WO2012110236A1 - Production de carbone et de gaz combustibles à partir de lignite - Google Patents

Production de carbone et de gaz combustibles à partir de lignite Download PDF

Info

Publication number
WO2012110236A1
WO2012110236A1 PCT/EP2012/000669 EP2012000669W WO2012110236A1 WO 2012110236 A1 WO2012110236 A1 WO 2012110236A1 EP 2012000669 W EP2012000669 W EP 2012000669W WO 2012110236 A1 WO2012110236 A1 WO 2012110236A1
Authority
WO
WIPO (PCT)
Prior art keywords
zone
lignite
brown coal
carbon
pyrolysis
Prior art date
Application number
PCT/EP2012/000669
Other languages
German (de)
English (en)
Inventor
Bernd Schottdorf
Original Assignee
European Charcoal Ag
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
Priority claimed from DE102011011521A external-priority patent/DE102011011521A1/de
Application filed by European Charcoal Ag filed Critical European Charcoal Ag
Priority to CN201280009211.0A priority Critical patent/CN103517969A/zh
Priority to EP12704699.3A priority patent/EP2675872A1/fr
Publication of WO2012110236A1 publication Critical patent/WO2012110236A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10F—DRYING OR WORKING-UP OF PEAT
    • C10F5/00—Drying or de-watering peat
    • C10F5/06—Drying or de-watering peat combined with a carbonisation step for producing turfcoal
    • 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
    • C10J3/22—Arrangements or dispositions of valves or flues
    • C10J3/24—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed
    • C10J3/26—Arrangements or dispositions of valves or flues to permit flow of gases or vapours other than upwardly through the fuel bed downwardly
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal

Definitions

  • the invention relates to a process for the production of carbon and combustible gases from lignite.
  • Lignite is the largest German fossil energy source. German brown coal has an average water content of about 50%. Their calorific value is relatively low, usually at most 28.5 MJ / kg, while that of hard coal is in the range of 35 MJ / kg.
  • Lignite is usually dried and burned to burn in house fire
  • Lignite briquettes processed. Dried lignite typically contains about 60-75% carbon, 6.0-5.8% hydrogen, 17-34% oxygen, 0.5-3% sulfur and 1-1, 2% nitrogen.
  • the object of the invention was to convert lignite into substances that can be burned in simpler, cheaper and less prone to failure facilities than in
  • Essentially pure, at least about 90% carbon comprises, which is continuously removed.
  • FIG. 1 shows a suitable one for carrying out the method according to the invention
  • Fig. 2 shows a suitable for carrying out the method according to the invention
  • FIG. 3 shows a further reactor battery suitable for carrying out the process according to the invention.
  • a carbon concentrate such as charcoal
  • ash and pyrolysis gas which are thermally and electrically easy to recycle, can be converted.
  • the method is based on wet lignite or dry lignite, e.g. in the form of lignite briquettes, which before the start of the procedure by means of a
  • Moistening device is moistened to a water content of about 30%, continuously from top to bottom in the direction of gravity four zones in one
  • Drying zone in which the wet or humidified brown coal is dried by rising hot vapors and gases
  • a second zone in which the dried lignite with a high stoichiometric deficit (e.g.
  • Pyrolysis gas is pyrolyzed, a third zone (flame zone) and a fourth zone
  • substantially oxygen-free means that 0.5% by volume or less of oxygen is contained in the gas atmosphere.
  • Substantially stoichiometric oxygenation based on the organic and metal-containing compounds means that no more than about 5% by weight of these compounds, based on the product of charring, i. the
  • a temperature of about 450 ° C to about 900 ° C preferably from about 500 ° C to about 550 ° C.
  • the temperature of lignite residues in the flame zone is less than 600 ° C, while the flames have the usual flame temperature of more than 1000 ° C.
  • the glow zone has a temperature of about 500 ° C to about 600 ° C, which is slightly below the combustion temperature of carbon on. With lignite having a variable water content, the temperature in the drying and pyrolysis zone can be controlled by controlling the air supply to maintain the required pyrolysis temperature.
  • the moist or humidified brown coal in the drying zone also serves as adsorbent for longer-chain hydrocarbons and any sulfur-containing gases that are generated in the underlying pyrolysis zone and evaporate upwards. As the lignite migrates down into the pyrolysis zone, the longer-chain hydrocarbons are then further pyroylzed.
  • pyrolysis gas which is mainly carbon monoxide (CO), carbon dioxide (C0 2 ), nitrogen (N 2 ), methane (CH 4 ), hydrogen (H 2 ), short-chain hydrocarbons and optionally sulfur-containing gases, such as H 2 S, COS, CS 2 , contains.
  • Very stable organic compounds such as highly condensed aromatics, are burned in the flame zone and glow region (incandescent zone) to C0 2, H 2 0 and, optionally, S0 2 or charred and metals are at least partially oxidized.
  • sulfur-containing gases such as H 2 S, COS and / or CS 2 are formed in appreciable quantities, they can be removed in a conventional manner, for example by means of desulfurization filters, from the gas leaving the reactor. Possibly contained S0 2 can also be removed by conventional methods, eg by lime washing.
  • WO 2010/124761 discloses a further development of the device and the method.
  • Fig. 1 shows such a conversion device 100, which is for continuous
  • Supply area 104 and a wall 108 which define an interior space 106, and a grid forming a bottom 1 10 and one on a lid 1 12 of the
  • the rotary valve 1 16 allows for the environment substantially gas-tight loading of the interior 106th
  • a gas outlet 1 18 is disposed on the lid 1 12, which is in communication with the interior 106 in the supply area 104.
  • a downwardly tapering funnel 120 is connected with its funnel wall 122 with the interior 106.
  • an air supply 134 e.g. in the form of a pipe.
  • a further downwardly leading pipe section 130 is connected.
  • the pipe section 130 opens into another
  • Rotary valve 136 which serves as a discharge device.
  • Supports 138 two of which are visible in Fig. 1, support the conversion device 100. The entire
  • Conversion device 100 or at least the wall 108 and the lid or are thermally insulated.
  • the insulation reduces or prevents the condensation of gases generated in the interior space 106 on the inside of the wall 108.
  • the conversion device 100 may further be followed by a fluid distribution device.
  • the fluid distribution device may be integrally formed in the conversion device.
  • the fluid distribution device has a mixing device arranged in a mixing device and a
  • Moistening device comprises.
  • the mixing device as a mixer or scrambled eggs.
  • the mixer can be arranged below the reactor space in a mixing chamber.
  • the interior 106 has four zones: a first upper zone (drying zone) 140 in
  • Supply area 104 in which the brown coal 102 is dried by rising warm vapors and gases 144 in the supply area 104.
  • a second zone (pyrolysis zone) 142 in which the dry brown coal is pyrolyzed with a large deficit or practical absence of oxygen to form pyrolysis gas.
  • the adjoining third zone 144 is a flame zone in which remaining organic compounds burn at the air flowing from below through the air supply 134.
  • a lowermost zone 146 which is a glow zone in which the temperature is regulated by incoming air through the controlled air supply 134 to a temperature of 500-600 ° C and in which the last organic products present in the lignite are carbon, leaving essentially carbon or a carbon concentrate 158, which is so friable that it falls through the grid 1 10.
  • the carbon 158 falls through the pressure of the overlying and continuously advancing brewing coal 102 as well as by gravity due to the grid 110 therethrough. Openings of the grate 1 10 are made adjustable, so that the coal size or the flow rate of the charcoal 102 and the carbon 158 is controlled by the size of the openings.
  • the carbon 158 falls due to gravity through the hopper 120, and the pipe section 130 in the other rotary valve 136, which discharges the carbon 158.
  • the carbon 158 can be sprayed / moistened and mixed with water by means of spray nozzles arranged in the walls or in the ceiling of the mixing chamber.
  • the fluid distribution device may allow a defined supply of water into the carbon 158, so that less any evaporating water, a desired suitable water content of, for example, 15 to 25%, in particular from 18 to 20%, can be achieved in the carbon concentrate.
  • the air supply 134 in the pipeline 130 shown in FIG. 1 controls the supply of air or oxygen into the interior space 106.
  • the convection-generated gas flow upwards in the supply area 104 draws ambient air through the opened air supply 134 and through the pipeline 130 and Funnel 120 up in the
  • gas outlet 118 is provided with a fan or the like, the pressure conditions in the upper region of the inner space 106 by the speed of the
  • Interior space 106 preferably in the upper region close to the rotary valve 116 via a correspondingly suitable sensor device which generates a control signal.
  • a control signal e.g. a negative pressure
  • FIG. 2 shows a reactor battery 200 for the continuous conversion of lignite.
  • the reactor battery 200 here comprises seven by six individual reactors, hereinafter referred to as cells 202, which are arranged in a cuboid.
  • the reactor battery is surrounded by a common reactor outer wall 204.
  • six transverse and five longitudinal dividing walls 206 extend within the outer walls 204 of the reactor.
  • All cells 202 are supplied with lignite continuously, as schematically indicated by the arrow 208 in FIG.
  • Lignite from a brown coal storage is about to pipes a rotary valve (not shown) and from there via distribution pipes (not shown) to the individual cells passed.
  • a teilpyrolytician conversion arise in the cells in addition to non-combustible and flammable gases with high calorific value, such as methane, carbon monoxide and hydrogen, and solid conversion product, namely carbon.
  • the gases are removed at the top of each cell, as indicated schematically by arrow 210 in FIG. 2, and are collected via pipes (not shown), compressed and stored or else used thermally (combustion).
  • the solid conversion product directs headers 212 below each cell, if necessary
  • the reactor outer wall 204 is thermally insulated with rockwool or other suitable insulating material. Within the reactor battery wall, heat exchange takes place through the transverse and partition walls 206. The cells 202, however, remain materially isolated from each other. This causes lower heat losses compared to thermally decoupled cells. Each cell 202 is provided with a controllable / adjustable air supply
  • FIG. 3 shows a reactor battery 300 according to the invention which, like the reactor battery 200 shown in FIG. 2, comprises a plurality of reactors, which are referred to below as cells 302.
  • the cells 302 are each provided with their own cell wall 304a, 304b. Between cell walls 304b of juxtaposed cells 302, a schematic distance is visible in Fig. 2, but in fact does not have to be present.
  • the cells are as close to each other as possible to allow good heat exchange between the cells 302.
  • external cells are at their outer
  • Cells walls 304a thermally insulated, 304b not on their inner cell walls.
  • a honeycomb honeycomb structure can improve the thermal properties (smaller outer surface).
  • two conversion regions are distinguishable.
  • the flame region 306 which comprises a flame zone and a glowing zone
  • lignite is charred in the case of substoichiometric oxygen supply to carbon.
  • the resulting hot gases rise up the supply area 308th Die hot gases even contain little or no oxygen, since this is almost used up during charring.
  • these hot gases cause drying, degassing and pyrolytic or partially pyrolytic conversion of lignite to combustible gases at temperatures of 500 to 900 ° C.
  • This gas essentially comprises hydrogen, carbon monoxide, methane, short-chain hydrocarbons, carbon dioxide, nitrogen and possibly sulfur-containing gases which are removed.
  • the pyrolysis shifts slightly towards a gasification, whereby more combustible gas can arise.
  • the heat required to dry the lignite can lower the temperature below the temperature necessary for pyrolysis.
  • the dehumidification or drying can be controlled by controlling the air supply, so that the process for lignite with variable
  • Water content is adjustable.
  • the control of the pyrolysis is carried out by regular, controllable or adjustable air supply lines (arrows 310) or gas outlets in each cell.
  • the cell walls 304b thereby prevent uncontrolled combustion channels 212 between the cells 302. If the cells 302 of the reactor battery 300 were combined into a single large combustion chamber, air from the air supply 310 of one cell and air from an adjacent air supply 310 could flow to a location in that large combustion chamber and form local combustion channels 312 in which lignite would burn completely, essentially producing only combustible and non-combustible gases but no more carbon and disrupting the process. Controlled partial pyrolytic decomposition would not be possible.
  • a grid 314 supports the reaction material, ie the lignite.
  • air is supplied through a feeder tube 310, for example, centrally to a respective single cell 302.
  • the amount of air is precisely controlled and z. B. regulated by the temperature of an exhaust stream.
  • charring of the brown coal or charring thereof occurs with substoichiometric oxygen supply.
  • the relative lack of oxygen due to throttled air supply leads to combustion (or Partial combustion) of the volatiles of the reaction material while the solid carbon in the form of carbon concentrate falls down through the grid 314 out of the cell.
  • the now largely oxygen-free reaction gas which mainly contains nitrogen and C0 2 , leaves the oxygen zone upwards at a temperature of about 500 to 600 ° C.
  • Brown coal which reaches this area on their way from above contains virtually no more water. It is heated under these conditions and gas is expelled pyrolytically. This rises further up and can be led out of the cell 302 led into a cogeneration plant or the like and the
  • the conversion device 100 and the cells 302 can be designed as containers or in container form, for example as overseas freight containers.
  • Several such containers can form a container battery.
  • the containers are easily transportable by conventional means and can be assembled on site to form a container battery.
  • the containers can be erected upright or transversely and connected to one another via a suitably suitable connecting means or connection, for example a framework, a flu, T-beam, screws, welded joints, etc.
  • Overseas containers are typically sea freight containers and ISO containers designed with 20- and 40-foot length and 8-foot width. Such overseas containers are not only ideal for transport on container ships, but also for transport by truck or rail.
  • Conversion devices in container form these easily accessible hard coal deposits can be transported, for example, in China, Russia or Canada. Also, the operation, replacement and maintenance of such Complete system of a conversion device in container form is easier.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Materials Engineering (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)

Abstract

L'invention concerne un procédé de production de carbone et de gaz combustibles à partir de lignite humide ou de lignite sec humidifié au début du processus, lequel procédé consiste à faire passer le lignite en continu de haut en bas dans le sens de la force de gravité à travers quatre zones dans un lit mouvant dans un réacteur approprié : une première zone, ou zone de séchage, dans laquelle le lignite humide ou humidifié est séché par des vapeurs et des gaz devenant de plus en plus chauds ; une deuxième zone, ou zone de pyrolyse, dans laquelle le lignite séché est soumis à une pyrolyse à un fort déficit stoechiométrique en oxygène, de préférence d'au moins 98 %, entraînant le dégagement d'un gaz de pyrolyse ; une troisième zone, ou zone de flamme, et une quatrième zone, ou zone de luminescence, qui forment ensemble une zone d'incandescence dans laquelle les composés organiques et contenant du métal restants sont oxydés et/ou brûlés/gazéifiés par un apport d'oxygène sensiblement stoechiométrique, le résidu non brûlé contenant du carbone sensiblement pur, à au moins environ 98 %, qui est prélevé en continu.
PCT/EP2012/000669 2011-02-17 2012-02-15 Production de carbone et de gaz combustibles à partir de lignite WO2012110236A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN201280009211.0A CN103517969A (zh) 2011-02-17 2012-02-15 由褐煤来生产碳和可燃气体
EP12704699.3A EP2675872A1 (fr) 2011-02-17 2012-02-15 Production de carbone et de gaz combustibles à partir de lignite

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011011521A DE102011011521A1 (de) 2009-12-29 2011-02-17 Erzeugung von Kohlenstoff und brennbaren Gasen aus Braunkohle
DE102011011521.8 2011-02-17

Publications (1)

Publication Number Publication Date
WO2012110236A1 true WO2012110236A1 (fr) 2012-08-23

Family

ID=45688426

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2012/000669 WO2012110236A1 (fr) 2011-02-17 2012-02-15 Production de carbone et de gaz combustibles à partir de lignite

Country Status (3)

Country Link
EP (1) EP2675872A1 (fr)
CN (1) CN103517969A (fr)
WO (1) WO2012110236A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013220501A1 (de) 2013-10-11 2015-04-16 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Kohle-Pyrolyse
DE102013221075A1 (de) 2013-10-17 2015-04-23 Technische Universität Bergakademie Freiberg Verfahren zur Kohletrocknung und Pyrolyse

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB679095A (en) * 1950-05-02 1952-09-10 Metallgesellschaft Ag Method of and apparatus for effecting thermal processes with finely granular or pulverulent carbonaceous substances with the production of active carbon
DE2747571A1 (de) * 1976-10-26 1978-04-27 Union Steel South Africa Verfahren zum kontinuierlichen erzeugen eines reduktionsgases und vorrichtung zum durchfuehren des verfahrens
GB2035366A (en) * 1978-10-16 1980-06-18 Schwarze Pumpe Gas Veb Treating brown coal or lignite
US4306506A (en) * 1980-06-02 1981-12-22 Energy Recovery Research Group, Inc. Gasification apparatus
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
DE102005038135B3 (de) 2005-08-11 2007-03-08 Schottdorf, Bernd, Dr. Vorrichtung und Verfahren zur kontinuierlichen Herstellung von Holzkohle
DE102007062414A1 (de) * 2007-12-20 2009-07-02 Conera Process Solutions Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
WO2010124761A1 (fr) 2009-04-27 2010-11-04 European Charcoal Ag Dispositif, son utilisation, procédé et système pour la transformation en continu d'une biomasse

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101636473A (zh) * 2007-02-16 2010-01-27 考奇碳与燃烧私人有限公司 干燥和气化方法
US9170019B2 (en) * 2008-08-30 2015-10-27 Dall Energy Holdings ApS Method and system for production of a clean hot gas based on solid fuels

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB679095A (en) * 1950-05-02 1952-09-10 Metallgesellschaft Ag Method of and apparatus for effecting thermal processes with finely granular or pulverulent carbonaceous substances with the production of active carbon
DE2747571A1 (de) * 1976-10-26 1978-04-27 Union Steel South Africa Verfahren zum kontinuierlichen erzeugen eines reduktionsgases und vorrichtung zum durchfuehren des verfahrens
GB2035366A (en) * 1978-10-16 1980-06-18 Schwarze Pumpe Gas Veb Treating brown coal or lignite
US4306506A (en) * 1980-06-02 1981-12-22 Energy Recovery Research Group, Inc. Gasification apparatus
EP1201731A1 (fr) * 2000-10-26 2002-05-02 RWE Rheinbraun Aktiengesellschaft Procédé de gazéification en lit fluidisé de solides contenant du carbone et installation de gazéification
DE102005038135B3 (de) 2005-08-11 2007-03-08 Schottdorf, Bernd, Dr. Vorrichtung und Verfahren zur kontinuierlichen Herstellung von Holzkohle
DE102007062414A1 (de) * 2007-12-20 2009-07-02 Conera Process Solutions Gmbh Autothermes Verfahren zur kontinuierlichen Vergasung von kohlenstoffreichen Substanzen
WO2010124761A1 (fr) 2009-04-27 2010-11-04 European Charcoal Ag Dispositif, son utilisation, procédé et système pour la transformation en continu d'une biomasse

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102013220501A1 (de) 2013-10-11 2015-04-16 Technische Universität Bergakademie Freiberg Verfahren und Vorrichtung zur Kohle-Pyrolyse
DE102013221075A1 (de) 2013-10-17 2015-04-23 Technische Universität Bergakademie Freiberg Verfahren zur Kohletrocknung und Pyrolyse

Also Published As

Publication number Publication date
CN103517969A (zh) 2014-01-15
EP2675872A1 (fr) 2013-12-25

Similar Documents

Publication Publication Date Title
CH615215A5 (fr)
WO2010003968A2 (fr) Procédé et dispositif pour produire du gaz de synthèse à faible teneur en goudrons à partir de biomasse
EP2563881B1 (fr) Procédé pour la gazéification de la biomasse
AT519471B1 (de) Verkohlungsanlage
EP2663742B1 (fr) Procédé et installation permettant la récupération d'énergie à partir de la biomasse et des déchets combustibles, en particulier des matières premières renouvelables, ainsi que leur carbonisation
EP2343349A1 (fr) Installation de fabrication de bois torréfié, charbon de bois, goudron de bois, vinaigre de bois et gaz de synthèse
DE102014003806A1 (de) Anlage und Verfahren zur Direktpyrolyse von Biomasse
DE102011011521A1 (de) Erzeugung von Kohlenstoff und brennbaren Gasen aus Braunkohle
EP2675872A1 (fr) Production de carbone et de gaz combustibles à partir de lignite
EP1377649B1 (fr) Installation et procede pour produire de l'energie par pyrolyse
AT512361B1 (de) Thermochemische Holzvergasungsanlage mit Festbettreaktor mit doppelt aufsteigender Gegenstromvergasung, Gasreinigung, Gasbereitstellung, Schadstoffverwertung und Schadstoffentsorgung für den Dauerbetrieb mit Gas-Kolbenmotoren und Gasturbinen
DE102007017859A1 (de) Vergaser
EP0271477A1 (fr) Dispositif pour le dégazage et la gazéification de combustible solide
EP3067407B1 (fr) Système et méthode pour la gazéification de matière carbonée
DE102016008289A1 (de) Vorrichtung und Verfahren zur allothermen Festbettvergasung von kohlenstoffhaltigem Material
DE102015215143B4 (de) Verfahren und Vorrichtung zur Schwachgaserzeugung durch thermochemische partielle Oxydation fester Biomasse
DE102007036514A1 (de) Verfahren und Vorrichtung zur Erzeugung eines Synthesegases aus einem biogenen Stoff
EP2771437A1 (fr) Procédé de fonctionnement d'un réacteur à gazéification
DE102013112995A1 (de) Verfahren zum Aufheizen eines Brennstoffbettes in einem Festbettdruckvergasungsreaktor
DD251043A3 (de) Verfahren zur herstellung von aktivkohle
DE102010044437A1 (de) Verfahren zur thermischen Behandlung organischer Ausgangsstoffe oder eines Gemisches organischer und anorganischer Ausgangsstoffe sowie Vorrichtung dazu
DE2608559B2 (de) Verfahren und Reaktor zur unter Gaserzeugung bewirkter Verbrennung organischer Brennstoffe
DE2526947A1 (de) Verfahren und vorrichtung zum herstellen von brenngas
DE3220126A1 (de) Verfahren und anlage zur gewinnung von generatorgas aus fossilen brennstoffen
EP2851410A1 (fr) Installation de gazéification de biomasse

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 12704699

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

REEP Request for entry into the european phase

Ref document number: 2012704699

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2012704699

Country of ref document: EP