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WO1993002162A1 - Procede de production de gaz synthetiques ou combustibles a partir de residus et de dechets solides ou pateux ou de combustibles a faible pouvoir calorifique dans un reacteur de gazeification - Google Patents

Procede de production de gaz synthetiques ou combustibles a partir de residus et de dechets solides ou pateux ou de combustibles a faible pouvoir calorifique dans un reacteur de gazeification Download PDF

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Publication number
WO1993002162A1
WO1993002162A1 PCT/EP1992/001607 EP9201607W WO9302162A1 WO 1993002162 A1 WO1993002162 A1 WO 1993002162A1 EP 9201607 W EP9201607 W EP 9201607W WO 9302162 A1 WO9302162 A1 WO 9302162A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
gas
gasification reactor
solid
fraction
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/EP1992/001607
Other languages
German (de)
English (en)
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
Family has litigation
First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=6436185&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO1993002162(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Veba Oel Technologie und Automatisierung GmbH, John Brown Deutsche Engineering GmbH filed Critical Veba Oel Technologie und Automatisierung GmbH
Priority to DE59207017T priority Critical patent/DE59207017D1/de
Priority to EP92916028A priority patent/EP0600923B1/fr
Priority to CA002113636A priority patent/CA2113636A1/fr
Publication of WO1993002162A1 publication Critical patent/WO1993002162A1/fr
Priority to FI940184A priority patent/FI106314B/fi
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
    • C10J3/58—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 claim 1.
  • Inferior fuels such as wet brown coal or hard coal with a high tar content, old tires, etc. can already be gasified today - even without undesired emissions in the product gas withdrawn; in particular, 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 for this purpose, in which the special feature is that the bulk material bed in the primary gas chamber is constructed in two layers.
  • a first layer of rubble Gutbettes 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 supplies the sensible heat required for the endothermic gasification process.
  • the primary gas burner z. B. waste 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 primary gas reacts with this batch to raw gas.
  • the raw gas has z. B. 1,864 ° C and then flows through the second bulk bed of coke and leaves this as finished product gas at the upper end of the shaft gasifier.
  • the thickness of the (second) bed of bulk goods ie the charge to be gasified (inferior fuel) and on the setting of the primary gasification, whether the charge lying behind the second bed of bulk goods, e.g. B. the higher quality coke, also gasified or used only or primarily as a filter for the raw gas passing through.
  • the setting of the Primärvergasu ⁇ g either the ratio of oxygen to carbon carrier in Bren ⁇ ner, or the total amount of Primärvergasungsstoffe ⁇ or - if introduced instead of air, pure oxygen through the burners' is - vapor on the ratio of oxygen to Wasser ⁇ (EP 0194252 Bl).
  • the invention is based on the object, in the gasification of inferior and / or difficult to handle starting materials and / or residues and waste materials containing organic constituents, in particular in the gasification of the shredder light fraction during motor vehicle utilization, a product gas quality which is as uniform as possible to ensure activity.
  • the gas fraction and the solid fraction in particular when the feedstock is a light shredder fraction, are obtained in a quantity ratio of combustible or gasifiable material as is the case for operation a shaft gasifier or entrained flow gasification reactor is required (about 60% gas fraction and about 40% solid fraction); it is practically not necessary to add other fuels in a primary gas burner;
  • the solid fraction from the thermal pretreatment has properties such as a smelted coke; therefore in the gasification on the use of z. B. cottage coke can be dispensed with entirely, so that the secondary fraction in the gasification reactor (solid charge) only consists of the solid fraction of the thermally treated inferior feedstock; if a shaft gasifier is used, it no longer requires two different charging goods and can therefore be of simpler construction, as described, for example, in DE 29 20 922 C3 or in EP 0 143 106 B1;
  • 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 operating according to the entrained flow principle (also known as the airborne dust principle) is preferred according to the invention, there is alternatively also a gasification reactor operating according to the fluidized bed principle, as it u. a. is addressed in EP-B1-0 011 151, for use according to the invention.
  • entrained flow principle also known as the airborne dust principle
  • a so-called fluidized bed gasifier uses a relatively wide and coarse grain size range for the solid to be gasified in the gasifier (typical values are 0.1 mm to 100 mm), grain size ranges of about 0.001 mm to 5 mm are used for so-called entrained flow gasifiers .
  • the particle size range of the solid fraction obtained behind the pyrolysis treatment stage according to the invention is adjusted after the pyrolysis treatment and before the entrained flow gasification by grinding, sieving and / or sifting, the particle size range being reduced (claim 2).
  • 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 major handling problems when charging the solid fraction; A relatively uniform product gas quality is also ensured with this driving style.
  • the shaft carburettors mentioned at the outset (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 bulk material bed formed by the solid charge material below the passage is formed above a support surface, the pro ⁇ duct gas and the slag are withdrawn from the gasification process in a suitable manner.
  • a primary gas burner 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 total primary gas burner, in order in this way to supply the endothermic gasification process with gasification heat.
  • the gas fraction and, if appropriate, further fuels are preferably supplied with the formation of 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 'the Vergasungsreak- Tor or the pyrolysis treatment stage for introducing heat for the endothermic pyrolysis or gasification step, or admixed to the product gas obtained behind the gasification reactor as part of the combustion or synthesis gas.
  • the liquid fraction obtained after 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 conveying bodies and procedures for this purpose 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, pasty not only contains solid / liquid mixtures, but also more or less thickened.
  • liquid feedstocks ie residues and waste materials and / or inferior fuels containing organic constituents, can in principle also be used or used for the production process of synthetic and / or fuel gases according to the invention.
  • liquid feedstocks of the aforementioned type can also be converted to synthesis and / or fuel gases in other processes.
  • gasification reactor in addition to those which, as is preferred, work according to the entrained flow principle or are designed as shaft gasifiers, other types of gasifiers can also be used according to the invention.
  • gasifiers can also be used according to the invention.
  • 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 slight negative pressure (if suction draft fans are used).
  • the invention is therefore based on the basic idea of producing synthetic and / or fuel gases from residues and waste materials containing organic constituents and / or inferior fuels (feedstock) with oxygen or oxygen-old gases and possibly water vapor, the feedstock first by thermal pretreatment with supply of heat and essentially avoiding combustion of constituents of the starting material (pyrolyzation treatment) into a gaseous and a solid fraction under operating conditions, the solid fraction to produce 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 procedural 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 is a block diagram as well
  • FIG. 2 shows a simplified process sketch for the application of a shaft gasifier.
  • FIG. 1 The block diagram shown in 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 stages ⁇ that are preferably used are additionally outlined with a dashed line.
  • feedstock an organic constituent containing residual or waste material and / or inferior fuel, hereinafter referred to as feedstock
  • a pyrolysis treatment stage 101 such as e.g. an indirectly heated rotary kiln (drum wall temperature up to 900 ° C).
  • the feed is pretreated, largely free of oxygen, with the addition of heat and essentially avoiding the burning of constituents of the feed at temperatures between approx. 300 and 650 ° C.
  • extraneous gas behind the gasification reactor 102 product gas and / or the condensation stage 103 downstream of a pyrolysis stage, preferably 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 sifting 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, are 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 vapor to the gasification reactor for the gasification and / or introduction of heat of reaction or is first passed through a condensation stage 103.
  • the residual gas deposited therein under the condensation conditions is either fed, preferably after passing through a pyrolysis gas purification stage 104, to the pyrolysis treatment stage for introducing process heat.
  • the pyrolysis gas can be fed to the gasification reactor 102 or the product gas stream behind it to introduce gasification heat. In these cases, a pyrolysis gas purification stage may be omitted.
  • the oil (liquid fraction) obtained behind 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 pyrolytic 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.
  • 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 further.
  • the product gas accumulating behind the gas purification stage 108 can, as is preferred, be fired in a power plant 109, possibly already existing, or, if necessary partially, in the pyrolysis treatment stage 101 or used as synthesis gas or other fuel gas.
  • Schachtverga ⁇ ser 100 shown in detail in FIG. 2 is known from DE 29 20 922 C3.
  • a pressure vessel 1 which has external insulation 33, forms the shaft carburetor 100.
  • the pressure vessel 1 has a vertical upper section and a laterally angled lower section.
  • the solid charge is placed on a lock 4, which after each cycle with an inert gas, for. B. steam is flushed through a line 5.
  • the lumpy, solid cargo arrives in a basket 3 from cooling water pipes accommodated in the pressure vessel 1 and forms a bed 11 therein with a cone of material 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 fill surface 13, which delimits the primary gas chamber 21 on this side, inevitably arises at the lower end of the fill 11.
  • the Schüttu ⁇ g 11 on a at the lower part of the basket 3 also formed by coolant lines slag pan 22.
  • the inside of the basket 3, including the slag tray 20, is provided with a refractory ramming compound 32.
  • the slope forming the lower free fill surface 13 of the fill 11 is at a distance from an overflow weir 16 formed on 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 wall 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 is arranged in the wall of the pressure vessel 1, 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 downward 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 opposite to the slag flow flowing to the overflow weir 16.
  • the "solid fraction” can be separated into its components “pyrolysis coke” and “valuable 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 carburetor 100 via the lock 4.
  • the "pyrolysis gas” (gas fraction) obtained in the thermal pretreatment is fed to the primary gas burner 2.

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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)

Abstract

Un procédé permet de produire des gaz synthétiques et/ou combustibles à partir de résidus et de déchets contenant des éléments organiques et ou de combustibles à faible pouvoir calorifique (matières chargées) avec des gaz contenant de l'oxygène, dans un gazéificateur vertical ou à courant volant. Afin d'obtenir un gaz ayant une qualité uniforme malgré les difficultés de traitement des matières chargées, qui peuvent notamment être constituées par des matières légères produites par un shredder de récupération de véhicules à moteur, un étage de traitement par pyrolyse précède le réacteur de gazéification. Les matières solides sortant de l'étage de traitement par pyrolyse sont gazéifiées dans le réacteur de gazéification et la fraction gazeuse sortant de l'étage de traitement par pyrolyse est utilisée pour apporter de la chaleur au processus de production et/ou pour produire davantage de gaz.
PCT/EP1992/001607 1991-07-15 1992-07-15 Procede de production de gaz synthetiques ou combustibles a partir de residus et de dechets solides ou pateux ou de combustibles a faible pouvoir calorifique dans un reacteur de gazeification Ceased WO1993002162A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
DE59207017T DE59207017D1 (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
EP92916028A EP0600923B1 (fr) 1991-07-15 1992-07-15 Procede de production de gaz synthetiques ou combustibles a partir de residus et de dechets solides ou pateux ou de combustibles a faible pouvoir calorifique dans un reacteur de gazeification
CA002113636A CA2113636A1 (fr) 1991-07-15 1992-07-15 Procede de production de gaz synthetiques ou combustibles a partir de residus ou de dechets solides ou pateux ou de combustibles pauvres dans un reacteur de gazeification
FI940184A FI106314B (fi) 1991-07-15 1994-01-14 Menetelmä synteesikaasun valmistamiseksi

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DEP4123406.5 1991-07-15
DE4123406A DE4123406C2 (de) 1991-07-15 1991-07-15 Verfahren zum Vergasen von minderwertigen festen Brennstoffen in einem schachtförmigen Vergasungsreaktor

Publications (1)

Publication Number Publication Date
WO1993002162A1 true WO1993002162A1 (fr) 1993-02-04

Family

ID=6436185

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP1992/001607 Ceased WO1993002162A1 (fr) 1991-07-15 1992-07-15 Procede de production de gaz synthetiques ou combustibles a partir de residus et de dechets solides ou pateux ou de combustibles a faible pouvoir calorifique dans un reacteur de gazeification

Country Status (7)

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

Cited By (3)

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US5550312A (en) * 1991-11-29 1996-08-27 Noell-Dbi Energie-Und Entsorgungstechnik Gmbh Method of thermal utilization of waste materials
DE19925316A1 (de) * 1999-05-27 2000-11-30 Technip Benelux B V Verfahren und Anlage zur autothermen Vergasung von festen Brennstoffen
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

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DE4308551A1 (de) * 1993-03-17 1994-01-05 Siemens Ag Verfahren und Einrichtung zum Entsorgen von Abfall
GR1001615B (el) * 1993-06-04 1994-07-29 Viokat Anonymos Techniki & Vio Μέ?οδος αεριοποίησης στερεών καυσίμων χαμηλού ?ερμικού περιεχομένου με ωφέλιμη αξιοποίηση στην παραγωγή ηλεκτρικής ενέργειας χωρίς δημιουργία ρύπανσης περιβάλλοντος.
DE4404673C2 (de) * 1994-02-15 1995-11-23 Entec Recycling Und Industriea Verfahren zur Erzeugung von Brenngas
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
DE19608093C2 (de) * 1996-03-02 2000-08-10 Krc Umwelttechnik Gmbh Verfahren zur Verwertung von Rest- und Abfallstoffen sowie heizwertarmen Brennstoffen in einem Zementofen
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
DE19936971C1 (de) * 1999-08-05 2001-03-01 Krupp Uhde Gmbh Mehrstufiges Beschickungsverfahren für stückiges Einsatzgut und Stoffgemische in Druckräume
DE19936972C1 (de) * 1999-08-05 2001-02-15 Krupp Uhde Gmbh Mehrstufiges Beschickungsverfahren für stückiges Einsatzgut und Stoffgemische in Druckräume
DE10010358A1 (de) * 2000-03-07 2001-09-27 Bsbg Bremer Sonderabfall Berat Verfahren und Vorrichtung zum Vergasen von brennbarem Material
DE10151054A1 (de) * 2001-10-16 2003-04-30 Karlsruhe Forschzent Verfahren zur Behandlung von Biomasse
FR2859216B1 (fr) * 2003-08-27 2008-07-04 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
DE10345672B4 (de) * 2003-10-01 2005-12-29 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
SE532711C2 (sv) * 2008-06-11 2010-03-23 Cortus Ab Förfarande och anläggning för framställning av syntesgas
EP2236587A1 (fr) * 2009-04-02 2010-10-06 General Electric Company Boues biologiques modifiées et procédé pour sa production et sa gazéification
IT1398667B1 (it) * 2009-06-18 2013-03-08 Vaiani Procedimento e impianto per la produzione di gas di sintesi da biomasse e/o rifiuti in genere
CZ2010807A3 (cs) * 2010-11-08 2010-12-22 Key@Group@Holding@@s@r@o Zpusob@zpracování@organického@odpadu@@zarízení@najeho@zpracování@a@použití@zpracovaných@produktu
DE112011104882A5 (de) * 2011-02-14 2013-11-28 Zbb Gmbh Vorrichtung und ein Verfahren zur thermochemischen Harmonisierung und Vergasung von Feuchtigkeits-Biomasse

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GB2109400A (en) * 1981-10-02 1983-06-02 Foster Wheeler Power Prod Thermal conversion systems
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JPH07502766A (ja) 1995-03-23
DE4123406C2 (de) 1995-02-02
FI940184A0 (fi) 1994-01-14
EP0600923B1 (fr) 1996-08-28
JP3203580B2 (ja) 2001-08-27
DE59207017D1 (de) 1996-10-02
EP0600923A1 (fr) 1994-06-15
CA2113636A1 (fr) 1993-02-04
EP0523815A1 (fr) 1993-01-20
AU2344492A (en) 1993-02-23
FI940184A7 (fi) 1994-03-11
DE4123406A1 (de) 1993-01-21

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