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WO2003106594A1 - Procede de gazeification de biomasse et installation correspondante - Google Patents

Procede de gazeification de biomasse et installation correspondante Download PDF

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Publication number
WO2003106594A1
WO2003106594A1 PCT/DE2003/002027 DE0302027W WO03106594A1 WO 2003106594 A1 WO2003106594 A1 WO 2003106594A1 DE 0302027 W DE0302027 W DE 0302027W WO 03106594 A1 WO03106594 A1 WO 03106594A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
combustion chamber
gas
gasification reactor
biomass
Prior art date
Application number
PCT/DE2003/002027
Other languages
German (de)
English (en)
Inventor
Ragnar Warnecke
Helmut Lessing
Original Assignee
Clausthaler Umwelttechnikinstitut Gmbh (Cutec-Institut)
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 Clausthaler Umwelttechnikinstitut Gmbh (Cutec-Institut) filed Critical Clausthaler Umwelttechnikinstitut Gmbh (Cutec-Institut)
Priority to AU2003250263A priority Critical patent/AU2003250263A1/en
Priority to DE10393350T priority patent/DE10393350D2/de
Publication of WO2003106594A1 publication Critical patent/WO2003106594A1/fr

Links

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
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • 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
    • C10J2300/0903—Feed preparation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0983—Additives
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/1215—Heating the gasifier using synthesis gas as fuel
    • 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
    • C10J2300/1223—Heating the gasifier by burners
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • C10J2300/1823—Recycle loops, e.g. gas, solids, heating medium, water for synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1838—Autothermal gasification by injection of oxygen or steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam only
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to a method for the gasification of biomass in a gasification reactor by thermo-chemical decomposition of hydrocarbons in a water vapor atmosphere.
  • the invention further relates to a plant for the gasification of biomass with a gasification reactor which is designed for the thermo-chemical decomposition of hydrocarbons in a water vapor atmosphere, and with a combustion chamber for the exothermic combustion of substances, preferably of oxidizing gases, but possibly also of liquid or solid Substances with atmospheric oxygen.
  • the aim of the synthesis of biomass is aliphatic
  • biological processes for the implementation of biomass such as. B. methane fermentation or alcoholic fermentation, known where primarily methane and secondary methanol or ethanol are produced.
  • the biological processes can only be used for selected biomass compositions and are restricted to the special composition of the biomass.
  • the speed of the biological processes is relatively low even in the optimal temperature range, so that large-scale application of the biological processes is hardly possible.
  • thermo-chemical thermolysis processes are known, but the use of the products of such thermolysis (pyrolysis) is severely restricted, since the thermolysis oil produced has a very heterogeneous composition and is not directly suitable for refining.
  • pyrolysis thermolysis
  • thermolysis oil produced has a very heterogeneous composition and is not directly suitable for refining.
  • flash pyrolysis inorganic constituents in the thermolysis oil make further treatment more difficult, the purification of the thermolysis oil present in the liquid phase being more difficult than the purification of a gas phase.
  • thermo-chemical reactolysis processes are known with which gaseous products are produced.
  • accompanying substances are present in the reactolysis gases which prevent direct synthesis.
  • cleaning processes are known for almost all accompanying substances.
  • reactolysis means a direct thermo-chemical decomposition of the biomass by gasification of the biomass in an atmosphere containing water vapor.
  • thermo-chemical thermolysis processes have so far also been used as a preliminary stage for reactolysis processes.
  • n (CO + 2 H 2 ) n H 2 O + (CH (2) ) n alKW
  • the synthesis gas can be generated from biomass by thermo-chemical conversion.
  • a direct thermochemical decomposition of the biomass with water vapor can be used according to the so-called reactolysis process in order to generate the synthesis gas as a mixture of carbon monoxide CO and hydrogen H 2 .
  • the following relationship applies:
  • thermo-chemical decomposition requires thermal support through an exothermic reaction, which can take place through internal combustion with oxygen or via an external energy supply.
  • a disadvantage of internal combustion is that the proportions of the gases required for the synthesis (carbon monoxide CO and hydrogen H 2 ) are shifted absolutely and in a relatively unfavorable manner with regard to their stoichiometric ratio.
  • carbon atoms in the biomass leave the balance as carbon dioxide CO 2 and thus reduce the amount of hydrocarbons that can be synthesized.
  • Fixed bed gasifiers entrained flow gasifiers and fluidized bed gasifiers are known for the gasification of biomass in the reactolysis process.
  • Fixed bed counterflow gasifiers have a very high tar content in the product gas, which makes aftertreatment extremely difficult.
  • fixed-bed DC gasifiers only produce small amounts of tar.
  • Fixed bed gasifiers have the disadvantage that stable beds have to be formed, so that the biomass has to be reliably pelleted.
  • preconditioning of biomass in lean gas, coke and oil is first carried out with the aid of pre-gasification. This is followed by gasification in the entrained flow at high temperatures in the upper region of the reactor using oxygen. The gases are then reduced in the same reactor at about 650 to 800 ° C. in the lower region of the reactor using steam.
  • the entrained flow gasifiers are relatively expensive due to the two reactors required and have a limited efficiency.
  • biomass is gasified in a fluidized bed system with air as the gasifying agent.
  • the fluidized bed gasifiers have a gasification zone which is swirled with steam and a combustion zone which is swirled with air. Charcoal is burned in the combustion zone, generating the thermal energy required for gasification.
  • the circulating bed material transports the heat from the combustion zone to
  • Gasification zone The problem is to prevent the exhaust gases from the combustion zone from mixing with the product gas and contaminating it, if possible.
  • Another embodiment of fluidized bed gasifiers use water vapor as a gasifying agent in order to carry out the so-called Battelle process or FICFB process (Fast Internally Cirulating Fluidized Bed).
  • Battelle process FICFB process
  • FICFB process Fast Internally Cirulating Fluidized Bed
  • This procedure has the advantage that it is possible to produce product gases with high purity in an energetically economical manner with relatively little investment in the plant.
  • the exothermic process of combustion of the oxidation gases is preferably maintained by product gases from the gasification reactor, which are introduced into the combustion chamber as oxidation gases.
  • the process can first be initiated by externally supplied oxidation gases and then the proportion of product gases in the oxidation gases can be increased.
  • a mixture of air, natural gas and product gas as the oxidizing gas is preferably passed into the combustion chamber and burned there.
  • the reactolysis process in the gasification reactor is preferably carried out in a hydrogen-containing atmosphere which has a gas mixture of oxygen, water vapor and natural gas as the reactolysis gas.
  • the biomass should be conditioned before gasification
  • Biomass can be made, for example, by mechanical comminution. The energy balance of the process can thus be improved.
  • the product gases generated by gasification of the biomass are then preferably cleaned and synthesized, for example, using the Fischer-Tropsch synthesis process.
  • the gasification of the biomass is preferably controlled by supplying oxygen. It is also particularly advantageous if the biomass is gasified in a fluidized bed with additives such as sand, aluminum oxide and / or dolomite or the like.
  • additives such as sand, aluminum oxide and / or dolomite or the like.
  • the residual solids resulting from the gasification can be removed from the gasification reactor by means of an outlet. After the residual solids have been sieved off, the sieved-out additives, in particular sand, can be fed back to the gasification reactor as additives.
  • the object is further achieved according to the invention by the generic system in that the gasification reactor is arranged gas-tightly separated from the combustion chamber in such a way that thermal energy is conducted from the combustion chamber into the gasification reactor and the combustion gases from the combustion chamber are separated from the product gases generated during the gasification of the biomass be derived.
  • Figure 1 - sectional view of a plant according to the invention for gasification of biomass.
  • FIG. 1 shows a plant 1 according to the invention for the gasification of biomass, which essentially has a gasification reactor 2 for the thermo-chemical decomposition of hydrocarbons in a water vapor atmosphere and a combustion chamber 3 separated from it in a gas-tight manner for the combustion of oxidation gases G.
  • the exothermic process of the combustion of oxidation gases G in the combustion chamber 3 is thus spatially separated from the reactolysis, i.e. H. thermo-chemical decomposition, in
  • Gasification reactor 2 carried out gas-tight.
  • the endothermic process of the reactolysis in the gasification reactor 2 is maintained by the exothermic process in the combustion chamber 3.
  • the gasification reactor 2 is accommodated in the combustion chamber 3, the outer wall of the gasification reactor 2 forming the inner wall of the combustion chamber 3.
  • the heat exchange from the combustion chamber 3 to the gasification reactor 2 thus takes place via the outer wall 4 of the gasification reactor 2. In this way, a complete separation of the product gases P generated in the gasification reactor 2 from the reductive one is achieved
  • the exothermic process in the combustion chamber 3 is maintained by the oxidizing gases G, which are fed into the combustion chamber 3 via a supply line 5 in the upper region.
  • the combustion process is obtained by atmospheric oxygen L and natural gas E. Later, the proportion of product gas P is increased and in particular the proportion of natural gas E is reduced.
  • the combustion gas A resulting from the combustion in the combustion chamber 3 is discharged through an exhaust gas outlet 9 in the lower region of the combustion chamber 3.
  • the gasification reactor 2 accommodated in the combustion chamber 3 has in the lower region a fluidized bed grate 10 inclined relative to the horizontal plane with gas passage openings. At least one feed line 11 for reactor lysis gases R opens below the fluidized bed grate to maintain the thermo-chemical
  • the reactor gases R are preferably a mixture of oxygen O, hydrogen H 2 and natural gas E.
  • the biomass B is preferably mixed with additives Z, such as. B. sand, aluminum oxide, dolomite etc. passed through a hopper 1 2 with feed into the gasification reactor 2. Over a
  • the gasification reactor 2 is operated at temperatures of approximately 500 to 900 ° C. in a reducing hydrogen atmosphere largely in the absence of air, so that thermo-chemical decomposition of the hydrocarbons is ensured.
  • the gas temperature in the outer combustion chamber 3 is approximately 800 to 1200 ° C., the combustion taking place in an oxidative atmosphere. It is essential to the invention that those generated during the combustion Exhaust gases A are derived separately from the product gases P by the combustion chamber 3 being gas-tight from the gasification reactor 2.
  • the endothermic process of gasification is maintained here by heat exchange from the combustion reactor 3 via the outer wall 4 into the gasification reactor 2.
  • the residual solids resulting from the gasification are discharged via a discharge into a sieve 16.
  • Aggregates Z, in particular sand, can be sieved out and returned to the gasification process via the filling funnel 1 2.
  • the remaining substances 1 7, however, are discarded.
  • the gasification process is preferably controlled initially autothermally with the addition of oxygen.
  • the biomass B should also be gasified in such a way that an almost ideal product gas mixture P of carbon monoxide CO and hydrogen H 2 is obtained in a molar ratio of approximately 1 to 2.
  • the generated product gases P are further processed in the centrifugal separator 14 after dedusting. This postprocessing process, not shown, can cool the product gases 9 via heat exchangers and downstream
  • an alternately switchable tar catalyst can be provided as a safety level if, for. B. the tar content increases inadmissibly during load changes. Possibly separated tar is burned off oxidatively by means of this alternating circuit. Removal of sulfur H 2 S and halides, e.g. B. HCI, with laundry can join. In addition, a shift stage and carbon dioxide washing can be provided.
  • the desired boiling cuts can be obtained from the resulting aliphatic hydrocarbons, such as in conventional gasoline and diesel production, using catalysts.
  • the primary oil produced during the synthesis can later be refined, the fuels being obtained from the corresponding boiling cuts and blended.

Landscapes

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

Abstract

L'invention concerne un procédé de gazéification de biomasse (B) dans un réacteur de gazéification (2) par décomposition thermochimique d'hydrocarbures dans une atmosphère de vapeur d'eau, qui comprend les étapes suivantes : brûler des substances dans une chambre de combustion (3) séparée de manière étanche aux gaz du réacteur de gazéification (2) ; acheminer l'énergie thermique dégagée de la chambre de combustion (3) jusque dans le réacteur de gazéification (2), et évacuer les gaz de combustion (A) provenant de la chambre de combustion (3) séparément des gaz-produits (P) obtenus lors de la gazéification de la biomasse (B).
PCT/DE2003/002027 2002-06-17 2003-06-17 Procede de gazeification de biomasse et installation correspondante WO2003106594A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
AU2003250263A AU2003250263A1 (en) 2002-06-17 2003-06-17 Method for the gasification of biomass and corresponding plant
DE10393350T DE10393350D2 (de) 2002-06-17 2003-06-17 Verfahren zur Vergasung von Biomasse und Anlage hierzu

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE10227074A DE10227074A1 (de) 2002-06-17 2002-06-17 Verfahren zur Vergasung von Biomasse und Anlage hierzu
DE10227074.0 2002-06-17

Publications (1)

Publication Number Publication Date
WO2003106594A1 true WO2003106594A1 (fr) 2003-12-24

Family

ID=29723216

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/DE2003/002027 WO2003106594A1 (fr) 2002-06-17 2003-06-17 Procede de gazeification de biomasse et installation correspondante

Country Status (3)

Country Link
AU (1) AU2003250263A1 (fr)
DE (2) DE10227074A1 (fr)
WO (1) WO2003106594A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3078727A1 (fr) * 2015-04-10 2016-10-12 Meva Energy AB Cyclone gazéificateur
WO2019033689A1 (fr) * 2017-08-14 2019-02-21 张达积 Générateur d'hydrogène par décomposition de vapeur de biomasse

Families Citing this family (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004032830A1 (de) * 2004-07-06 2006-02-23 Rolf Schmitt Verfahren zur Erzeugung von wasserstoffreichen Synthesegas aus biogenen Stoffen und sonstigen kohlenstoffhaltigen Verbindungen mittels Wasserdampfvergasung (Dampfreformierung) in einem indirekt beheizten Wirbelschichtreaktor bei gleichzeitiger partieller Oxidation der Einsatzstoffe durch geregelte Einbringung von Sauerstoff in den Wirbelschichtreaktor (Hybridverfahren)
DE102007004294A1 (de) * 2007-01-23 2008-07-24 Spot Spirit Of Technology Ag Verfahren und Vorrichtung zur Herstellung von Energie, Treibstoffen oder chemischen Rohstoffen unter Einsatz von CO2-neutralen biogenen Einsatzstoffen
DE102007050566A1 (de) 2007-10-23 2009-05-07 Stevanović, Dragan, Dr. Verfahren und Vorrichtung zur Vergasung von kohlenstoffhaltigen Rohstoffen
DE102008014297A1 (de) 2007-11-16 2009-05-20 Krones Ag Verfahren und Vorrichtung zur Umwandlung kohlenstoffhaltiger Rohstoffe
DE102008049728A1 (de) * 2008-09-30 2010-04-29 Highterm Research Gmbh Verfahren zum Anfahren eines Wirbelschichtreaktors und Wirbelschichtreaktor zum Ausführen des Verfahrens
DE102009011356A1 (de) 2009-03-05 2010-09-09 Krones Ag Verfahren und Vorrichtung zum Herstellen eines kohlenstoffhaltigen Brennstoffs
DE102009038323A1 (de) 2009-08-21 2011-02-24 Krones Ag Verfahren und Vorrichtung zur Verwertung von Biomasse
DE102009038322A1 (de) 2009-08-21 2011-02-24 Krones Ag Verfahren und Vorrichtung zur Umwandlung thermischer Energie aus Biomasse in mechanische Arbeit
DE102011075438A1 (de) 2011-05-06 2012-11-08 Bilfinger Berger Industrial Services Gmbh Verfahren und Vorrichtung zur Erzeugung von Synthesegas aus kohlestoffhaltigen Edukten durch Vergasung
DE102021134191A1 (de) 2021-12-22 2023-06-22 BHYO GmbH Verfahren und Anlageverbund zur Erzeugung von Synthesegas

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001012754A1 (fr) * 1999-08-19 2001-02-22 Manufacturing And Technology Conversion International, Inc. Turbine a gaz avec systeme de reformage a la vapeur chauffe indirectement

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19900116C2 (de) * 1999-01-05 2002-02-14 Univ Muenchen Tech Vorrichtung zum Erzeugen von Brenngas durch allotherme Vergasung von Biomasse

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2001012754A1 (fr) * 1999-08-19 2001-02-22 Manufacturing And Technology Conversion International, Inc. Turbine a gaz avec systeme de reformage a la vapeur chauffe indirectement

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3078727A1 (fr) * 2015-04-10 2016-10-12 Meva Energy AB Cyclone gazéificateur
WO2019033689A1 (fr) * 2017-08-14 2019-02-21 张达积 Générateur d'hydrogène par décomposition de vapeur de biomasse

Also Published As

Publication number Publication date
DE10393350D2 (de) 2005-06-02
DE10227074A1 (de) 2004-01-15
AU2003250263A1 (en) 2003-12-31

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