EP0955350B1 - Dispositif et méthode pour la gazéification de bois - Google Patents

Dispositif et méthode pour la gazéification de bois Download PDF

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Publication number
EP0955350B1
EP0955350B1 EP98830256A EP98830256A EP0955350B1 EP 0955350 B1 EP0955350 B1 EP 0955350B1 EP 98830256 A EP98830256 A EP 98830256A EP 98830256 A EP98830256 A EP 98830256A EP 0955350 B1 EP0955350 B1 EP 0955350B1
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EP
European Patent Office
Prior art keywords
inner casing
diaphragm
zone
reactor
lower section
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Expired - Lifetime
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EP98830256A
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German (de)
English (en)
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EP0955350A1 (fr
Inventor
Marco Spegni
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Mase Generators SpA
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Mase Generators SpA
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Priority to EP98830256A priority Critical patent/EP0955350B1/fr
Priority to DE69816033T priority patent/DE69816033T2/de
Priority to AT98830256T priority patent/ATE244289T1/de
Publication of EP0955350A1 publication Critical patent/EP0955350A1/fr
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Publication of EP0955350B1 publication Critical patent/EP0955350B1/fr
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    • 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
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/485—Entrained flow gasifiers
    • C10J3/487—Swirling or cyclonic gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C10K1/024—Dust removal by filtration
    • 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
    • C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
    • 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
    • C10J2300/0916—Biomass
    • C10J2300/092—Wood, cellulose
    • 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
    • C10J2300/12—Heating the gasifier
    • C10J2300/1246—Heating the gasifier by external or indirect heating

Definitions

  • the present invention relates to a device for the gasification of wood and, in general, is part of the technology of apparatuses by means of which a solid fuel, in this case a biomass consisting of wood, is only partially oxidised in order to obtain a combustible gas.
  • a solid fuel in this case a biomass consisting of wood
  • the gasification of a wooden biomass is a thermochemical process based on the partial oxidation of vegetable carbon and the breakdown of the products deriving from the thermal decomposition of the biomasses, including the decomposition of the water absorbed by the original biomass and that of formation. This reaction is followed by reduction of the carbon dioxide on a bed of incandescent pure carbon automatically generated by the previous reaction.
  • the above-mentioned reactions occur under conditions of thermal equilibrium, with a production of heat sufficient to allow the thermochemical process to supply its own energy, without the aid of external energy sources.
  • the set of reactions which break down the biomass into simple elements of the pyroligneous derivatives is that characteristic of wood chemistry, although the quantity varies according to the type and characteristics of the biomass gasified.
  • the device forming the subject-matter of the present invention comprises, in particular, a reactor in which the above-mentioned gasification process which, to summarise, envisages the drying, pyrolisis, carbonisation and gasification of the solid wooden biomass, is effected according to a procedure generally known as the "Imbert process".
  • This type of process envisages the use of a vertical gasification device in which the wood, fed in continuously from the top of the device, gradually moves towards the base, undergoing said gasification with concurrent flow; that is to say, in which the gaseous flow of the products of the reaction, of the water vapour, of the fuel, and finally of the comburent atmospheric air, all follow the direction from top to bottom.
  • the device is of the type comprising vertical outer walls, a head and a base which together form a long tank with a vertical longitudinal axis; a heating zone inside the tank, near the base, this zone being surrounded by lower portions of the walls of said tank; a plurality of comburent air conveyor elements, located in the oxidation zone and in fluid communication with an external air source, so that the air can be transferred from the air source to the oxidation zone; a discharge zone for the gas produced by the reactor, normally called the neck, located below the conveyor elements and having a hole that allows the discharge of the gas to the outside of the tank.
  • the main disadvantage of such types of wood gasification devices is the high content of dust and tar transported by the gas, which, downstream of the reactor, require expensive and not completely effective filtration plants, envisaged to make the gas suitable for use in internal combustion engines.
  • the tar content produced in the gasifier device reactor is in inverse proportion to the local oxidation-reduction reaction temperatures.
  • the comburent air conveyor elements are distributed over the walls of the reactor in such a way that they lie on a horizontal plane and are all oriented so as to direct the air conveyed by each of them exactly to a central point of the heating zone.
  • the discharge zone has a twin truncated cone structure, in which the smaller bases of the two truncated cones are opposite one another and are joined at a narrow central zone, in which the discharge hole or neck is located.
  • the nozzles Due to the high temperatures of the gas (1000 - 1400 °C); the high chemical reactivity of the gas; its strong abrasive action caused by the speed and the large amount of dust transported, the nozzles are made of special, high-alloy steels, which are stainless and resistant to high temperatures.
  • the reactor operating temperature is limited, in use, to the maximum temperature sustainable by the nozzle and the materials of which the reactor core is made.
  • the reactor core therefore, constitutes a critical element for further raising the reactor general operating temperatures and requires complex construction solutions that are expensive to maintain, since despite the careful selection of construction materials, the reactor is subject to rapid deterioration of its mechanical characteristics, thus requiring necessary and frequent stopping of the gasifier plant in which the reactor is installed and complex reactor part substitutions.
  • both documents CH-A-227948 and US-A-4459136 show an apparatus for dryng, pyrolizing and also gasifying of wood comprising an outer container, an inner casing having an upper cylindrical section and a reactor zone presenting an oxidation zone and a discharge zone.
  • the discharge zone presenting a diaphragm, a discharge hole in which pass a gaseous fluid and a plurality of fluid conveyor elements to supply flow of air.
  • a part of the solid particles rests on the diaphragm while the gaseous flow bringing some solid particles pass through the discharge hole.
  • Document FR-A-901589 shows a device of the type above disclosed but it does not show a diaphragm to ,mantain the solid particles and the fluid conveyor elements.
  • an apparatus for driyng, pyrolizing and also gasifying wood comprising an outer container, an inner casing having an upper cylindrical section and a reactor zone presenting an oxidation zone and a discharge zone.
  • the discharge zone presenting a discharge hole in which pass a gaseous fluid and a plurality or fluid conveyor elements to supply flow of air and directed in the upper portion of the oxidation zone. It is to be noted that in this document the solid particles fall with the gaseosus flow through the discharge hole and rest on the surface of the bottom of the outer container.
  • the aim of the present invention is to overcome the above-mentioned disadvantages, allowing the creation of gasifier devices in which the relative reactors are able to operate without disadvantages at operating temperatures that are higher than those that can currently be reached and substantially uniform in a manner that was impossible using conventional plant.
  • a gasifier device comprising a reactor in which the fluid conveyor elements or comburent conveyor nozzles are oriented in such a way that a flow of air is sent to the oxidation zone, said flow of air imparting to the gaseous mixtures and reagents produced in the reactor a rotary motion about the longitudinal axis of the gasifier, in addition to the conventional forward motion, towards the discharge zone or neck, directed parallel with said longitudinal axis.
  • the reactor reaction zone also comprises a diaphragm held crossways by the reactor walls, said diaphragm having a discharge hole.
  • the diaphragm delimits a duct with a through-section whose shape varies suddenly, creating a situation in which the dynamics of the gases in transit are similar to those of the cyclone effect.
  • the gas drawn by the flow of air sent by the conveyor elements moves forwards, turning about the longitudinal axis and, at the moment in which it is intercepted by the diaphragm and forced to pass through the discharge hole or neck with smaller diameter, is subjected to a violent acceleration that separates the solid particles which it transports, causing them to be deposited on the vertical walls of the reactor and on the surface of the diaphragm.
  • the solid particles settle in a funnel shape and coat the walls of the diaphragm and the connecting zone between the diaphragm and the inner walls of the reactor with refractory material as far as the nozzles.
  • the coating consisting of ash, of which the surface is in a melted paste state, is deposited, drips and is continuously regenerated during the turbulent gasification process, thus protecting the metal walls of the reactor from heat and, lacking cohesion, from mechanical stress.
  • the gasifier device is also equipped with heat exchangers with fins which, applied to the outer wall of the inner container or tank, allow partial recovery of the heat energy carried by the exiting gas and containment of its temperature, improving the energy equilibrium of the gasification reaction by raising the general tank temperatures, raising the oxidation-reduction temperatures and drying the wood which, therefore, does not have to be pretreated outside the gasifier device.
  • the top of the gasifier device is fitted with a head vapour condenser, which allows any excess humidity in the raw wooden biomass to be condensed and extracted.
  • Raising of the reactor operating temperatures and the reduction of the risk of cold veins in the reagent gases allows maximised breaking of the heavy chains deriving from the tar and pyroligneous oils into light, volatile chains, comprising gaseous hydrocarbon fractions and into simple carbon and hydrogen elements.
  • the present invention also provides a gasification method implemented by the device equipped with the reactor made according to the present invention.
  • Figure 1 illustrates a gasifier device, labelled as a whole with the numeral 1, envisaged for the production of combustible gas from a wooden biomass, by means of a thermochemical process based on the partial oxidation of vegetable carbon and the thermal decomposition of the pyroligneous compounds deriving from the thermal decomposition of the biomasses, and also relative to the decomposition of the water absorbed by the original biomass and that of formation.
  • the device 1 comprises a long, cylindrical outer container 2, substantially vertical, with a vertical outer side wall 3, a head 5 and base 6, connected to one another.
  • the outer container 2 houses a tubular inner casing 4.
  • the inner casing 4 is mounted within the outer container 2 at a distance designed to delimit a gap 17 between them, and they are positioned axial to one another on a shared vertical, longitudinal axis 2a.
  • the outer container 2 is basically cylindrical.
  • the inner casing 4 is made of stainless steel, resistant to high temperatures and the chemical action of the process gases and has two cylindrical end sections 4a and 4b, with different diameters, joined to one another by an intermediate truncated cone portion or hopper 4c, which connects the upper cylindrical section 4a with larger diameter, to the lower cylindrical section 4b with smaller diameter.
  • the inner casing 4 houses a biomass oxidation zone 7, at the lower cylindrical section 4b of the casing 4 and equipped with a plurality of fluid conveyor elements or nozzles 8 and a zone 9 for discharge of the gas towards the outside of the casing 4.
  • the conveyor elements 8 ( Figure 2) comprise a set of nozzles which: are distributed over the wall of the lower cylindrical section 4b; are coplanar with one another and located on a basically horizontal plane; and are connected with a ring-shaped chamber 10 that encompasses the lower cylindrical section 4b of the inner casing 4.
  • the ring-shaped chamber 10 is connected to an external air source 21 (schematically illustrated in the figures) by a connector 11, so that the air is transferred from the source 21 into the oxidation zone 7 by the nozzles 8.
  • the unit comprising the lower cylinder 4b, ring-shaped chamber 10 and nozzles 8, constitutes the so-called reactor 22.
  • the conveyor elements 8 are oriented on the wall of the lower cylindrical section 4b in such a way that they respectively direct the flow of air 8f conveyed by each of them tangentially to a horizontal circle 12 centred on the longitudinal axis 2a (see also Figure 7).
  • the discharge zone 9, located below the conveyor elements 8, comprises a flat, ring-shaped diaphragm 13, through the centre of which there is a cylindrical discharge hole 14 (Figure 4).
  • the diaphragm 13 is supported crossways by the lower cylindrical section 4b of the inner casing 4 and, approximately half way down the casing, by means of a ring-shaped washer 15 ( Figures 5 and 6), which connects the diaphragm 13 to the wall of the lower cylindrical section 4b.
  • the flow of fuel air 8f fed into the oxidation zone 7 imparts to the gaseous flow 8g in which the gases and solid particles generated in the gasification process flow together, a rotation about the longitudinal axis 2a.
  • the reactor 22 Since the reactor 22 is of the type with concurrent flow, as it rotates, the gaseous flow 8g simultaneously moves along the longitudinal axis 2a of the lower cylinder 4b, towards the discharge zone 9 below.
  • the above-mentioned elements diaphragm 13, washer 15 and walls of the lower cylindrical section 4b together form a transit duct, whose through-section is suddenly reduced at the discharge hole 14.
  • the flow of gases 8g is intercepted by the diaphragm 13 and washer 15, undergoing a modification in its fluid dynamics, which creates a fluid stagnation in the zones of the transit duct closest to the connecting zone between the diaphragm 13 and the inner wall of the casing 4.
  • the solid particles transported by the gaseous flow 8g are, therefore, deposited on the diaphragm 13, on the washer 15 and on the vertical inner wall of the lower cylindrical section 4b of the reactor 22, gradually coating them with a mass 16 of particles ( Figure 9) which are deposited and accumulate in controlled, regular shapes, which in the case illustrated in the figure are represented by truncated cones set opposite one another.
  • the masses 16 of particles deposited on the vertical inner wall of the lower cylindrical section 4b constitute, as indicated above, a mass 16 with the shape of a funnel of particles, in a melted paste state on the surface, and basically comprise ash and coal dust.
  • the diaphragm 13, washer 15 and hole 9 assembly is followed by a further portion of the lower cylindrical section 4b, which forces the gases to make contact for longer periods with the reducing carbon masses which fill the gap 17.
  • the masses 16 of ash also form downstream of the diaphragm 13, following the sudden widening of the cross-section encountered by the gaseous flow that exits the discharge hole 14 below the diaphragm 13.
  • the masses 16 of ash located below the diaphragm 13 also remain stably in position during continuous operation of the reactor 22.
  • the increase in and homogeneous distribution of the temperatures is allowed, on one hand, by an increased heat resistant capacity of the walls of the lower cylinder 4b and diaphragm 13, and on the other hand, by reduced heat dispersion from the oxidation zone 7 to the outside of the container 2.
  • the above description refers to tubular nozzles; however, many alternative embodiments are possible, with equivalent functions.
  • conveyor elements 8 may comprise simple holes 8', which in the example illustrated are round, made in the wall of the lower cylindrical section 4b of the inner casing 4 and oriented in such a way that they are offset according to angles ⁇ designed to direct the flow of air 8f eccentrically relative to the longitudinal axis 2a of the container 2.
  • the outer container 2 is fitted with a heat exchanger 18 to recover at least part of the heat carried by the gases that flow out of the inner casing 4.
  • the heat exchanger 18 (see also Figure 3) comprises a plurality of flat, rectangular fins 19, attached vertically to the innermost casing 4 of the device 1.
  • the fins 19 are distributed evenly along the outer edge of the inner casing 4 and project into the gap 17, protruding radially towards the outermost casing 3.
  • the gases that flow out of the inner casing 4 through the discharge hole 14 are caused to rise up through the gap 17 from the base 6 to the head 5.
  • the gases touch the fins 19 and, cooling, give up part of their heat which, through the wall of the upper cylindrical section 4a of the inner casing 4, is transferred to the biomass still to be treated, that in the meantime is moving downwards inside the inner casing 4 and proceeds from the head 5 to the base 6, gradually being dried and subjected to a carbonisation pre-treatment.
  • the heat exchanger 18 allows not only the advantage of recovering heat useful to the thermal equilibrium of the process, but also heats the biomass stored in the upper cylindrical section 4a of the inner casing 4, promoting its drying, the formation of water vapour that enters the general concurrent flow of treated compounds and, finally, allowing an advantageous reduction in the temperature of the gases exiting the reactor 22.
  • the head 5 of the device 1 is fitted with a vapour condenser 20, which allows the adjustable separation and elimination of any excess humidity in the biomass.
  • the device 1 envisages the insertion of the wooden biomass to be treated in the upper cylindrical section 4a, through the head 5.
  • the biomass therefore, constitutes a column of layered material, which gradually descends along the axis 2a of the inner casing 4 and, during this movement, is dried at the top of the upper cylindrical section 4a, carbonised at the bottom of the cylindrical section 4a and of the truncated cone connector or hopper 4c and, finally gasified at the lower cylindrical section 4b of the inner casing 4.
  • the size of the biomass is gradually reduced, so that the product exiting the lower cylindrical section 4b is represented only by the gases and the ash generated in the partial combustion and by the fragments of pure carbon with a smaller cross-section than the discharge zone 9 of the diaphragm 13.
  • Part of the ash is deposited on the base 6 of the outer container 2, from which it is extracted using conventional extraction means, not illustrated.
  • the ash which remains suspended in the gas is eliminated by means of a battery of filters, again not illustrated, as they do not form part of the present invention, located downstream of the device. Finally, the gases exiting the battery of filters are sent on for use, for example, to fuel internal combustion engines that drive generators.
  • the invention thus designed allows full achievement of the aim of economically obtaining, with reduced running costs, a gas from which the dust and tar have been removed to a degree suited to the construction specifications of conventional engines for the generation of electrical or mechanical energy.
  • the device with the relative reactor operating in accordance with the method described is more adaptable to the chemical-physical characteristics of wood, with increased operating flexibility of the gasification device.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Processing Of Solid Wastes (AREA)
  • Chemical And Physical Treatments For Wood And The Like (AREA)

Claims (7)

  1. Un dispositif pour la gazéification de bois, comprenant une cuve extérieure (2), un corps intérieur (4), ayant tous deux un axe longitudinal vertical (2a), une tête (5) et une base (6), ledit corps intérieur ayant une section supérieure cylindrique (4a), une trémie (4c) et une section inférieure (4b) ; une zone d'oxydation (7) étant située à l'intérieur de la section inférieure (4b) du corps intérieur (4) à proximité de la base (6) ; une pluralité d'éléments (8, 8') d'acheminement de fluide étant disposés au niveau de la zone d'oxydation (7) et en communication de fluide avec une source d'air externe (21) de sorte que l'air puisse être transféré de la source d'air (21) à la zone d'oxydation (7), lesdits éléments d'acheminement de fluide (8, 8') étant orientés de manière à envoyer dans la zone d'oxydation (7) un flux d'air (8f) qui génère un flux gazeux (8g) contenant les gaz générés, ladite zone inférieure (4b) et ladite zone d'oxydation définissant un réacteur (22) ; une zone (9) pour l'évacuation du gaz produit par le réacteur (22) étant située en dessous des éléments d'acheminement (8, 8') et présentant un trou (14) pour l'évacuation du gaz à l'extérieur du corps intérieur (4) ; ladite zone d'évacuation (9) comprenant une membrane (13) fixée à la section inférieure (4b) du corps intérieur (4) transversalement à l'axe longitudinal (2a) et présentant le trou d'évacuation (14) en question, la membrane (13) délimitant, avec les parois intérieures de la section inférieure (4b), un conduit de transit pour le flux gazeux (8g) ayant une section qui varie brusquement, dans lequel le flux gazeux (8g) est intercepté par la membrane (13) et dévié vers le trou d'évacuation (14), ladite interception entraínant le flux gazeux (8g) à libérer des particules solides qui s'accumulent sur la membrane (13) et les parois intérieures verticales adjacentes de ladite section (4b) et y restent, les isolant au moins partiellement contre la chaleur et les protégeant d'un contact direct avec le flux gazeux (8g) successif qui passe à travers le conduit de transit et le trou d'évacuation (14) ; ledit dispositif étant caractérisé en ce que lesdits éléments d'acheminement comprennent des tubes (8) orientés tangentiellement à un cercle commun (12) pour faire tourner le flux gazeux (8g) autour de l'axe longitudinal (2a) et le faire avancer en même temps vers la zone d'évacuation (9) parallèlement à l'axe longitudinal (2a).
  2. Le dispositif selon la revendication 1, caractérisé en ce que lesdits éléments d'acheminement comprennent des lumières (8') réalisées dans les parois de la section (4b) du corps intérieur (4).
  3. Le dispositif selon la revendication 1, caractérisé en ce que lesdits éléments d'acheminement (8, 8') et ledit cercle (12) sont coplanaires.
  4. Le dispositif selon la revendication 1, caractérisé en ce que ladite section inférieure (4b) a la forme d'un tube cylindrique et comprend une membrane (13) supportée par une bague plate (15), cette dernière étant supportée transversalement à l'axe longitudinal (2a) par les parois intérieures de la section inférieure (4b) du corps intérieur (4).
  5. Le dispositif selon la revendication 1, caractérisé en ce que ledit corps intérieur (4) et ladite cuve extérieure (2) sont montés coaxialement l'un par rapport à l'autre et séparés de manière à délimiter ensemble un espace (17), ledit espace (17) étant parcouru par le flux gazeux (8g) qui s'écoule hors du trou d'évacuation (14).
  6. Le dispositif selon la revendication 5, caractérisé en ce que ledit espace (17) est pourvu d'ailettes (19) d'échange de chaleur fixées au corps intérieur (4).
  7. Une méthode pour la gazéification de bois comprenant les phases suivantes :
    introduction d'une biomasse de bois à traiter dans une section cylindrique supérieure (4a) d'un dispositif (1) qui comprend une cuve extérieure (2), un corps intérieur (4), ayant tous deux un axe longitudinal vertical (2a), une tête (5) et une base (6), ledit corps intérieur présentant la section cylindrique supérieure (4a) en question, une trémie (4c) et une section inférieure (4b) ; une zone d'oxydation (7) étant située à l'intérieur de la section inférieure (4b) du corps intérieur (4) à proximité de la base (6) ; une pluralité d'éléments d'acheminement de fluide (8, 8') orientés tangentiellement à un cercle commun (12) étant disposés au niveau de la zone d'oxydation (7) et en communication de fluide avec une source d'air externe (21) de sorte que l'air puisse être transféré de la source d'air (21) à la zone d'oxydation (7), ladite section inférieure (4b) et ladite zone d'oxydation définissant un réacteur (22) ; une zone (9) pour l'évacuation du gaz produit par le réacteur (22) étant située en dessous des éléments d'acheminement (8, 8') susmentionnés et présentant un trou (14) pour l'évacuation du gaz à l'extérieur du corps intérieur (4) ;
    séchage de la biomasse de bois dans la partie haute de la section cylindrique supérieure (4a) ;
    carbonisation de la biomasse de bois séchée dans la partie basse de la section cylindrique (4a) ; et
    gazéification de la biomasse de bois carbonisée au niveau de la section cylindrique inférieure (4b) du corps intérieur (4) ;
    ladite méthode étant caractérisée en ce que ladite phase de gazéification de la biomasse de bois comprend les phases suivantes :
    impression au flux gazeux (8g) contenant les gaz générés par le réacteur (22) d'un mouvement de rotation autour de l'axe longitudinal (2a) et d'un mouvement d'avancement simultané vers une zone d'évacuation (9) vers l'extérieur du corps intérieur (4) ;
    interception du flux (8g) par une membrane (13) orientée transversalement à l'axe longitudinal (2a) et conformée de manière à constituer, avec les parois intérieures adjacentes de la section inférieure (4b), un conduit de transit ayant une section qui varie brusquement, dans lequel le flux (8g) est intercepté par cette même membrane (13) et brusquement dévié vers un trou d'évacuation (14), ladite phase d'interception entraínant la libération de particules solides qui s'accumulent sur la membrane (13) et les parois intérieures verticales (4) de la section inférieure (4b), les recouvrant au moins partiellement de manière à les isoler thermiquement et à éviter que le flux gazeux (8g) ne vienne en contact direct avec la membrane (13) et les parois (4) de la section inférieure (4b).
EP98830256A 1998-04-28 1998-04-28 Dispositif et méthode pour la gazéification de bois Expired - Lifetime EP0955350B1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP98830256A EP0955350B1 (fr) 1998-04-28 1998-04-28 Dispositif et méthode pour la gazéification de bois
DE69816033T DE69816033T2 (de) 1998-04-28 1998-04-28 Vorrichtung und Methode zur Vergasung von Holz
AT98830256T ATE244289T1 (de) 1998-04-28 1998-04-28 Vorrichtung und methode zur vergasung von holz

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP98830256A EP0955350B1 (fr) 1998-04-28 1998-04-28 Dispositif et méthode pour la gazéification de bois

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EP0955350A1 EP0955350A1 (fr) 1999-11-10
EP0955350B1 true EP0955350B1 (fr) 2003-07-02

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EP98830256A Expired - Lifetime EP0955350B1 (fr) 1998-04-28 1998-04-28 Dispositif et méthode pour la gazéification de bois

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AT (1) ATE244289T1 (fr)
DE (1) DE69816033T2 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008043131A1 (de) 2008-10-23 2010-04-29 Burkhardt Gmbh Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004020919B4 (de) * 2004-04-28 2009-12-31 Kbi International Ltd. Reaktor zur thermischen Abfallbehandlung mit Eindüsungsmitteln
DE102007002895B4 (de) 2006-01-20 2021-08-26 Uwe Athmann Vorrichtung zur Holzvergasung
DE102009012501B4 (de) * 2008-03-12 2012-05-24 Alfred Heine Reaktor für eine Holzvergaseranlage und Verfahren zum Betreiben des Reaktors

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CH227948A (de) * 1941-10-25 1943-07-31 Isliker Albert Gasgenerator für feste Brennstoffe.
FR901589A (fr) * 1942-07-09 1945-07-31 Gazogène à tirage renversé
CH237348A (de) * 1943-08-07 1945-04-30 Porsche Kg Gaserzeuger.
DE3131476C2 (de) * 1981-08-08 1983-12-22 Fritz Werner Industrie-Ausrüstungen GmbH, 6222 Geisenheim Holzgasgenerator
NL8900939A (nl) * 1989-04-14 1990-11-01 Eduard Thomas Jacobus Van Der Gasgenerator.

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102008043131A1 (de) 2008-10-23 2010-04-29 Burkhardt Gmbh Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe
DE102008043131B4 (de) * 2008-10-23 2012-09-20 Burkhardt Gmbh Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe

Also Published As

Publication number Publication date
ATE244289T1 (de) 2003-07-15
EP0955350A1 (fr) 1999-11-10
DE69816033T2 (de) 2004-06-03
DE69816033D1 (de) 2003-08-07

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