WO2010046222A2 - Procédé et dispositif pour la gazéification thermochimique de combustibles solides - Google Patents

Procédé et dispositif pour la gazéification thermochimique de combustibles solides Download PDF

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Publication number
WO2010046222A2
WO2010046222A2 PCT/EP2009/062807 EP2009062807W WO2010046222A2 WO 2010046222 A2 WO2010046222 A2 WO 2010046222A2 EP 2009062807 W EP2009062807 W EP 2009062807W WO 2010046222 A2 WO2010046222 A2 WO 2010046222A2
Authority
WO
WIPO (PCT)
Prior art keywords
gasification
fuel
medium
zone
carburetor
Prior art date
Application number
PCT/EP2009/062807
Other languages
German (de)
English (en)
Other versions
WO2010046222A3 (fr
Inventor
Klaus Weichselbaum
Original Assignee
Burkhardt Gmbh
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Burkhardt Gmbh filed Critical Burkhardt Gmbh
Priority to EP09783675.3A priority Critical patent/EP2356200B1/fr
Publication of WO2010046222A2 publication Critical patent/WO2010046222A2/fr
Publication of WO2010046222A3 publication Critical patent/WO2010046222A3/fr
Priority to HRP20180376TT priority patent/HRP20180376T1/hr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • C10J3/30—Fuel charging devices
    • 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
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • 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
    • C10J3/50—Fuel charging devices
    • C10J3/503—Fuel charging devices for gasifiers with stationary fluidised bed
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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

Definitions

  • the present invention relates to a one-step process for the thermochemical gasification of solid fuels according to the principle of an ascending DC gasification.
  • the fuel is supplied to a gasification chamber against the force of gravity and flows through in the same direction by a gasification medium and an emerging product gas.
  • a corresponding gasifier for the thermochemical gasification of solid fuels has a gasification chamber and a fuel supply, which supplies the fuel against gravity to the gasification chamber and a supply for a gasification medium in the gasification chamber.
  • the carburetor has a top side arranged on the gasification chamber outlet for a product gas.
  • thermochemical gasification has been known for a long time in the prior art, and in connection with regenerative power generation and waste and waste disposal, a great potential has been seen in gasification for quite some time. Nevertheless, no such method has been able to establish itself on the market in large numbers until now.
  • Descending DC gasifiers have been operated in large numbers in the form of the Imbert carburetor and similar equipment during World War II, and are being used in this or slightly modified form for most of the smaller carburetor installations since they provide a low-tar gas. They are characterized in that the fuel sinks by gravity down and the carburetor from the gasification agent and product gas is also flowed through in this direction. They require coarse-grained fuel with a relatively narrow particle size distribution, otherwise the downstream reduction zone will be "clogged" by fines and thus become insufficiently permeable to the product gas fuel gas contaminated with a high tar content is produced.
  • the object of the present invention is to provide a gasification process and a device which, with simple plant technology, enable the production of a low-tarry product gas.
  • a fuel is supplied to a gasification chamber contrary to gravity and flows through a gasification medium and a product gas formed in the same direction.
  • Suitable fuels are all carbonaceous solids such as biomass, sewage sludge, plastics and the like.
  • a gasification space is provided, a fuel supply, which supplies the fuel against gravity to the gasification space and a supply for a gasification medium.
  • an outlet for a product gas is furthermore arranged.
  • the fuel is fed to the gasification chamber continuously or at least quasi-continuously, that the gasification medium through the supplied fuel is fed through a layer forming oxidation tion zone and in this case the amount of the supplied gasification medium is adjusted by a control unit such that in a reduction zone above the oxidation zone, a stationary fluidized bed is formed.
  • the fuel supply is here preferably designed to be adjustable for continuous or quasi-continuous fuel supply.
  • the feed for the gasification medium is arranged below reaction zones which form in a layered manner in the gasification space in order to achieve a uniform flow through the pyrolysis, oxidation and reduction zone, which is formed substantially homogeneously.
  • the fuel in the gasification chamber is conveyed substantially homogeneously from bottom to top through the gasification space and flows through the gasification medium from below.
  • the fuel itself forms a distributor plate for producing a stationary fluidized bed.
  • the supplied amount of the gasification medium is in this case controllable by a control unit such that in the lower regions of the carburetor in the fuel supply and the pyrolysis zone is a fixed bed, in the overhead reduction zone, however, can form a fluidized bed.
  • This is made possible by the increase in volume of the gasification medium flowing through as a result of the strong rise in temperature in the oxidation zone and by the pyrolysis and combustion gases which form.
  • the fuel as a distributor plate or the corresponding supply of the gasification medium, a stable over a wide range of air volume fluidized bed can be generated.
  • a substantially improved implementation of the pyrolysis coke formed in the oxidation zone in gas and fly ash is possible. Due to the uniform ge flow through the pyrolysis, oxidation and reduction zone in this case a comparatively tarerarmes gas can be generated, with a very uniform quality of the gas can be achieved by the continuous fuel supply and the almost complete implementation of the pyrolysis coke.
  • the inventive method or the gasifier according to the invention thus operates on the basic principle of an ascending DC gasification, which is combined with an integrated fluidized bed.
  • the reduction zone above the oxidation zone is completely formed as a stationary fluidized bed.
  • the implementation of the fuel or the pyrolysis coke can be done in a favorable manner and in a short time.
  • the fuel in the gasification space is loosened contactless and mixed.
  • the loosening and mixing of the fuel is not actively mixing, but only passively, by continuously sufficient free-flowing, fresh fuel is supplied. Due to the uniform flow through the reaction zones and the introduction of the gasification medium from below through the fuel through the mixing and loosening is further supported.
  • the fuel is thereby kept constantly in motion, whereby a channel and bridging in the fuel can be avoided.
  • Devices for conveying and / or mixing the fuel are in this case arranged exclusively outside the gasification space, so that there are no components in the temperature-loaded zones of the gasification space.
  • the carburetor according to the invention can thereby trouble-free operated and is exposed to little wear.
  • the structural complexity of such a carburetor is low.
  • additional mixing devices can also be used.
  • the method is preferably carried out in such a way that the fuel in the oxidation zone is burned from top to bottom at a substantially constant speed. This can be achieved by a corresponding continuous supply of the gasification medium, so that forms a layered oxidation zone at a constant ratio of the supply of the gasification medium and the fuel.
  • a pellet-shaped fuel is used as fuel, preferably wood pellets are used.
  • wood pellets are used.
  • the homogeneity and flowability of pelletized fuels enables a relatively simple carburetor design using simple conveyor technology and thus leads to cost-effective overall systems.
  • the extra cost over non-pelleted fuels is more than offset.
  • chips of small grain size are equally conceivable and suitable.
  • the gasification medium is supplied together with the fuel and flows successively through a pyrolysis zone, the oxidation zone and the reduction zone.
  • the feed for the gasification medium is preferably formed together with the fuel supply.
  • the gasifier is operable with different power.
  • the fuel is conveyed through the gasification space with the speed decreasing towards the top.
  • the gasification chamber has an upwardly widening cross-section. This ensures that the fuel is passed through the carburetor with the speed decreasing at the top. As a result, adaptation to the processes taking place at different speeds in the individual reaction zones is possible in a favorable manner.
  • the position of the oxidation zone in the gasification chamber always adjusts itself at the point where the combustion rate and the feed rate coincide.
  • a particularly advantageous embodiment of the invention provides that an ash discharge device is formed only by the outlet for the product gas and the exiting product gas.
  • the resulting ash is discharged in this case completely by the exiting product gas. Due to the upper burnup and the almost complete material conversion, no further discharge devices for the ash are required.
  • the gasification chamber is surrounded by an insulation, preferably of ceramic fibers. give.
  • the thermal load of the carburetor outer wall can be reduced thereby.
  • the gasification medium and / or the fuel are preheated.
  • Part of the required process heat can thus be introduced into the process from the outside.
  • the required process heat can also be completely autothermal by means of substoichiometric combustion of a part of the fuel.
  • a feed for superheated steam and / or air is arranged in the region of the reduction zone.
  • the reduction of the oxidation products can thereby be favorably influenced and the gas composition adapted to the requirements.
  • At least one temperature sensor is arranged in the gasification space, which monitors the fill level of the gasification space.
  • a plurality of sensors are arranged in the gasification space, which detect the position of the forming reaction zones, in particular the oxidation zone. Since in the method according to the invention or in the device according to the invention, the individual reaction zones develop very homogeneously and in layers, they have clear temperature differences. The position of the reaction zones and the filling level in the gasification space can thereby be detected simply, cost-effectively and without the arrangement of moving parts by means of temperature sensors.
  • a wall of the gasification chamber is made of a conventional steel. Due to the uniform flow through the reaction zones and the high material conversion in the fluidized bed can be generated in the apparatus according to the invention a tarerarmes product gas at relatively low temperatures of about 850 ° C maximum. In the area of high temperatures, a redu- decorating atmosphere. The structural complexity of the carburetor can thus be kept low by using a conventional steel. Special refractory lining, high temperature resistant steels or ceramics are not required.
  • the ash discharged with the product gas is separated from the product gas by means of a separation device. This can be accomplished by simple means, such as a cyclone separator.
  • Figure 1 shows an embodiment of a carburetor according to the invention in a schematic vertical section and a schematic representation of the method according to the invention
  • Figure 2 is a schematic representation of the method according to the invention, wherein the reduction zone is in the form of a fluidized bed.
  • the carburetor 1 has a fuel supply 2 in the carburetor bottom with a delivery unit 5 for the fuel.
  • a gasification chamber 3 is arranged, which has a variable cross-section in the example shown.
  • the gasification chamber 3 is frusto-conical and separated from the outer Vergaserwandung by an insulation 4.
  • a gas collecting chamber 12 is formed, in which the resulting gases 14 are collected and withdrawn through the outlet 7 arranged on the top side of the gasification chamber 3. Furthermore, the carburetor 1 has a feed 6 for a Verga- sungsmedium 16, which is in operative connection with a control unit 15.
  • the control unit 15 controls the amount of the gasification medium 16 supplied in such a way that a fluidized bed 17 is automatically formed without mechanical distributor bottoms in the gasification space and without additional fluidizing means.
  • FIG. 1 shows a carburetor 1, in which the feed 6 for the gasification medium 16 is formed together with the feed 2 for the fuel 8.
  • the fuel 8 flows through from below from the gasification medium 16, so that the mixing of the fuel 8 is supported and a uniform distribution of the gasification medium 16 over the entire cross section is ensured.
  • the supply of the gasification medium 16 can also, as shown in FIG. 2, take place laterally below the pyrolysis zone 9 through an annular nozzle. Again, however, there is the supply of the gasification medium 16 through the fuel 8 therethrough, to thereby achieve a thorough mixing of the fuel 8 and uniform distribution of the gasification medium 16. Additional mechanical mixing devices are therefore not required. In addition, it can be prevented that fines from the overhead reaction zones 9, 10, 1 1 get back into the fuel 8.
  • the fuel 8 against the force of gravity continuously or quasi-continuously, that is, the same amount of fuel per unit time, pressed by the fuel supply 2 into the gasification chamber 3 and funded by the carburetor.
  • the fuel 8 in this case flows through the gasification medium 16 and product gas 14 in the same direction. It is therefore in this respect an ascending DC gasification.
  • a gasification medium 16 is advantageously used preheated air.
  • the process can also be completely autothermic.
  • the combustion of the fuel 8 takes place from top to bottom, with a layer-shaped oxidation zone 10 is formed at a suitable constant ratio of air supply to fuel.
  • temperatures of about 800 ° C is formed below the same also a layered pyrolysis zone 9, in which decomposes the fuel 8 at temperatures around 500 ° C in pyrolysis and gaseous compounds.
  • the gas-air mixture formed in the pyrolysis zone 9 by the air 16 flowing through the fuel 8 from below through the fuel 8 maintains the energy production in the oxidation zone 10, where a part of these gases and the pyrolysis coke burns.
  • the remaining pyrolysis coke formed in the pyrolysis zone 9 gradually migrates upwards through the oxidation zone 10 and forms a reduction zone 11 over it.
  • the illustration of FIG. 2 shows a process in which the reduction zone 11 is formed essentially completely in the form of a fluidized bed 17.
  • FIG. 1 a method according to FIG. 1 is also possible, wherein the reduction zone 11 above the oxidation zone 10 is initially formed in a layered form. In the upper region of the gasification space, however, the reduction zone 11 is present as a fluidized bed 17. In each case, the gasification is carried out according to the principle of an ascending DC gasification, which, however, according to the invention is combined with an integrated fluidized bed 17 in the reduction zone 11.
  • the pyrolysis coke is flowed through, inter alia, by CO 2 and H 2 O from the pyrolysis zone 9 and the oxidation zone 10, these being reduced endothermically to the combustible gases CO and H 2 , as a result of which the pyrolysis coke is gasified.
  • the resulting gas pressure causes the pyrolysis coke to be raised and thereby loosened. It forms according to the invention by the appropriate adjustment of the supplied amount of the gasification medium 16 and the flow of the fuel 8 from below an equilibrium between the gas pressure and the weight of the pyrolysis coke up to the fluidized bed.
  • the fuel 8 forms a distributor plate for fluidized bed production through its continuous delivery with appropriate control of the supply of the gasification medium 16.
  • the fluidized bed 17 can be produced without further fluidizing agent. This makes it possible to almost completely convert the pyrolysis coke formed in the oxidation zone 10 to gas and fly ash and thus to achieve a high degree of efficiency of the overall process. It has been shown that the fluidized bed 17 is stable in the carburetor 1 according to the invention over a relatively wide range of air volumes and thus the regulation of the amount of air through the control unit 15 to the necessary for the thermochemical gasification air rates is easily possible.
  • the resulting ash is preferably discharged as fly ash without additional discharge devices with the process gas 14 and then separated from the product gas 14 by simple means, for example by a cyclone separator. Due to the upper burnup in the inventive method and the leadership of the gasification medium 16th As well as the product gas 14 through the carburetor 1 and the good implementation of the fuel 8, the product gas 14 with the outlet 7 as discharge devices for the ashes is completely sufficient. If, however, excess pyrolysis coke is produced or intentionally generated, this can likewise be taken off together with the resulting dusty ash with the product gas 14.
  • the uniform flow through the very homogeneously forming pyrolysis, oxidation and reduction zones 9, 10, 1 1 leads to the production of a tarry gas of very uniform quality at comparatively low temperatures of about 850 ° C. in the oxidation zone 10 it is possible to carry out a carburettor 1 according to the invention without the use of special high-temperature-resistant steels or ceramics. Even conventional structural steel can be used, since no significant oxidation takes place due to the reducing atmosphere of the substoichiometric combustion. The avoidance of the usual in the prior art ceramic components also leads due to low heat capacity advantageously short heating and cooling times when starting and stopping inventive carburetor. 1
  • a preferred embodiment of a carburettor 1 according to the invention has, as shown in the example, an upwardly widening cross-section of the gasification space 3. This allows operation with different performance, because it causes the fuel 8 to move upwards through the gasifier 1 with decreasing speed.
  • the firing to be carried out in the oxidation zone 10 at a substantially constant speed now leads to a self-regulating setting of a stable operating point at which the oxidation zone 10 remains at the point where the rate of burnup and feed rate of the fuel 8 coincide.
  • the continuous or quasi-continuous supply of new fuel 8 in particular in connection with the changing cross-section of the gasification chamber 3, ensures a constant movement and thorough mixing of the material and thus prevents the formation of channels and bridges in the oxidation and reduction zone 10, 11 without any further mechanical devices.
  • a plurality of superposed temperature sensors 13 is further arranged, which cooperate with the control unit 15 and the level of the gasification chamber 3 and the position of the reaction zones (9, 10, 1 1) detect by measurement.
  • the boundaries between the fuel 8 and the pyrolysis and oxidation zone (9, 10) and between the reduction zone (1 1) and the gas collecting space above (12) are due to the very homogeneous formation in the inventive method and the carburetor 1 according to the invention characterized by significant temperature differences.
  • the control technology important position of the reaction zones 9, 10, 1 1, in particular the oxidation zone 10, and the filling level can thus be detected in a simple manner cost and without moving parts.
  • an inventive carburetor 1 manages without moving parts in the hot area and has no mechanically loaded hot parts, which often constitute a source of interference in the prior art.
  • the carburetor 1 according to the invention finds by self-regulating properties with low mechanical and / or electronic control effort a stable operating point and thus provides a durable tarerarmes product gas with only slightly fluctuating quality. Channel and bridge formation as well as tar slippage can be avoided.
  • the gasifier 1 according to the invention is therefore particularly suitable for small and medium-sized systems up to about 1 MW electrically, since no complex gas aftertreatment is required. It is also possible to directly produce a motorable product gas. Furthermore is by means of the device according to the invention with appropriate process control and the production of charcoal possible.
  • the fuel 8 used need not be coarse and may contain high amounts of fines, since a tendency to clog is avoided by the inventive device and process control. Thus, fuels 8 which are available in sufficient quantity on the market can be used.
  • the carburetor 1 according to the invention can also be manufactured and operated cost-effectively.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Processing Of Solid Wastes (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)
  • Treatment Of Sludge (AREA)
  • Gasification And Melting Of Waste (AREA)

Abstract

L'invention porte sur un procédé en une étape pour la gazéification thermochimique de combustibles solides (8), utilisant le principe de la gazéification à co-courant ascendant. Dans ce procédé, on amène un combustible (8), contre la force de gravité, dans un compartiment de gazéification (3), on mélange un fluide de gazéification (16) au combustible à co-courant, et on évacue à co-courant un produit gazeux (14) qui se forme. Le combustible (8) est amené en continu au compartiment de gazéification (3), et le fluide de gazéification (16) est amené par en bas, en traversant le combustible ainsi amené (8), à une zone d'oxydation (10) à structure stratifiée. La quantité du fluide de gazéification amené (16) est alors ajustée à l'aide d'une unité de régulation (15), de telle sorte qu'il se forme un lit fluidisé stationnaire (17) dans une zone de réduction (11) au-dessus de la zone d'oxydation (10). Dans un gazéificateur correspondant (1), l'amenée (2) du combustible est réalisée de façon à amener en continu ou d'une manière quasi-continue le combustible, et l'amenée (16) destinée au fluide de gazéification (16) est disposée au-dessous de zones de réaction (9, 10, 11), qui doivent prendre une structure stratifiée dans le compartiment de gazéification (3). Le combustible (8) forme alors un fond de soufflage pour le fluide de gazéification (16), pour réaliser un lit fluidisé (17).
PCT/EP2009/062807 2008-10-23 2009-10-02 Procédé et dispositif pour la gazéification thermochimique de combustibles solides WO2010046222A2 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
EP09783675.3A EP2356200B1 (fr) 2008-10-23 2009-10-02 Procédé pour la gazéification thermochimique de combustibles solides
HRP20180376TT HRP20180376T1 (hr) 2008-10-23 2018-03-02 Postupak za termokemijsko rasplinjavanje krutih goriva

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008043131.1 2008-10-23
DE102008043131A DE102008043131B4 (de) 2008-10-23 2008-10-23 Verfahren und Vorrichtung zum thermochemischen Vergasen fester Brennstoffe

Publications (2)

Publication Number Publication Date
WO2010046222A2 true WO2010046222A2 (fr) 2010-04-29
WO2010046222A3 WO2010046222A3 (fr) 2010-07-22

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Country Status (4)

Country Link
EP (1) EP2356200B1 (fr)
DE (1) DE102008043131B4 (fr)
HR (1) HRP20180376T1 (fr)
WO (1) WO2010046222A2 (fr)

Cited By (3)

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Publication number Priority date Publication date Assignee Title
US8546636B1 (en) 2013-01-28 2013-10-01 PHG Energy, LLC Method for gasifying feedstock
US8721748B1 (en) 2013-01-28 2014-05-13 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
EP2886190A1 (fr) 2013-12-18 2015-06-24 Syncraft Engineering GmbH Procédé et dispositif destinés au déchargement d'impuretés

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DE102009047445A1 (de) 2009-12-03 2011-06-09 Burkhardt Gmbh Anlage zum Erzeugen eines Produktgases aus organischen Einsatzstoffen
ES2662406T3 (es) 2015-04-30 2018-04-06 Ws-Wärmeprozesstechnik Gmbh Procedimiento y dispositivo para la gasificación de biomasa
EP3309240A1 (fr) 2016-10-12 2018-04-18 WS-Wärmeprozesstechnik GmbH Procédé et dispositif de gazéification de biomasse
CN115261074B (zh) * 2022-07-29 2023-04-11 赣州市怡辰宏焰能源科技有限公司 一种带水箱塔式炉排气化炉

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EP0531778A1 (fr) * 1991-08-23 1993-03-17 Poretti- Gaggini Sa Gazéificateur à équicourant
WO1997001617A1 (fr) * 1995-06-27 1997-01-16 Ver Verwertung Und Entsorgung Von Reststoffen Gmbh Procede et dispositif permettant de produire du gaz combustible

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8546636B1 (en) 2013-01-28 2013-10-01 PHG Energy, LLC Method for gasifying feedstock
US8721748B1 (en) 2013-01-28 2014-05-13 PHG Energy, LLC Device with dilated oxidation zone for gasifying feedstock
US8829262B2 (en) 2013-01-28 2014-09-09 PHG Energy, LLC Method for gasifying feedstock
EP2886190A1 (fr) 2013-12-18 2015-06-24 Syncraft Engineering GmbH Procédé et dispositif destinés au déchargement d'impuretés

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DE102008043131A1 (de) 2010-04-29
EP2356200A2 (fr) 2011-08-17
DE102008043131B4 (de) 2012-09-20
EP2356200B1 (fr) 2017-12-27
WO2010046222A3 (fr) 2010-07-22
HRP20180376T1 (hr) 2018-04-20

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