EP1129154A1 - Verfahren und vorrichtung zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser - Google Patents

Verfahren und vorrichtung zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser

Info

Publication number
EP1129154A1
EP1129154A1 EP00951552A EP00951552A EP1129154A1 EP 1129154 A1 EP1129154 A1 EP 1129154A1 EP 00951552 A EP00951552 A EP 00951552A EP 00951552 A EP00951552 A EP 00951552A EP 1129154 A1 EP1129154 A1 EP 1129154A1
Authority
EP
European Patent Office
Prior art keywords
fuel
reactor
gasifying reactor
gasifying
feed
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.)
Granted
Application number
EP00951552A
Other languages
English (en)
French (fr)
Other versions
EP1129154B1 (de
EP1129154B8 (de
Inventor
Esa Kurkela
Pekka Stahlberg
Ilkka Haavisto
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.)
KOKEMAEEN KAASUTIN OY
Wartsila Finland Oy
Original Assignee
Condens Oy
Valtion Teknillinen Tutkimuskeskus
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 Condens Oy, Valtion Teknillinen Tutkimuskeskus filed Critical Condens Oy
Publication of EP1129154A1 publication Critical patent/EP1129154A1/de
Publication of EP1129154B1 publication Critical patent/EP1129154B1/de
Application granted granted Critical
Publication of EP1129154B8 publication Critical patent/EP1129154B8/de
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L1/00—Passages or apertures for delivering primary air for combustion 
    • F23L1/02—Passages or apertures for delivering primary air for combustion  by discharging the air below the fire
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/34—Grates; Mechanical ash-removing devices
    • C10J3/40—Movable grates
    • C10J3/42—Rotary grates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/58—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
    • C10J3/72—Other features
    • C10J3/725—Redox processes
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content
    • C10K3/008—Reducing the tar content by cracking
    • 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
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/02—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment
    • C10K3/023—Reducing the tar content
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/027—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment pyrolising or gasifying stage
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23K—FEEDING FUEL TO COMBUSTION APPARATUS
    • F23K3/00—Feeding or distributing of lump or pulverulent fuel to combustion apparatus
    • F23K3/16—Over-feed arrangements
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L9/00—Passages or apertures for delivering secondary air for completing combustion of fuel 
    • F23L9/02—Passages or apertures for delivering secondary air for completing combustion of fuel  by discharging the air above the fire
    • 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
    • C10J2200/15—Details of feeding means
    • C10J2200/158—Screws
    • 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
    • C10J2300/0956—Air or oxygen enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2205/00—Waste feed arrangements
    • F23G2205/12—Waste feed arrangements using conveyors
    • F23G2205/121—Screw conveyor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2209/00—Specific waste
    • F23G2209/26—Biowaste

Definitions

  • the invention relates to a method for gasifying carbon-containing fuel by counter- current principle in a fixed layer gasifier, where fuel and from under the fuel bed primary air is fed to the gasifying reactor and product gas is removed from above of the fuel bed.
  • the invention relates also to an apparatus for application of the method.
  • Prior art apparatus for gasifying fuel in fixed layer gasifiers exist in two basic types, that is cocurrent gasifiers and countercurrent gasifiers.
  • the fuel is fed to upper parts of the gasifying reactor, from which it is flows due to gravity through drying, pyrolysis, oxidizing and reducing zones.
  • the gasifying air is introduced directly to the hottest combustion zone, through which even the products of pyrolysis travel.
  • the diameter of the combustion zone is often smaller than in other parts of the reactor.
  • a cocurrent gasifier is applicable only to good quality fuels in piece form that flow without interference through the gasifyig reactor, such as chopped wood, briquets, wood charcoal in piece form and good quality chips.
  • the operation of the gasifying reactor is easily disturbed due to channeling of the bed and arching of the fuel.
  • the temperature in the combustion zone rises often to such high values that the ashes of many biofuels melt.
  • a nearly ash-free pure wood fuel or a fuel the ashes of which don't melt easily are used in cocurrent gasifiers.
  • the scaling of the gasifier of the cocurrent gasifier is difficult, because while the gasifying reactor and its narrowing, choke, diameters get larger, it is very difficult to accomplish an evenly hot oxidizing zone and due to this, the tars are not totally disintegrated. Furthermore, a total conversion of the remaining coal is not accomplished in the gasifying reactor whereby the efficiency remains low.
  • the fuel also flows due to gravity downwards from the above.
  • the gasifying air is introduced upwards from down below in a direction opposite to the flow of fuel.
  • the fuel is thus dried and undergoes pyrolysis in upper parts of the gasifying reactor, whereby the pyrolysis products enter almost as such into the product gas, that is, the tars do not disintegrate as in cocurrent gasifiers.
  • the remaining charcoal from pyrolysis travels eventually through the oxidizing zone, where in practice all combustible material is reacted, whereby the conversion of charcoal is more or less complete.
  • the thermal efficiency of the countercurrent gasifier is thus higher than that of the cocu ⁇ ent gasifier.
  • the problems of melting ashes encountered with the cocurrent gasifiers can be avoided by regulating the temperature of the oxidizing zone by means of added steam.
  • the gasifying reactor can be designed as a simple chute oven where choke structures are not needed.
  • an objective of the invention is to free the coimtercurrent gasifier of the problems mentioned above and at the same time, produce product gas, the tar content of which is at the level of the cocurrent gasifier.
  • an objective is to produce gas with a low tar content of various types of biofuels that are not applicable to traditional fixed layer gasifiers. This has been accomplished as represented in accompanying claims.
  • An objective of the invention is thus a method for gasifying carbon-containing fuel in a fixed layer gasifier according to the coimtercurrent principle, where fuel is fed to the gasifying reactor to at least one point, which is, when seen from the reactor bottom up, at a height that is 20-70% of total height of the reactor, whereby below the feed point the fuel bed forms a primary zone, where pyrolysis, reductive and oxidative reactions occur, and whereby primary air is fed from under the fuel bed and from the reactor, from above of the fuel bed, product gas is removed.
  • the invention is characterized in that to the gasifying reactor (7), to the secondary zone above the feed point of the fuel (1) and above the fuel bed, secondary air is fed at least to the immediate vicinity of the fuel bed.
  • fuel is fed to the gasifying reactor to a point, the height of which is, when seen from the reactor bottom up, 30- 50% of total reactor height.
  • fuel is fed to the gasifying reactor essentially at its imaginary vertical axis.
  • the fuel may be fed to the gasifying reactor also near the reactor wall, for example.
  • the fuel is fed with the aid of a feed pipeline extending to the point of feed, whereby it is especially preferred that the feed pipeline is vertical.
  • the fuel is fed to the gasifying reactor in a compulsory manner.
  • This kind of compulsory feeding of fuel to the gasifying reactor can be accomplished with a screw feeder, for example, that feeds new fuel against the bed in the gasifying reactor.
  • a compulsory feeding of fuel is preferably accomplished with the aid of a vertical feed pipeline when wishing to feed the fuel to the imaginary vertical axis of the gasifying reactor.
  • the number of feed points depends on the size of the gasifying reactor, that is, for example, the bigger the reactor, the more feed pipelines are preferably used. It is even possible to arrange the feed pipelines in such a manner that they are arranged to different points of the reactor cross-section. It is preferred that the feed points are in the same plane when viewed vertically.
  • the fuel may be, for example, coal, peat, solid biomass such as sawdust or wood chips, or waste-based recycled fuel.
  • Secondary air is fed to the process most preferably in several stages, of which the first feed takes place to essentially immediate vicinity of the pyrolysis layer.
  • the temperature of the secondary zone can be raised to a level of 400-1000°C, preferably 650-800°C.
  • pyrolysis products formed in gasifying that is tars
  • the primary zone temperature is downgraded enough by feeding water vapor in order for the fuel ashes not to melt in the gasifier.
  • a movable grate on the bottom of the gasifying reactor is preferably arranged a movable grate according to some known technique per se, for example a rotating cone- shaped grate.
  • the primary air is fed to the reactor preferably through the grate.
  • the primary air can consist also of some other oxidizing gas than air, for example oxygen or a mixture of oxygen and water vapor. It is even possible to add water vapor to the air.
  • carrier air can be fed into the fuel in at least one point of the fuel feed line. This carrier air forms at the same time part of the secondary air needed.
  • a cracking organ for the product gas which constitutes a tertiary zone.
  • the cracking organ may be a thermal or catalytic cracking organ according to some technique known per se, which may in addition be based on tertiary air feed.
  • the easily decomposed and unstable organic compounds contained in the product gas of the coimtercurrent gasifier are decomposed in two or more stages, of which the first is the decomposition in the secondary zone described above, and other decompositions taking place in the cracking organ of the tertiary zone.
  • the temperature of the tertiary zone is higher than the temperature in the secondary zone, for example 800-1100°C.
  • an object of the invention is an apparatus for application of the method described above, which apparatus comprises a fixed layer gasifier, where the opening for fuel of one or more feed inlets is situated in the gasifying reactor at a height that is 20-70% of the total height of the gasifying reactor, and which has a feed inlet for primary air as well as an outlet channel for product gas.
  • the apparatus is characterized in that the inlet opening for fuel of a feed pipeline is situated in the gasifying reactor at a height that is 20-70% of the total height of the gasifying reactor and that in the gasifying reactor, above the opening of a feed inlet is arranged at least one secondary air feed inlet.
  • the secondary air feed inlets of the apparatus are preferably arranged in annular and staged manner in the vertical direction of the gasifying reactor in one or more planes.
  • the height of the gasifying reactor is 3-4 m
  • the height of the primary zone of the gasifying reactor is about 0,7 - 1,5 m.
  • FIG. 1 is presented feeding of fuel 1 through a feeding channel 2 to a purge container 3.
  • a resolve unit 6 that disperses the fuel 1 to an even mass.
  • fuel 1 is transported to a gasifying reactor 7 with the aid of screw conveyors 10, 11 that are mounted in feed pipelines 8 and 9.
  • more feed pipelines for carrier gas can be arranged in feed pipelines 8, 9.
  • the inlet opening of feed pipeline 9 is situated in the middle of gasifying reactor 7 to which the screw conveyor 11 is compulsorily feeding fuel 1.
  • the pretreatment of fuel of the inventive apparatus before it is fed to the gasifying reactor may be realized also by some other means known per se.
  • FIG. 1 is presented secondary air feed pipeline inlets 12, 13 that are arranged in the gasifying reactor 7, above the inlet opening of the feed pipeline 9. It is preferred that secondary air inlet is accomplished through several annularly mounted air nozzles that are situated in more than one plane vertically.
  • the grate 14 On the bottom of the gasifying reactor 7 there is also a movable grate 14 according to some technique known er se to those skilled in the art.
  • the grate 14 may be a three-dimensional cone-shaped, periodically and slowly rotating grate shown in the picture.
  • the grate 14 Through the grate 14 primary air and steam 15 are fed into the gasifying reactor through a feed inlet 16. It is preferred that the grate 14 is designed such that primary air and steam 15 are fed into the gasifying reactor 7 in more than one plane.
  • an outlet opening 17 for removal of bottom ashes from the gasifying reactor 7.
  • the outlet opening 17 is according to some technique known per se, for example a bottom valve.
  • FIG. 1 is also presented an outlet channel 18 for product gas, the opening of which in situated in upper parts of the gasifying reactor 7.
  • product gas is introduced to a cracker 19, which in the apparatus shown is of a two-piece design.
  • the cracker 19 that is shown comprises in the first place a thermal cracker 20 into which tertiary air 21 is introduced, and thereafter a catalytic cracker 22.
  • the thermal and catalytic crackers are according to some technique known pe se. It is also evident that the product gas may be purified by some other means known to those skilled in the art.
  • the purified product gas 23 is obtained from the apparatus through outlet channel 24.
  • the temperature in the secondary zone of the gasifying reactor was 660°C and the temperature of the gas exiting from a thermal cracker connected to the rear of the gasifying reactor was 710°C.
  • the dust content of the product gas was when measured after cracking 0.1-0.5 g/m 3 n and the tar contents before and after cracking were 2.8-3.5 g/m 3 n and 1.1-2.2 g/m 3 n.
  • the temperature in the secondary zone of the gasifying reactor was 750°C and the temperature of the gas exiting from a thermal cracker connected to the rear of the gasifying reactor was 820°C.
  • the dust content of the product gas was when measured after cracking 0.1 g/m 3 n and the tar contents before and after cracking were 2.2-2.9 g/m 3 n and 0.7 g/m 3 n.
  • the temperature in the secondary zone of the gasifying reactor was 750°C and the temperature of the gas exiting from a thermal cracker connected to the rear of the gasifying reactor was 870°C.
  • the dust content of the product gas was when measured after cracking 0.25 g/m 3 n and the tar contents before and after cracking were 2.7-2.9 g/m 3 n and 0.3-0.4 g/m 3 n.
  • the temperature in the secondary zone of the gasifying reactor was 760°C and the temperature of the gas exiting from a thermal cracker connected to the rear of the gasifying reactor was 870°C.
  • the dust content of the product gas was when measured after cracking 0.5-0.6 g/m 3 n and the tar contents before and after cracking were 2.1-3.7 g/m 3 n and 0.6 g/m 3 n.
  • Table 1 The Fuels Used in the Examples
  • the tar contents of the product gas after the secondary zone of the gasifying reactor were about 2-4 g/m 3 n.
  • the tar content of the prodct gas is of the order of 50 g/m 3 n.
  • the tar content of product gas achieved by the inventive method was even lower than what has been determined with applicant's own fluidized bed gasifiers, and is very close to the level (about 1,5 g/m n) that was realized when gasifying ideal chopped wood with commercial Martezon Cocurrent Gasifier.
  • the purification of the product gases of the examples was investigated also by introducing the product gases to both a thermal and a catalytic cracker to which tertiary air was fed.
  • the tar content of product gases was after the thermal cracker 300-700 mg/m 3 n, and when the product gases were additionally driven through a nickel catalysis cracker, a tar content of 10-150 mg/m 3 n was achieved.
  • traditional thermal cracking of the product gas of a traditional countercurrent gasifier produces a tar content of 1500-4000 mg/m 3 n, that is, by the inventive method considerably lower tar contents are realized.
EP00951552A 1999-07-28 2000-07-27 Verfahren zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser Expired - Lifetime EP1129154B8 (de)

Applications Claiming Priority (5)

Application Number Priority Date Filing Date Title
FI991653 1999-07-28
FI991653 1999-07-28
FI992111 1999-09-30
FI992111A FI112798B (fi) 1999-07-28 1999-09-30 Menetelmä ja laitteisto hiilipitoisen polttoaineen kaasuttamiseksi kiinteäkerroskaasuttimessa
PCT/FI2000/000662 WO2001014502A1 (en) 1999-07-28 2000-07-27 Method and apparatus for gasifying carbon-containing fuel in a fixed layer gasifier

Publications (3)

Publication Number Publication Date
EP1129154A1 true EP1129154A1 (de) 2001-09-05
EP1129154B1 EP1129154B1 (de) 2007-03-07
EP1129154B8 EP1129154B8 (de) 2007-08-29

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP00951552A Expired - Lifetime EP1129154B8 (de) 1999-07-28 2000-07-27 Verfahren zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser

Country Status (8)

Country Link
EP (1) EP1129154B8 (de)
AT (1) ATE356184T1 (de)
AU (1) AU6445000A (de)
DE (1) DE60033782T2 (de)
DK (1) DK1129154T3 (de)
ES (1) ES2284513T3 (de)
FI (1) FI112798B (de)
WO (1) WO2001014502A1 (de)

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AU2002317170A1 (en) † 2001-05-31 2002-12-09 Bernd Joos Device for producing a combustible gas mixture
AUPR650501A0 (en) * 2001-07-20 2001-08-09 Generation Technology Research Pty Ltd A feeder for high moisture content coal
DE102007012452B4 (de) 2007-03-15 2014-01-16 SynCraft Enegineering GmbH Vergaser
WO2010081444A2 (de) * 2009-01-13 2010-07-22 Dinano Ecotechnology Llc Anordnung zur vergasung von kohlenstoffhaltigen ausgangsstoffen
IT1399655B1 (it) * 2010-04-26 2013-04-26 Bertei Processo ed apparato per la gassificazione di materiali organici
AT510063B8 (de) * 2010-06-21 2012-08-15 Windhager Zentralheizung Technik Gmbh Feuerung zur verbrennung von feststoffen
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JP6392733B2 (ja) * 2015-11-25 2018-09-19 株式会社エルコム 固形燃料供給装置
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CN110160070B (zh) * 2018-03-27 2021-08-03 大唐长热吉林热力有限公司 绿色环保型农林木质废料焚烧炉以及供暖供热水系统
CH717852A1 (de) 2020-09-15 2022-03-15 Eyco Direkt Anstalt Auswringvorrichtung für ein Wischgerät und Auswringsystem mit einer Auswringvorrichtung und einem Eimer.
EP4326838A1 (de) * 2021-04-19 2024-02-28 Hot Lime Labs Limited Verbesserter aufwindvergaser und verfahren zur verwendung

Family Cites Families (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE2061829C2 (de) * 1970-12-16 1982-01-14 Metallgesellschaft Ag, 6000 Frankfurt Verfahren zur thermischen Behandlung feinkörniger Feststoffe in einem Wirbelbett mit Innenverbrennung
US3820964A (en) * 1972-05-30 1974-06-28 Cons Natural Gas Svc Refuse gasification process and apparatus
DE2700044A1 (de) * 1977-01-03 1978-07-06 Didier Eng Verfahren zur verhinderung von kondensation beim transport heissen koksofenrohgases zur verwendungsstelle
DE2837416C3 (de) * 1978-08-28 1981-11-05 Didier Engineering Gmbh, 4300 Essen Vorrichtung zur Weiterverarbeitung von Kohleentgasungsrohgas
DE3151477C2 (de) * 1981-12-24 1985-10-10 Kernforschungsanlage Jülich GmbH, 5170 Jülich Schachtvergaser zur kontinuierlichen Erzeugung von Brenngas aus organischem Material
DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
AT388925B (de) * 1987-01-29 1989-09-25 Voest Alpine Ind Anlagen Verfahren zum vergasen von brennstoffen mit sauerstoff in einem schachtfoermigen ofen
US5020453A (en) * 1990-02-12 1991-06-04 Kabushiki Kaisha Plantec Vertical incinerator
US5195449A (en) * 1992-02-12 1993-03-23 Kiyoharu Michimae Dry distillation type incinerator

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of WO0114502A1 *

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP4151706A1 (de) * 2021-09-15 2023-03-22 Bios Bioenergiesysteme GmbH Verfahren und vorrichtung zur herstellung eines teer- und staubarmen produktgases

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ES2284513T3 (es) 2007-11-16
WO2001014502A1 (en) 2001-03-01
FI112798B (fi) 2004-01-15
EP1129154B1 (de) 2007-03-07
DE60033782T2 (de) 2007-10-31
DE60033782D1 (de) 2007-04-19
FI19992111A (fi) 2001-01-28
AU6445000A (en) 2001-03-19
DK1129154T3 (da) 2007-07-09
ATE356184T1 (de) 2007-03-15
EP1129154B8 (de) 2007-08-29

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