EP0523815A1 - Verfahren zum Herstellen von Synthese- oder Brenngasen aus festen oder pastösen Rest- und Abfallstoffen oder minderwertigen Brennstoffen in einem Vergasungsreaktor - Google Patents

Verfahren zum Herstellen von Synthese- oder Brenngasen aus festen oder pastösen Rest- und Abfallstoffen oder minderwertigen Brennstoffen in einem Vergasungsreaktor Download PDF

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Publication number
EP0523815A1
EP0523815A1 EP92202501A EP92202501A EP0523815A1 EP 0523815 A1 EP0523815 A1 EP 0523815A1 EP 92202501 A EP92202501 A EP 92202501A EP 92202501 A EP92202501 A EP 92202501A EP 0523815 A1 EP0523815 A1 EP 0523815A1
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EP
European Patent Office
Prior art keywords
gasification reactor
gas
gasification
pyrolysis treatment
solid
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
EP92202501A
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German (de)
English (en)
French (fr)
Inventor
Karl-Heinz Redepenning
H. Peter Wenning
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.)
Veba Oel Technologie und Automatisierung GmbH
John Brown Deutsche Engineering GmbH
Original Assignee
Veba Oel Technologie und Automatisierung GmbH
John Brown Deutsche Engineering GmbH
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
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Application filed by Veba Oel Technologie und Automatisierung GmbH, John Brown Deutsche Engineering GmbH filed Critical Veba Oel Technologie und Automatisierung GmbH
Publication of EP0523815A1 publication Critical patent/EP0523815A1/de
Pending 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/64—Processes with decomposition of the distillation products
    • C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
    • C10J2300/1606—Combustion processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/164—Integration of gasification processes with another plant or parts within the plant with conversion of synthesis gas
    • C10J2300/1643—Conversion of synthesis gas to energy
    • 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

Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • Inferior fuels such as wet brown coal or hard coal with a high tar content, old iron, etc.
  • the product gas can be free or almost free of impurities which reduce the calorific value and restrict further use and pollute the environment.
  • a shaft-shaped gasification reactor has been developed, the special feature of which is that the bulk material bed in the primary gas chamber is constructed in two layers.
  • a first layer of the bulk bed consists of a relatively high quality coke.
  • the second layer of the bulk bed is stored as a relatively thin layer on the first bulk layer and is formed by the inferior fuel.
  • the free bulk surface of the second bulk material layer faces the primary gas burner in the primary gas chamber.
  • a fuel, oxygen or air and possibly water vapor are applied to the primary gas burner and provide the sensible heat required for the endothermic gasification process.
  • the primary gas burner z. B. used oils and a pasty residue from a paper mill.
  • the primary gas generated by the combustion in the burner occurs at a temperature of 1500 to 1800 ° C.
  • the cargo to be gasified low-quality fuel, e.g. a mixture of used tires and deinking sludge
  • the raw gas has z. B. 1,864 ° C and then flows through the second bed of coke and leaves it as a finished product gas at the top of the shaft gasifier.
  • the primary gasification is set either via the ratio of oxygen to carbon carrier in the burner, or via the total amount of primary gasification substances or - if pure oxygen is introduced via the burner instead of air - via the ratio of oxygen to water vapor (EP 0 194 252 B1).
  • the object of the invention is to ensure as uniform a product gas quality as possible in the gasification of inferior and / or difficult to handle feedstocks and / or residues and waste materials containing organic constituents, in particular in the gasification of the shredder light fraction during motor vehicle recycling.
  • Gasification reactors operating according to the preferred entrained flow principle are sufficiently known and therefore do not require any special description at this point; reference is made, for example, to DE-C2 27 21 047 and EP-B1-0 011 151. While the use of a gasification reactor working according to the entrained flow principle (also known as the fly dust principle) is preferred according to the invention, alternatively there is also a gasification reactor working according to the fluidized bed principle, as described u. a. is addressed in EP-B1-0 011 151, for use according to the invention.
  • entrained flow principle also known as the fly dust principle
  • the solids obtained after the pyrolysis treatment stage can preferably be used can be used directly in the shaft gasifier without a special adjustment of the grain size range and without great handling problems when charging the solid fraction; A relatively uniform product gas quality is also ensured with this driving style.
  • the above-mentioned shaft carburetors (EP-B1-0 194 252) are basically suitable for such an application.
  • Such a shaft gasifier has a shaft-shaped container for receiving the solid cargo to be obtained behind the pyrolysis treatment stage, forming a traveling layer with a passage for the cargo at the lower end of the container.
  • a primary gas chamber Connected to the passage is a primary gas chamber arranged under the container and fired by a primary gas burner, in which a bed surface facing the primary gas burner of a bed of bulk material formed by the solid cargo below the passage is formed, the product gas and the slag from the gasification process be deducted in a suitable manner.
  • a shaft gasifier it is advantageous to supply the fraction which is gaseous behind the pyrolysis treatment stage and which is gaseous under operating conditions of the pyrolysis treatment to the primary gas burner in order to supply the endothermic gasification process with heat of gasification.
  • the gas fraction and, if appropriate, further fuels are preferably fed in by forming an entrained flow in the primary gas chamber.
  • the gas fraction obtained after the pyrolysis treatment stage is preferably first subjected to a condensation step.
  • the gas fraction obtained after the condensation stage is then further used in the synthetic and / or fuel gas production process according to the invention.
  • this gas fraction is the gasification reactor or the pyrolysis treatment stage for introducing heat for the endothermic pyrolysis or gasification step or added to the product gas obtained behind the gasification reactor as part of the combustion or synthesis gas.
  • the liquid fraction obtained behind the condensation stage can possibly be used in another process, but is preferably fed to the gasification reactor for gasification and / or for the introduction of heat for the endothermic gasification process.
  • the solid fraction obtained after the pyrolysis treatment stage and the liquid fraction obtained after the condensation stage are mixed and fed to the gasification reactor together, depending on the consistency of the mixture, preferably a pump or a screw machine being used. Suitable funding bodies and procedures for this are known from DE-C2-27 21 047 and EP-B1-0 011 151 as examples.
  • feedstocks to be processed according to the invention are either essentially solid or pasty, with pasty not only solid / liquid mixtures but also more or less thickened Liquids are to be understood, in principle liquid feedstocks, ie residues and waste materials and / or inferior fuels containing organic constituents, can also be used or also used for the production process of synthetic and / or fuel gases according to the invention. As a rule, however, liquid feedstocks of the aforementioned type can also be converted into synthesis and / or fuel gases in other processes.
  • gasifier can also be used in accordance with the invention in addition to those which, as is preferred, work on the entrained flow principle or are designed as shaft gasifiers.
  • gasifiers An example of this are the fluidized bed gasifiers already mentioned.
  • the gasification is generally carried out under a pressure of preferably 10 to 100 bar. Basically, higher gasification pressures are possible.
  • the gasification can also be carried out at atmospheric pressure or in a slightly negative pressure (if suction fans are used).
  • the invention is therefore based on the basic idea of producing synthetic and / or fuel gases from residual and waste materials and / or inferior fuels (feedstock) containing organic constituents with oxygen or oxygen-containing gases and possibly water vapor, first by subjecting the feedstock to a thermal pretreatment Supply of heat and essentially avoiding the burning of constituents of the feed (pyrolysis treatment) into a gaseous and a solid fraction under operating conditions to separate the solid fraction by producing the synthesis and / or fuel gas in the To gasify the gasification reactor and to process the gas fraction at least partially in the manufacturing process for introducing process heat and / or for producing additional amounts of synthesis gas and / or fuel gas.
  • pyrolysis plants are generally known for this; Because of their knowledge of their structure and their process conditions, these need not be explained in detail here.
  • Typical examples of pyrolysis plants which can be used according to the invention and other inferior fuels are e.g. B. the pyrolysis of waste wood in the fluidized bed reactor or the pyrolysis of chemical production residues in the rotary tube reactor.
  • FIG. 1 applies in principle to every type of gasification reactor, but is explained below primarily in connection with the preferred use of an entrained-flow gasification reactor. Alternative procedures are shown in dashed lines. Process steps that are preferably used are additionally outlined with a dashed line.
  • a residual or waste material and / or inferior fuel containing organic components hereinafter referred to as feed
  • a pyrolysis treatment stage 101 such as e.g. an indirectly heated rotary kiln (drum wall temperature up to 900 ° C).
  • the feed material is pretreated, largely without oxygen, with the addition of heat and essentially avoiding the burning of constituents of the feed material at temperatures between approximately 300 and 650 ° C.
  • extraneous gas, product gas obtained behind the gasification reactor 102 and / or behind a condensation stage 103 downstream of the pyrolysis stage, preferably occurring in a pyrolysis gas purification stage 104 can be used.
  • the intermediate product obtained from the feed material in the pyrolysis treatment stage 101 is separated as steam (Gas fraction) and coke (solid fraction) removed.
  • the solid fraction is adjusted, if necessary after setting the grain size range in a grinding, sieving and / or screening stage 105, to the level which is compatible with the respective gasification reactor type (gasification reactor 102) and fed to the gasification reactor 102, for example pneumatically.
  • Recyclables contained in the solid fraction e.g. B. metals can in a separation stage 106, z. B. a screening device, be removed before the solid fraction is fed to the gasification reactor 102.
  • the gas fraction obtained behind the pyrolysis treatment stage 101 is either fed as steam to the gasification reactor for gasification and / or introduction of heat of reaction or first passed through a condensation stage 103.
  • the residual gas deposited therein, which occurs under the condensation conditions, is fed to the pyrolysis treatment stage for introducing process heat either, preferably after passing through a pyrolysis gas purification stage 104.
  • the pyralysis gas can be fed to the gasification reactor 102 or the product gas stream occurring behind it to introduce gasification heat. In these cases, a pyrolysis gas cleaning stage may not be necessary.
  • the oil (liquid fraction) obtained after the condensation stage 103 is recycled in other processes or, as is preferred, introduced into the gasification reactor 102. Especially when this oil is to be gasified together with the solid fraction from the pyrolysis treatment stage 101, the two fractions can first be combined and fed to the gasification reactor 102 by means of a pump or screw machine 107.
  • Inorganic components occur behind the gasification reactor, which no longer have to be deposited, but instead can be used as recyclables.
  • the product gas obtained behind the gasification reactor 102 will generally be cleaned in a gas cleaning stage 108.
  • the constituents removed from the product gas can be fed to the gasification reactor 102 at least as a partial stream, so that they are divided there into product gas or inorganic constituents.
  • enriched harmful gas components such as sulfur, salts and heavy metals, can be used.
  • the product gas accumulating behind the gas purification stage 108 can, as is preferred, be fired in a power plant 109, which may be already present, or, if appropriate partially, in the pyrolysis treatment stage 101 or used as synthesis gas or other fuel gas.
  • the shaft carburetor 100 shown in detail in FIG. 2 is known from DE 29 20 922 C3.
  • the pressure vessel 1 has a vertical upper section and a laterally angled section.
  • the solid charge is fed through a lock 4, which after each cycle with an inert gas, for. B. steam is flushed through a line 5.
  • the lumpy, solid charge passes into a basket 3, which is accommodated in the pressure vessel 1, from cooling water pipes and forms a bed 11 in the latter with a pouring cone having an upper free surface 12.
  • the lines of the basket 3 are supplied via a lower ring distributor 31, to which down pipes 30, which lie in the space between the basket 3 and the pressure vessel 1, lead from an upper ring distributor 29, to which a cooling water supply line 7 is connected.
  • the basket 3 has in the lower third an inward projection 20 which forms the upper boundary of an underlying primary gas chamber 21. Because of the narrowing (passage) present in the basket 3, an inclined embankment-like free bed surface 13 is inevitably formed at the lower end of the bed 11, which bounds the primary gas chamber 21 on this side.
  • the bed 11 stands on a slag pan 22 also formed by coolant lines on the lower part of the basket 3.
  • the inside of the basket 3 including the slag tray 20 is provided with a refractory ramming compound 32.
  • the embankment forming the lower free fill surface 13 of the fill 11 is at a distance from one of the overflow weir 16 formed from the corner of the slag tray 22 facing away from the fill 11.
  • the liquid slag with a free surface can collect between the lower free bed surface 13 and the overflow weir 16 in a slag bath 14 taken up by the slag pan 22.
  • the outer part of the primary gas chamber 21 is delimited by the refractory mass 32 of the basket 3.
  • a primary gas burner 2 Directly opposite the overflow weir 16 in the wall of the pressure vessel 1 is a primary gas burner 2, to which the gas fraction from the thermal pretreatment of the inferior fuel, oxygen or oxygen-containing gas and possibly steam are fed.
  • the primary gas jet 15 formed by the primary gas burner 2 is inclined downwards in the direction of the lower free bed surface 13 and the free surface of the slag bath 14 directed. In this way, intensive gasification is achieved at the lower free bed surface 13 and also the constituents containing carbon floating on the slag bath 14 and a blockage of the overflow weir 16 is prevented, because the primary gas jet 15 is directed against the slag flow flowing to the overflow weir 16.
  • the feed material referred to as "waste” is first fed to a plant for thermal pretreatment designated "pyrolysis".
  • pyrolysis This takes place with the addition of heat and essentially avoiding the burning of constituents of the starting material (low-quality fuel), the process being carried out in a manner known per se in such a way that a gas and a solid fraction are formed, which are separated from one another and in FIG. 2 on the one hand as “pyrolysis gas” (gas fraction) and on the other hand as “pyrolysis coke and valuable materials” (solid fraction).
  • pyrolysis gas gas fraction
  • solid fraction pyrolysis coke and valuable materials
  • any liquid fraction that occurs can be a component of the “solid fraction” and / or “gas fraction”.
  • the following process conditions are set: Temperatures approx. 300 - 650 ° C and a degassing pressure of approx. 0.9 X 105 to1.2 X 105 Pascal.
  • the "solid fraction” can be separated into its components “pyrolysis coke” and “recyclable materials” in a separating apparatus, such as an air classifier, a sieve or other.
  • a separating apparatus such as an air classifier, a sieve or other.
  • the "pyrolysis coke” is then fed to the shaft gasifier 100 via the lock 4.
  • the "pyrolysis gas” (gas fraction) obtained in the thermal pretreatment is fed to the primary gas burner 2.
  • the product gas is obtained after flowing through the bed 11 at the gas outlet 6 and from there after further cleaning of gas and solid impurities (H2S, HCL, dust) with CHP designated cogeneration plant as a gaseous fuel for machines such.
  • CHP gas and solid impurities
  • the pyrolysis drum can be heated either directly by burning pyrolysis gas or indirectly by removing flue gas from the CHP.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Gasification And Melting Of Waste (AREA)
EP92202501A 1991-07-15 1992-07-15 Verfahren zum Herstellen von Synthese- oder Brenngasen aus festen oder pastösen Rest- und Abfallstoffen oder minderwertigen Brennstoffen in einem Vergasungsreaktor Pending EP0523815A1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19914123406 DE4123406C2 (de) 1991-07-15 1991-07-15 Verfahren zum Vergasen von minderwertigen festen Brennstoffen in einem schachtförmigen Vergasungsreaktor
DE4123406 1991-07-15

Publications (1)

Publication Number Publication Date
EP0523815A1 true EP0523815A1 (de) 1993-01-20

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ID=6436185

Family Applications (2)

Application Number Title Priority Date Filing Date
EP92916028A Expired - Lifetime EP0600923B1 (de) 1991-07-15 1992-07-15 Verfahren zum herstellen von synthese- oder brenngasen aus festen oder pastösen rest- und abfallstoffen oder minderwertigen brennstoffen in einem vergasungsreaktor
EP92202501A Pending EP0523815A1 (de) 1991-07-15 1992-07-15 Verfahren zum Herstellen von Synthese- oder Brenngasen aus festen oder pastösen Rest- und Abfallstoffen oder minderwertigen Brennstoffen in einem Vergasungsreaktor

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP92916028A Expired - Lifetime EP0600923B1 (de) 1991-07-15 1992-07-15 Verfahren zum herstellen von synthese- oder brenngasen aus festen oder pastösen rest- und abfallstoffen oder minderwertigen brennstoffen in einem vergasungsreaktor

Country Status (7)

Country Link
EP (2) EP0600923B1 (fi)
JP (1) JP3203580B2 (fi)
AU (1) AU2344492A (fi)
CA (1) CA2113636A1 (fi)
DE (2) DE4123406C2 (fi)
FI (1) FI106314B (fi)
WO (1) WO1993002162A1 (fi)

Cited By (13)

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WO1994021751A1 (de) * 1993-03-17 1994-09-29 Siemens Aktiengesellschaft Verfahren und einrichtung zum entsorgen von abfall
WO1994029410A1 (en) * 1993-06-04 1994-12-22 Biokat Corporation Gasification of low calorific value solid fuels to produce electric energy
WO1995021903A1 (de) * 1994-02-15 1995-08-17 Crg Kohlenstoffrecycling Ges.Mbh Verfahren zur erzeugung von brenngas
DE19608093C2 (de) * 1996-03-02 2000-08-10 Krc Umwelttechnik Gmbh Verfahren zur Verwertung von Rest- und Abfallstoffen sowie heizwertarmen Brennstoffen in einem Zementofen
DE10010358A1 (de) * 2000-03-07 2001-09-27 Bsbg Bremer Sonderabfall Berat Verfahren und Vorrichtung zum Vergasen von brennbarem Material
WO2003033624A1 (de) * 2001-10-16 2003-04-24 Forschungszentrum Karlsruhe Gmbh Verfahren zur pyrolyse und vergasung von biomasse
EP1510567A1 (fr) * 2003-08-27 2005-03-02 Institut Francais Du Petrole Procédé et installation de production à haut rendement d'un gaz de synthèse dépollué à partir d'une charge riche en matière organique.
EP1520900A1 (de) * 2003-10-01 2005-04-06 Forschungszentrum Karlsruhe GmbH Verfahren zur Vergasung von Pyrolysekondensaten
DE19513832B4 (de) * 1995-04-12 2005-08-11 Future Energy Gmbh Verfahren zur Verwertung von Rest- und Abfallstoffen durch Kombination einer Wirbelschichtthermolyse mit einer Flugstromvergasung
GR20080100221A (el) * 2008-04-02 2009-11-19 Μεθοδος αναβαθμισης αεριων προερχομενων απο θερμικη αποδομηση οργανικης μαζας
EP2236587A1 (en) * 2009-04-02 2010-10-06 General Electric Company Modified bio-slurry and process for its production and gasification
ITPR20090048A1 (it) * 2009-06-18 2010-12-19 Renzo Vaiani Procedimento e impianto per la produzione di gas di sintesi da biomasse e/o rifiuti in genere
WO2012063137A3 (en) * 2010-11-08 2012-09-13 Key Group Holding S.R.O. Processing equipment for organic waste

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ATE134698T1 (de) * 1991-11-29 1996-03-15 Noell En Und Entsorgungstechni Verfahren zur thermischen verwertung von abfallstoffen
DE19853717C2 (de) * 1998-11-20 2000-12-21 Krc Umwelttechnik Gmbh Verfahren und Vorrichtungen zur Vergasung kompaktierter organischer Materialien
DE19853713C2 (de) * 1998-11-20 2003-03-13 Bbp Power Plants Gmbh Verfahren zur stofflichen und energetischen Verwertung von Rest- und Abfallstoffen
DE19925316A1 (de) * 1999-05-27 2000-11-30 Technip Benelux B V Verfahren und Anlage zur autothermen Vergasung von festen Brennstoffen
DE19936972C1 (de) * 1999-08-05 2001-02-15 Krupp Uhde Gmbh Mehrstufiges Beschickungsverfahren für stückiges Einsatzgut und Stoffgemische in Druckräume
DE19936971C1 (de) * 1999-08-05 2001-03-01 Krupp Uhde Gmbh Mehrstufiges Beschickungsverfahren für stückiges Einsatzgut und Stoffgemische in Druckräume
DE10258485A1 (de) * 2002-12-10 2004-07-08 Innovativer Anlagenbau E&H Gmbh Verfahren und Vorrichtung zur Gewinnung von Wärmeenergie und/oder motortauglichem Gas durch Vergasung von Feststoffen
SE532711C2 (sv) * 2008-06-11 2010-03-23 Cortus Ab Förfarande och anläggning för framställning av syntesgas
CA2800606C (en) * 2011-02-14 2018-01-02 Zbb Gmbh Device and method for the thermochemical carbonization and gasification of wet biomass

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WO1981000112A1 (en) * 1979-07-05 1981-01-22 Kiener Karl Process and plant for the gazification of solid fuels
GB2109400A (en) * 1981-10-02 1983-06-02 Foster Wheeler Power Prod Thermal conversion systems
EP0120397A2 (de) * 1983-03-23 1984-10-03 C. Deilmann AG Einrichtung zur Gewinnung von Energie aus pyrolisierbaren, kohlenstoffhaltigen Abfallstoffen wechselnder Zusammensetzung
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WO1981000112A1 (en) * 1979-07-05 1981-01-22 Kiener Karl Process and plant for the gazification of solid fuels
GB2109400A (en) * 1981-10-02 1983-06-02 Foster Wheeler Power Prod Thermal conversion systems
US4497637A (en) * 1982-11-22 1985-02-05 Georgia Tech Research Institute Thermochemical conversion of biomass to syngas via an entrained pyrolysis/gasification process
EP0120397A2 (de) * 1983-03-23 1984-10-03 C. Deilmann AG Einrichtung zur Gewinnung von Energie aus pyrolisierbaren, kohlenstoffhaltigen Abfallstoffen wechselnder Zusammensetzung
WO1990002162A1 (de) * 1988-08-23 1990-03-08 Roessle Gottfried Allothermes verfahren zur erzeugung eines brenngases aus müll oder aus müll zusammen mit kohle und vorrichtung zur durchführung des verfahrens

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1994021751A1 (de) * 1993-03-17 1994-09-29 Siemens Aktiengesellschaft Verfahren und einrichtung zum entsorgen von abfall
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WO1995021903A1 (de) * 1994-02-15 1995-08-17 Crg Kohlenstoffrecycling Ges.Mbh Verfahren zur erzeugung von brenngas
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DE10010358A1 (de) * 2000-03-07 2001-09-27 Bsbg Bremer Sonderabfall Berat Verfahren und Vorrichtung zum Vergasen von brennbarem Material
WO2003033624A1 (de) * 2001-10-16 2003-04-24 Forschungszentrum Karlsruhe Gmbh Verfahren zur pyrolyse und vergasung von biomasse
FR2859216A1 (fr) * 2003-08-27 2005-03-04 Inst Francais Du Petrole Procede et installation de production a haut rendement d'un gaz de synthese depollue a partir d'une charge riche en matiere organique
EP1510567A1 (fr) * 2003-08-27 2005-03-02 Institut Francais Du Petrole Procédé et installation de production à haut rendement d'un gaz de synthèse dépollué à partir d'une charge riche en matière organique.
EP1520900A1 (de) * 2003-10-01 2005-04-06 Forschungszentrum Karlsruhe GmbH Verfahren zur Vergasung von Pyrolysekondensaten
GR20080100221A (el) * 2008-04-02 2009-11-19 Μεθοδος αναβαθμισης αεριων προερχομενων απο θερμικη αποδομηση οργανικης μαζας
EP2236587A1 (en) * 2009-04-02 2010-10-06 General Electric Company Modified bio-slurry and process for its production and gasification
ITPR20090048A1 (it) * 2009-06-18 2010-12-19 Renzo Vaiani Procedimento e impianto per la produzione di gas di sintesi da biomasse e/o rifiuti in genere
WO2012063137A3 (en) * 2010-11-08 2012-09-13 Key Group Holding S.R.O. Processing equipment for organic waste

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DE4123406A1 (de) 1993-01-21
EP0600923B1 (de) 1996-08-28
DE4123406C2 (de) 1995-02-02
WO1993002162A1 (de) 1993-02-04
DE59207017D1 (de) 1996-10-02
CA2113636A1 (en) 1993-02-04
EP0600923A1 (de) 1994-06-15
AU2344492A (en) 1993-02-23
FI940184A (fi) 1994-03-11
FI106314B (fi) 2001-01-15
JPH07502766A (ja) 1995-03-23
JP3203580B2 (ja) 2001-08-27
FI940184A0 (fi) 1994-01-14

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