[go: up one dir, main page]

WO2001014502A1 - Procede et appareil de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe - Google Patents

Procede et appareil de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe Download PDF

Info

Publication number
WO2001014502A1
WO2001014502A1 PCT/FI2000/000662 FI0000662W WO0114502A1 WO 2001014502 A1 WO2001014502 A1 WO 2001014502A1 FI 0000662 W FI0000662 W FI 0000662W WO 0114502 A1 WO0114502 A1 WO 0114502A1
Authority
WO
WIPO (PCT)
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.)
Ceased
Application number
PCT/FI2000/000662
Other languages
English (en)
Inventor
Esa Kurkela
Pekka STÅHLBERG
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.)
CONDENS Oy
VTT Technical Research Centre of Finland Ltd
Original Assignee
CONDENS Oy
VTT Technical Research Centre of Finland Ltd
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, VTT Technical Research Centre of Finland Ltd filed Critical CONDENS Oy
Priority to AU64450/00A priority Critical patent/AU6445000A/en
Priority to DK00951552T priority patent/DK1129154T3/da
Priority to EP00951552A priority patent/EP1129154B8/fr
Priority to DE60033782T priority patent/DE60033782T2/de
Publication of WO2001014502A1 publication Critical patent/WO2001014502A1/fr
Anticipated expiration legal-status Critical
Ceased 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.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

La présente invention concerne un procédé destiné à gazéifier un combustible contenant du carbone dans un gazéifieur à lit fixe selon le principe à contre-courant, dans lequel l'alimentation du réacteur de gazéification en combustible est effectuée en au moins un point, situé, à partir du fond du réacteur, à une hauteur comprise entre 20 et 70 % de la hauteur totale du réacteur, le lit de combustible formant en dessous de ce point une zone primaire, dans laquelle se produisent des réactions de pyrolyses réductrices et oxydantes, le procédé comprenant une alimentation en air primaire sous le lit de combustible et une sortie de gaz de combustion au dessus du lit de combustible. L'invention est caractérisée en ce que, concernant le réacteur de gazéification (7) et la zone secondaire au dessus de l'arrivée de combustible (1) on effectue une alimentation en air secondaire au moins à proximité et au dessus du lit de combustible. L'invention concerne aussi un appareil destiné à appliquer le procédé.
PCT/FI2000/000662 1999-07-28 2000-07-27 Procede et appareil de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe Ceased WO2001014502A1 (fr)

Priority Applications (4)

Application Number Priority Date Filing Date Title
AU64450/00A AU6445000A (en) 1999-07-28 2000-07-27 Method and apparatus for gasifying carbon-containing fuel in a fixed layer gasifier
DK00951552T DK1129154T3 (da) 1999-07-28 2000-07-27 Fremgangsmåde til forgasning af carbonholdigt brændstof i en gasgenerator med fast lag
EP00951552A EP1129154B8 (fr) 1999-07-28 2000-07-27 Procede de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe
DE60033782T DE60033782T2 (de) 1999-07-28 2000-07-27 Verfahren zur vergasung von kohlenstoffhaltigen treibstoffen in einem festbettvergaser

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
FI991653 1999-07-28
FI19991653 1999-07-28
FI992111A FI112798B (fi) 1999-07-28 1999-09-30 Menetelmä ja laitteisto hiilipitoisen polttoaineen kaasuttamiseksi kiinteäkerroskaasuttimessa
FI19992111 1999-09-30

Publications (1)

Publication Number Publication Date
WO2001014502A1 true WO2001014502A1 (fr) 2001-03-01

Family

ID=26160769

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/FI2000/000662 Ceased WO2001014502A1 (fr) 1999-07-28 2000-07-27 Procede et appareil de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe

Country Status (8)

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

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2003008864A1 (fr) * 2001-07-20 2003-01-30 Generation Technology Research Pty Ltd Dispositif d'alimentation de charbon a haute teneur en humidite
WO2002097015A3 (fr) * 2001-05-31 2004-05-06 Bernd Joos Dispositif de production d'un melange gazeux combustible
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser
ITPI20100052A1 (it) * 2010-04-26 2011-10-27 Matteo Bertei Processo ed apparato per la gassificazione di materiali organici
CN103697478A (zh) * 2014-01-14 2014-04-02 中信重工机械股份有限公司 水泥窑协同处理城市垃圾系统的连续给料装置及工艺
JP2017096558A (ja) * 2015-11-25 2017-06-01 株式会社エルコム 固形燃料供給装置
CN110160059A (zh) * 2018-03-27 2019-08-23 郭全华 农林木质废料焚烧方法
CN110160061A (zh) * 2018-02-07 2019-08-23 夏培准 节能环保生态系统
CN110160070A (zh) * 2018-03-27 2019-08-23 郭全华 绿色环保型农林木质废料焚烧炉以及供暖供热水系统
CN110160053A (zh) * 2018-02-07 2019-08-23 夏培准 秸秆焚烧炉
CN110160069A (zh) * 2018-03-27 2019-08-23 郭全华 绿色环保型农林木质废料焚烧方法
CN110160078A (zh) * 2018-02-07 2019-08-23 夏培准 秸秆焚烧方法
WO2022225407A1 (fr) * 2021-04-19 2022-10-27 Hot Lime Labs Limited Gazéifieur à tirage ascendant amélioré et procédés d'utilisation

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2010081444A2 (fr) * 2009-01-13 2010-07-22 Dinano Ecotechnology Llc Dispositif de gazéification de matières de départ carbonées
AT510063B8 (de) * 2010-06-21 2012-08-15 Windhager Zentralheizung Technik Gmbh Feuerung zur verbrennung von feststoffen
CN102809148B (zh) * 2012-08-23 2014-12-10 郑州市鼎力干燥设备有限公司 一种继燃热气发生炉
CH717852A1 (de) 2020-09-15 2022-03-15 Eyco Direkt Anstalt Auswringvorrichtung für ein Wischgerät und Auswringsystem mit einer Auswringvorrichtung und einem Eimer.
EP4151706B1 (fr) * 2021-09-15 2025-05-07 Bios Bioenergiesysteme GmbH Procédé et dispositif de fabrication d'un produit de gaz à faible teneur en goudron et en poussières

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3804581A (en) * 1970-12-16 1974-04-16 Metallgesellschaft Ag Process of thermally treating fine-grained solids in an internally heated fluidized bed
US3820964A (en) * 1972-05-30 1974-06-28 Cons Natural Gas Svc Refuse gasification process and apparatus
US4178266A (en) * 1977-01-03 1979-12-11 Didier Engineering Gmbh Process for conveying hot crude coke oven gas from coke ovens to a position of utilization while preventing condensation of higher hydrocarbons
GB2115537A (en) * 1981-12-24 1983-09-07 Kernforschungsanlage Juelich Shaft furnace for producing combustible gas from organic material
US4407701A (en) * 1978-08-28 1983-10-04 Didier Engineering Gmbh Apparatus for treating gases produced from coal
DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
US4776285A (en) * 1987-01-29 1988-10-11 Voest-Alpine Aktiengesellschaft Process for gasifying fuels with oxygen or oxygen-containing gases to be carried out in a shaft-like furnace arrangement
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

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3804581A (en) * 1970-12-16 1974-04-16 Metallgesellschaft Ag Process of thermally treating fine-grained solids in an internally heated fluidized bed
US3820964A (en) * 1972-05-30 1974-06-28 Cons Natural Gas Svc Refuse gasification process and apparatus
US4178266A (en) * 1977-01-03 1979-12-11 Didier Engineering Gmbh Process for conveying hot crude coke oven gas from coke ovens to a position of utilization while preventing condensation of higher hydrocarbons
US4407701A (en) * 1978-08-28 1983-10-04 Didier Engineering Gmbh Apparatus for treating gases produced from coal
GB2115537A (en) * 1981-12-24 1983-09-07 Kernforschungsanlage Juelich Shaft furnace for producing combustible gas from organic material
DE3239624A1 (de) * 1982-10-26 1984-04-26 Kiener Pyrolyse Gesellschaft für thermische Abfallverwertung mbH, 7000 Stuttgart Gasgenerator
US4776285A (en) * 1987-01-29 1988-10-11 Voest-Alpine Aktiengesellschaft Process for gasifying fuels with oxygen or oxygen-containing gases to be carried out in a shaft-like furnace arrangement
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

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2002097015A3 (fr) * 2001-05-31 2004-05-06 Bernd Joos Dispositif de production d'un melange gazeux combustible
EP1436364B2 (fr) † 2001-05-31 2016-02-10 Bernd Joos Dispositif de production d'un melange gazeux combustible
WO2003008864A1 (fr) * 2001-07-20 2003-01-30 Generation Technology Research Pty Ltd Dispositif d'alimentation de charbon a haute teneur en humidite
DE102007012452A1 (de) 2007-03-15 2008-09-25 Mci Management Center Innsbruck Internationale Fachhochschulgesellschaft Mbh Vergaser
DE102007012452B4 (de) * 2007-03-15 2014-01-16 SynCraft Enegineering GmbH Vergaser
ITPI20100052A1 (it) * 2010-04-26 2011-10-27 Matteo Bertei Processo ed apparato per la gassificazione di materiali organici
CN103697478A (zh) * 2014-01-14 2014-04-02 中信重工机械股份有限公司 水泥窑协同处理城市垃圾系统的连续给料装置及工艺
JP2017096558A (ja) * 2015-11-25 2017-06-01 株式会社エルコム 固形燃料供給装置
CN110160078A (zh) * 2018-02-07 2019-08-23 夏培准 秸秆焚烧方法
CN110160061A (zh) * 2018-02-07 2019-08-23 夏培准 节能环保生态系统
CN110160061B (zh) * 2018-02-07 2021-02-05 夏培准 节能环保生态系统
CN110160053A (zh) * 2018-02-07 2019-08-23 夏培准 秸秆焚烧炉
CN110160059A (zh) * 2018-03-27 2019-08-23 郭全华 农林木质废料焚烧方法
CN110160069A (zh) * 2018-03-27 2019-08-23 郭全华 绿色环保型农林木质废料焚烧方法
CN110160070A (zh) * 2018-03-27 2019-08-23 郭全华 绿色环保型农林木质废料焚烧炉以及供暖供热水系统
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
WO2022225407A1 (fr) * 2021-04-19 2022-10-27 Hot Lime Labs Limited Gazéifieur à tirage ascendant amélioré et procédés d'utilisation

Also Published As

Publication number Publication date
DK1129154T3 (da) 2007-07-09
ATE356184T1 (de) 2007-03-15
AU6445000A (en) 2001-03-19
ES2284513T3 (es) 2007-11-16
EP1129154B1 (fr) 2007-03-07
DE60033782T2 (de) 2007-10-31
DE60033782D1 (de) 2007-04-19
FI112798B (fi) 2004-01-15
FI19992111L (fi) 2001-01-28
EP1129154A1 (fr) 2001-09-05
EP1129154B8 (fr) 2007-08-29

Similar Documents

Publication Publication Date Title
EP1129154B1 (fr) Procede de gazeification de combustible contenant du carbone dans un gazeifieur a lit fixe
US4498909A (en) Process for the gasification of fuels
US5026403A (en) Three stage process for producing producer gas from combustible waste products
CN100457870C (zh) 生产燃料气体的方法和气体发生器
KR100641760B1 (ko) 가연성 합성 기체 제조 방법 및 제조 장치
EP3519537B1 (fr) Procédé de conversion de matière carbonée en gaz de synthèse à faible teneur en goudrons
US6615748B2 (en) Gasifier
EP1606370B1 (fr) Procede de production d'un gaz de synthese
EP2633003B1 (fr) Production d'un gaz de synthèse par chauffage d'une biomasse oxydée avec un gaz chaud obtenu à partir de l'oxydation de produits résiduels
WO2007081296A1 (fr) Gazogene a ecoulement descendant/ascendant pour production de gaz de synthese a partir de dechets solides
AU2011336788A1 (en) Method and apparatus for particle recycling in multiphase chemical reactors
WO2015102480A2 (fr) Appareil permettant de produire des biocarburants à partir de biomasse
EP0108317B1 (fr) Procédé de gazéification de produits ligno-cellulosiques et dispositif pour sa mise en oeuvre
JP2012500297A (ja) ２段階同伴ガス化装置および方法
Hamel et al. Autothermal two-stage gasification of low-density waste-derived fuels
CN102453550A (zh) 多喷嘴分级给氧气流床气化炉及其气化方法
DK2281864T3 (en) Solid fuel gasification process and apparatus
Kurkela et al. Production of synthesis gas from biomass residues by staged fixed-bed gasification-results from pilot test campaigns
JP2009108188A (ja) 炭素質原料のガス化装置およびガス化方法
CA2077029A1 (fr) Installation de gazeification a circulation divergente
RU2414503C1 (ru) Установка для получения синтез-газа пиролизом твердого углесодержащего сырья
FI62554B (fi) Foerfarande och anordning foer foergasning av fast kolhaltigt material
CA3172343C (fr) Systeme de traitement de dechets
JP2008169354A (ja) 石炭の水素化熱分解方法及び装置
CA2432202C (fr) Gazeifieur de dechets organiques

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BY BZ CA CH CN CR CU CZ DE DK DM DZ EE ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NO NZ PL PT RO RU SD SE SG SI SK SL TJ TM TR TT TZ UA UG US UZ VN YU ZA ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): GH GM KE LS MW MZ SD SL SZ TZ UG ZW AM AZ BY KG KZ MD RU TJ TM AT BE CH CY DE DK ES FI FR GB GR IE IT LU MC NL PT SE BF BJ CF CG CI CM GA GN GW ML MR NE SN TD TG

WWE Wipo information: entry into national phase

Ref document number: 2000951552

Country of ref document: EP

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWP Wipo information: published in national office

Ref document number: 2000951552

Country of ref document: EP

REG Reference to national code

Ref country code: DE

Ref legal event code: 8642

NENP Non-entry into the national phase

Ref country code: JP

WWG Wipo information: grant in national office

Ref document number: 2000951552

Country of ref document: EP