaterial einstellt.
- EP 0302 849:
- Eine zirkulierende Wirbelschicht, die eine Weiterentwicklung der DE 28 36 531 darstellt, durch ihre Baugröße jedoch eher an eine stationäre als an eine zirkulierende Wirbelschicht erinnert.
- DE 33 20 049:
- Ein stationäres Wirbelschichtverfahren, bei dem sich durch unterschiedliche Betthöhen eine Zirkulation von Bettmaterial einstellt.
- WO 90105020:
- Eine extern zirkulierende Wirbelschichtfeuerung, bei der im absteigenden Bett Wärmetauschflächen zur Kühlung des umlaufenden Bettmaterials angeordnet sind.
- Fig. 1
- einen Querschnitt durch eine Ausführungsform der erfindungsgemäßen Vorrichtung, bei der die Einrichtung zur Trennung der Gase von den Feststoffpartikeln Einbauten aufweist, und
- Fig. 2
- einen Querschnitt durch eine andere Ausführungsform der erfindungsgemäßen Vorrichtung, bei der die Einrichtung zur Trennung der Gase von den Feststoffpartikeln ein Zyklon ist.
Claims (28)
- Verfahren zum Gewinnen heizwertreicher Brenngase, bei welchem kohlenstoffhaltige Stoffe in einer Feststoffpartikel enthaltenden Wirbelschicht mit Hilfe eines gasförmigen Vergasungsmittels unter Wärmezufuhr allotherm vergast und die gebildeten Gase von den Feststoffpartikeln getrennt und abgezogen werden, wobei die Feststoffpartikel in einem absteigenden ersten Bett (1) indirekt erwärmt und einem aufsteigenden, fluidisierten zweiten Bett (2) zugeführt werden, in dem die Wirbelschicht gebildet wird und der Hauptteil der Vergasung erfolgt.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das absteigende erste Bett (1) durch Einspritzung eines Gases aufgelockert wird.
- Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das absteigende erste Bett (1) leicht fluidisiert wird.
- Verfahren nach wenigstens einem der vorstehenden Ansprüche, dadurch gekennzeichnet, daß das absteigende erste Bett (1) indirekt mit Hilfe eines Wärmetauschers, durch den ein Heizmedium strömt, erwärmt wird.
- Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß das Heizmedium bei der Wärmeabgabe an das absteigende erste Bett (1) pulsierend strömt.
- Verfahren nach wenigstens einem der vorstehenden Ansprüche, dadurch gekennzeichnet, daß die Vergasung unter Druck erfolgt.
- Verfahren nach wenigstens einem der Ansprüche 1 bis 5, dadurch gekennzeichnet, daß die Vergasung unter atmosphärischen Bedingungen erfolgt.
- Verfahren nach wenigstens einem der vorstehenden Ansprüche, dadurch gekennzeichnet, daß die kohlenstoffhaltigen Stoffe aus flüssigen, pastösen oder festen Stoffen, insbesondere aus Koks, Erdöl, Biomasse oder Abfallstoffen, bestehen.
- Verfahren nach wenigstens einem der vorstehenden Ansprüche, dadurch gekennzeichnet, daß das Vergasungsmittel Wasserdampf ist.
- Vorrichtung zur Durchführung des Verfahrens nach Anspruch 1 miteinem Reaktionsbereich (3) für die Vergasung der kohlenstoffhaltigen Stoffe,einer Einrichtung (4) zur Erzeugung des aufsteigenden fluidisierten Wirbelschichtbettes (2) im Reaktionsbereich (3)einer Einrichtung (5) zur Trennung der bei der Vergasung entstehenden Gase von den Feststoffpartikeln und zur Abführung dieser Gase,einem Aufheizbereich (6) für die Aufheizung der Feststoffpartikel im absteigenden Bett (1), wobei der Aufheizbereich (6) vom Reaktionsbereich (3) im wesentlichen getrennt ist,einer in einem unteren Bereich des Aufheizbereiches (6) vorgesehenen Einrichtung (7) für die Überführung der erwärmten Feststoffpartikel aus dem Aufheizbereich (6) in den Reaktionsbereich (3), undeiner indirekten Wärmezufuhreinrichtung (8), die dem Aufheizbereich (6) zugeordnet ist und mit deren Hilfe die für die allotherme Vergasung erforderliche Wärmeenergie zuführbar ist.
- Vorrichtung nach Anspruch 10, dadurch gekennzeichnet, daß der Aufheizbereich (6) und der Reaktionsbereich (3) durch eine unterschiedliche Fluidisierung des Wirbelbettes getrennt sind, wobei die unterschiedliche Fluidisierung eine Zirkulation des Bettmaterials um eine oder mehrere im wesentlichen horizontale Achsen bewirkt.
- Vorrichtung nach Anspruch 11, dadurch gekennzeichnet, daß die im wesentlichen horizontalen Achsen ringförmig geschlossen sind.
- Vorrichtung nach Anspruch 10, dadurch gekennzeichnet, daß der Aufheizbereich (6) und der Reaktionsbereich (3) durch eine Wand (9) getrennt sind.
- Vorrichtung nach Anspruch 10, dadurch gekennzeichnet, daß der Aufheizbereich (6) und der Reaktionsbereich (3) jeweils in einem eigenen Reaktor ausgebildet sind.
- Vorrichtung nach einem der Ansprüche 13 oder 14, dadurch gekennzeichnet, daß die Einrichtung (7) für die Überführung der erwärmten Feststoffpartikel eine Wandöffnung (10) oder eine Rohrleitung ist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 15, dadurch gekennzeichnet, daß die Einrichtung (7) für die Überführung der erwärmten Feststoffpartikel ein Düsenboden (11) zur leichten Fluidisierung der Feststoffpartikel aufweist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 16, dadurch gekennzeichnet, daß die indirekte Wärmezufuhreinrichtung (8) wenigstens ein von einem Heizmedium durchströmbarer Wärmetauscher (12) ist, der im oder am Aufheizbereich (6) vorgesehen ist.
- Vorrichtung nach Anspruch 17, dadurch gekennzeichnet, daß der Wärmetauscher (12) wenigstens ein Resonanzrohr (13) aufweist, in dem das Heizmedium bei der Wärmeabgabe an den Aufheizbereich (6) pulsierend strömt.
- Vorrichtung nach Anspruch 18, dadurch gekennzeichnet, daß das Resonanzrohr (13) zur Resonanzerzeugung mit einer Brennkammer verbunden ist.
- Vorrichtung nach Anspruch 17, dadurch gekennzeichnet, daß zur Resonanzerzeugung ein akustischer Schwinger vorgesehen ist, der getrennt von einer Brennkammer angeordnet ist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 20, dadurch gekennzeichnet, daß die Einrichtung zur Erzeugung des aufsteigenden fluidisierten Wirbelschichtbettes (2) ein in einem unteren Bereich des Reaktionsbereiches (3) vorgesehener Düsenboden (15) ist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 21, dadurch gekennzeichnet, daß die Einrichtung zur Trennung der bei der Vergasung entstehenden Gase von den Feststoffpartikeln in Zyklon ist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 22, dadurch gekennzeichnet, daß die senkrechte Abströmung der im aufsteigenden Bett erzeugten Gase durch Einbauten (18,19) blockiert ist, die eine mehrfache Umlenkung der Gasströmung bedingt und die mehrfache Umlenkung zu einer weitgehenden Abtrennung der Feststoffpartikel aus dem Gasstrom führt.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 23, dadurch gekennzeichnet, daß zur Ausbildung eines Feststoffpartikelkreislaufes eine Einrichtung (16) für die Überführung der Feststoffpartikel aus dem Reaktionsbereich (3) in den Aufheizbereich (6) vorgesehen ist.
- Vorrichtung nach Ansprüche 24, dadurch gekennzeichnet, daß die Einrichtung für die Überführung (16) der Feststoffpartikel aus dem Reaktionsbereich (3) in den Aufheizbereich (6) eine Wandöffnung (17) oder eine Rohrleitung ist.
- Vorrichtung nach wenigstens einem der Ansprüche 24 und 25, dadurch gekennzeichnet, daß die Einrichtung (16) für die Überführung der Feststoffpartikel in einem oberen Bereich des Reaktionsbereiches (3) vorgesehen ist.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 21, dadurch gekennzeichnet, daß eine Zufuhreinrichtung (21) für die kohlenstoffhaltigen Stoffe in den Aufheizbereich (6) mündet.
- Vorrichtung nach wenigstens einem der Ansprüche 10 bis 27, dadurch gekennzeichnet, daß eine Zufuhreinrichtung für die kohlenstoffhaltigen Stoffe in den Reaktionsbereich (3) mündet.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE19948332 | 1999-10-07 | ||
DE19948332A DE19948332B4 (de) | 1999-10-07 | 1999-10-07 | Verfahren und Vorrichtung zum Gewinnen heizwertreicher Brennstoffe |
PCT/EP2000/009767 WO2001025371A1 (de) | 1999-10-07 | 2000-10-05 | Verfahren und vorrichtung zum gewinnen heizwertreicher brenngase |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1218471A1 EP1218471A1 (de) | 2002-07-03 |
EP1218471B1 true EP1218471B1 (de) | 2005-02-02 |
Family
ID=7924827
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP00969430A Expired - Lifetime EP1218471B1 (de) | 1999-10-07 | 2000-10-05 | Verfahren und vorrichtung zum gewinnen heizwertreicher brenngase |
Country Status (9)
Country | Link |
---|---|
US (3) | US20020148597A1 (de) |
EP (1) | EP1218471B1 (de) |
AT (1) | ATE288466T1 (de) |
AU (1) | AU7915000A (de) |
DE (2) | DE19948332B4 (de) |
DK (1) | DK1218471T3 (de) |
ES (1) | ES2235961T3 (de) |
PT (1) | PT1218471E (de) |
WO (1) | WO2001025371A1 (de) |
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AU2003266006A1 (en) * | 2002-09-10 | 2004-04-30 | Manufacturing And Technology Conversion International, Inc. | Steam reforming process and apparatus |
CA2496839A1 (en) | 2004-07-19 | 2006-01-19 | Woodland Chemical Systems Inc. | Process for producing ethanol from synthesis gas rich in carbon monoxide |
AU2006278693A1 (en) * | 2005-08-08 | 2007-02-15 | Eli Lilly And Company | Assembly for filling a container of a delivery device with a pharmaceutical |
WO2007117590A2 (en) * | 2006-04-05 | 2007-10-18 | Woodland Biofuels Inc. | System and method for converting biomass to ethanol via syngas |
US8690977B2 (en) * | 2009-06-25 | 2014-04-08 | Sustainable Waste Power Systems, Inc. | Garbage in power out (GIPO) thermal conversion process |
DE102009039920A1 (de) | 2009-09-03 | 2011-03-10 | Karl-Heinz Tetzlaff | Verfahren und Vorrichtung zur Nutzung von Sauerstoff bei der Dampfreformierung von Biomasse |
DE102009039836A1 (de) * | 2009-09-03 | 2011-03-10 | Karl-Heinz Tetzlaff | Synthesegasreaktor mit beheizter Kokswolke |
DE102009039837A1 (de) * | 2009-09-03 | 2011-03-10 | Karl-Heinz Tetzlaff | Elektrische Heizung für einen Wirbelschichtreaktor zur Herstellung von Synthesegas |
FI122040B (fi) * | 2009-11-10 | 2011-07-29 | Foster Wheeler Energia Oy | Menetelmä ja järjestely polttoaineen syöttämiseksi kiertoleijupetikattilaan |
FI20096170A (fi) * | 2009-11-10 | 2011-05-11 | Foster Wheeler Energia Oy | Menetelmä ja järjestely polttoaineen syöttämiseksi kiertoleijupetikattilaan |
FI123548B (fi) * | 2010-02-26 | 2013-06-28 | Foster Wheeler Energia Oy | Leijupetireaktorijärjestely |
DE102011015807A1 (de) | 2011-04-01 | 2012-10-04 | H S Reformer Gmbh | Steigerung der Effizienz der Beheizung allothermer Reaktoren |
US8968693B2 (en) | 2012-08-30 | 2015-03-03 | Honeywell International Inc. | Internal cyclone for fluidized bed reactor |
US9725663B2 (en) | 2013-01-22 | 2017-08-08 | Themochem Recovery International, Inc. | Integrated two-stage thermochemical heat pipe reactor having a partitioned vessel |
ITUA20162165A1 (it) * | 2016-04-04 | 2016-07-04 | Enrico Bocci | Internal Circulating Dual Bubbling Fluidised Bed Gasifier |
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US4515659A (en) * | 1982-09-30 | 1985-05-07 | Ford Motor Company | Pyrolytic conversion of plastic and rubber waste to hydrocarbons with basic salt catalysts |
DE3320049A1 (de) * | 1983-06-03 | 1984-12-06 | Inter Power Technologie GmbH, 6600 Saarbrücken | Verfahren zum betreiben einer wirbelschichtfeuerung |
SE460146B (sv) * | 1986-08-14 | 1989-09-11 | Goetaverken Energy Syst Ab | Anordning vid foerbraenningsanlaeggning med cirkulerande fluidbaedd |
DE3635215A1 (de) * | 1986-10-16 | 1988-04-28 | Bergwerksverband Gmbh | Verfahren zur allothermen kohlevergasung und wirbelbett-gasgenerator zur durchfuehrung des verfahrens |
AT401419B (de) * | 1987-07-21 | 1996-09-25 | Sgp Va Energie Umwelt | Wirbelschichtverfahren zur vergasung und verbrennung von brennstoffen sowie vorrichtung zu seiner durchführung |
EP0324957A1 (de) * | 1987-12-22 | 1989-07-26 | Waagner-Biro Aktiengesellschaft | Verfahren und Einrichtung zur thermischen Herstellung von Chemierohstoffen |
DK633488D0 (da) * | 1988-11-11 | 1988-11-11 | Risoe Forskningscenter | Reaktor |
US5059404A (en) * | 1989-02-14 | 1991-10-22 | Manufacturing And Technology Conversion International, Inc. | Indirectly heated thermochemical reactor apparatus and processes |
TW245651B (en) * | 1994-02-24 | 1995-04-21 | Babcock & Wilcox Co | Black liquor gasifier |
DE19736867C2 (de) * | 1997-08-25 | 2003-01-16 | Montan Tech Gmbh | Verfahren zur allothermen Vergasung von organischen Stoffen und Stoffgemischen |
EP1187892B1 (de) * | 1999-06-09 | 2004-12-29 | Technische Universität München Lehrstuhl für Thermische Kraftanlagen | Vorrichtung zur vergasung kohlenstoffhaltiger einsatzstoffe |
-
1999
- 1999-10-07 DE DE19948332A patent/DE19948332B4/de not_active Expired - Fee Related
-
2000
- 2000-10-05 DK DK00969430T patent/DK1218471T3/da active
- 2000-10-05 AT AT00969430T patent/ATE288466T1/de active
- 2000-10-05 PT PT00969430T patent/PT1218471E/pt unknown
- 2000-10-05 DE DE50009434T patent/DE50009434D1/de not_active Expired - Lifetime
- 2000-10-05 ES ES00969430T patent/ES2235961T3/es not_active Expired - Lifetime
- 2000-10-05 EP EP00969430A patent/EP1218471B1/de not_active Expired - Lifetime
- 2000-10-05 WO PCT/EP2000/009767 patent/WO2001025371A1/de active Application Filing
- 2000-10-05 AU AU79150/00A patent/AU7915000A/en not_active Abandoned
-
2002
- 2002-04-05 US US10/116,038 patent/US20020148597A1/en not_active Abandoned
-
2005
- 2005-02-18 US US11/060,322 patent/US7094264B2/en not_active Expired - Fee Related
-
2006
- 2006-07-07 US US11/482,626 patent/US7507266B2/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
PT1218471E (pt) | 2005-05-31 |
ATE288466T1 (de) | 2005-02-15 |
EP1218471A1 (de) | 2002-07-03 |
US7094264B2 (en) | 2006-08-22 |
AU7915000A (en) | 2001-05-10 |
DE50009434D1 (de) | 2005-03-10 |
ES2235961T3 (es) | 2005-07-16 |
US7507266B2 (en) | 2009-03-24 |
US20020148597A1 (en) | 2002-10-17 |
DE19948332B4 (de) | 2005-09-22 |
US20050166457A1 (en) | 2005-08-04 |
WO2001025371A1 (de) | 2001-04-12 |
DE19948332A1 (de) | 2001-05-03 |
US20060265955A1 (en) | 2006-11-30 |
DK1218471T3 (da) | 2005-03-14 |
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