EP0239589B1 - Vergaser mit hohem durchfluss für biomasse bei schwacher gasgeschwindigkeit - Google Patents

Vergaser mit hohem durchfluss für biomasse bei schwacher gasgeschwindigkeit Download PDF

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Publication number
EP0239589B1
EP0239589B1 EP19860905659 EP86905659A EP0239589B1 EP 0239589 B1 EP0239589 B1 EP 0239589B1 EP 19860905659 EP19860905659 EP 19860905659 EP 86905659 A EP86905659 A EP 86905659A EP 0239589 B1 EP0239589 B1 EP 0239589B1
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EP
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Prior art keywords
bed
gasifier
entrained
gas
sand
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EP19860905659
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English (en)
French (fr)
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EP0239589A1 (de
Inventor
Herman F. Feldmann
Mark A. Paisley
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Battelle Development Corp
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Battelle Development Corp
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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
    • C10J3/46—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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C10J3/12—Continuous processes using solid heat-carriers
    • 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
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • 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
    • 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
    • C10J2300/09—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
    • 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
    • C10J2300/0973—Water
    • 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
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
    • C10J2300/1637—Char combustion
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
    • 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
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1853—Steam reforming, i.e. injection of steam only

Definitions

  • This invention relates to gasifiers for entrained bed combustors particularly as applied to biomass gasification for the production of a medium Joule (Btu) grade fuel gas from a variety of biomass forms including shredded bark, wood chips, sawdust, sludges and other carbonaceous fuels or feedstocks.
  • a medium Joule (Btu) grade fuel gas from a variety of biomass forms including shredded bark, wood chips, sawdust, sludges and other carbonaceous fuels or feedstocks.
  • the process system according to this invention relates to production of gas by use of a high throughput gasifier employing hot sand circulation for process heat.
  • the exothermic combustion reactions can be separated from the endothermic gasification reactions.
  • the exothermic combustion reactions can take place in or near the combustor while the endothermic gasification reactions take place in the gasifier. This separation of endothermic and exothermic processes results in a high energy density product gas without the nitrogen dilution present in conventional air-blown gasification systems.
  • the present invention relates to a novel method of operating a gasifier preferably for a parallel entrained bed pyrolysis unit, i.e., a system comprising an endothermic reaction zone distinct from the exothermic reaction zone of the combustor wherein the heat from the exothermic zone is transferred to the endothermic reaction zone by circulation of an inert particulate solid such as sand.
  • a gasifier preferably for a parallel entrained bed pyrolysis unit, i.e., a system comprising an endothermic reaction zone distinct from the exothermic reaction zone of the combustor wherein the heat from the exothermic zone is transferred to the endothermic reaction zone by circulation of an inert particulate solid such as sand.
  • W So is the specific sand throughput and determines the fluid-bed cross sectional area required to achieve the total sand feed rate which in turn is related to the wood rate by the heat balance.
  • the expression for the residence time in terms of the above parameters is given by
  • the present invention is able to gasify 9800 kg/m 2- h (2000 Ibs/ft 2- hr) and even exceed 22000 kg/m 2- h (4500 Ib/ft 2- hr) through a unit of 25 cm (10 inch) (0.83 ft) diameter and length of 67 cm (22 feet). Further, the operation is smooth and without any evidence of slugging.
  • the present invention is a radical departure from the teachings and conventional wisdom of the prior art.
  • Bailie U.S. Patent 3,853,498 describes a process involving separate gasification and combustion zones.
  • both zones are conventional fluid-bed reactors.
  • Published wood throughput values for the Bailie process typically do not exceed 585 kg/m 2- h (120 Ibs/ft 2- hr). Fluidization would occur typically with inlet gas velocities of 30-90 cm/s (1-3 ft/sec) to provide good fluidization.
  • transfer of circulating sand is by direct flow from fluid-bed to fluid-bed rather than by entrainment and exit out the top of the reaction vessel.
  • Squires U.S. Patent 4,032,305 discloses another circulating bed gasifier for coal and coke gasification known as a "fast fluid-bed".
  • the fast fluid-bed can operate in a two-zone configuration of an exothermic combustion zone and an endothermic gasification zone.
  • Squires states that the minimum velocity to achieve a circulating fast fluid-bed is a little more than 1,8 m/s (6 ft/sec) with particles having an average diameter of 60 microns.
  • Squires prefers operating with particles no larger than 250 microns.
  • the present invention uses particles typically of 20-1000 and preferably 300-800 microns. Scaling the 1,8 m/s (6 ft/sec) minimum velocity recommended by Squires based on finer particles to the coarser particles of this invention, one would estimate a minimum velocity of 9,15 m/s (30 ft/sec) would be required to achieve fast fluid-bed conditions.
  • the gasifier according to the present invention operates in the entrained mode but at inlet gas velocities below and wood throughputs that are well beyond what would be expected based on a knowledge of the prior art. In spite of the fact that the system operates at inlet velocities typical of fluid-beds, the reactor operates in the entrained mode.
  • This invention comprises the unexpected discovery that it is possible to gasify biomass at very high wood throughputs but in an entrained gasifier operating at low inlet gas velocities.
  • Entrainment rates in order to operate in an entrained mode depended to lesser or greater degrees on a large number of complexly interrelated variables including particle size, density, uniformity of particles, column diameter, baffling, bed depth, but primarily it was believed on high inlet gas velocity.
  • the gasifier according to our invention is basically a reactor with a fluid-bed of sand at the reactor base operated at wood feed rates sufficiently high to generate enough product gas to circulate sand and gasified char by entrainment.
  • the gasifier is essentially a hybrid with an entrained zone above a fluidized bed gasifier.
  • the annular shaped gasifier vessel has a conventional gas distribution plate near the bottom and there it has openings for biomass feedstock entry, inert material circulation or recirculation, and fluidizing gas inletting.
  • the reaction vessel has an exit at or near the top leading to a separator from which product gas is discharged and solids are recycled to the bottom of the gasifier or preferably recycled via an exothermic combustor to reheat the inert material.
  • the biomass gasifier operates with a recirculating particulate phase and at inlet gas velocities in the range required to fluidize the sand or other recirculating particulate phase.
  • a velocity of 24 ⁇ 61 cm/s (0.8 to 2 ft/sec) with a 0,3-0,85 mm (20x50 mesh) sand has allowed smooth stable operation.
  • Velocities of 15 ⁇ 215 cm/s (0.5 to 7 ft/sec) can be used.
  • the biomass gasifier operates at wood feed rates that exceed 15650 kg/m 2- h (3000 lbs/hr) of dry biomass (per square foot) of reactor cross sectional area. Throughputs of 21500 kg/m 2- h (4400 Ibs-ft2/hr) are achievable and possibly even higher.
  • the inlet for wood feed and recirculating sand is located at the base of the reactor in the neighborhood of the gas distributor.
  • the gasifier additionally has provision for removal of the circulating particulate phase and char by entrainment. For example, separation of the particulate phase, such as sand and char from the product gas, can be accomplished by conventional cyclone(s).
  • the low inlet gas velocity high throughput biomass gasifier of the present invention operates with biomass throughputs of from 980 (200) and preferably 2450-21500 kg/m 2- h (500-4400 Ib/ft 2- hr) but with inlet gas velocities of 15-215 cm/s (0.5-7 ft/sec). This operating range corresponds approximately with Region IV of the graph.
  • Region I visualizes the operating parameters known to the art for conventional fluidized and entrained beds. Such beds in practice are bounded by a biomass throughput of 9800 kg/m 2- h (2000 Ib/ft 2- hr) and a minimum inlet velocity of 3-3,6 m/s (10-12 ft/sec) up to approximately 9 m/s (30 ft/sec).
  • Region 11 illustrates the operating region of "fast fluid-beds". To achieve the bed density necessary for a fast fluid-bed a minimum solids circulation rate is usually required.
  • Region II includes the transport velocities commonly used in vertical pneumatic conveying of particulate material. This is the typical operating region of entrained systems regardless of the wood throughput.
  • Region III illustrates the operating region of conventional fluid-beds. Such beds do not operate in the entrained mode. Experience at throughputs above 980 kg/m 2- h (200 Ib/ft 2- hr) is unavailable to date for conventional fluid beds.
  • the method of operating a gasifier according to this invention comprises introducing inlet gas at a gas velocity not exceeding 2,1 m/s (7 ft/sec) to fluidize a high average density bed in a gasifier vessel.
  • the high average density bed is formed into a dense fluidized bed in a first space region by means of the inlet gas.
  • the dense fluidized bed contains a circulating first heated relatively fine and inert solid bed particle component.
  • Carbonaceous material is inputted into the first space region with dense fluidized bed at a rate from 980 (200) and preferably 2450-21500 kg/m 2- h (500-4400 Ibs/ft 2- hr) and endothermal pyrolysis of the carbonaceous material is accomplished by means of the circulating heated inert material so as to form a product gas. Contiguous to and above the dense fluidized bed a lower average density entrained space region is formed containing an entrained mixture of inert solid particles, char and carbonaceous material and the product gas.
  • the entrained mixture is then removed from the entrained space region of the gasifier to a separator such as a cyclone wherein the entrained mixture of inert solid particles, char and carbonaceous material is separated from the product gas.
  • a separator such as a cyclone wherein the entrained mixture of inert solid particles, char and carbonaceous material is separated from the product gas.
  • at least the inert solid particles are returned to the first space region after passage through an exothermic reaction zone such as a combustor to first heat the inert particles.
  • an exothermic reaction zone such as a combustor
  • a fluidized bed of heated sand or other relatively inert material at the lower end of the gasifier vessel forms a region of relatively high density.
  • Inputted wood or other carbonaceous material being lighter than the sand, floats on the fluidized sand.
  • an entrained region of sand, char and carbonaceous particles forms in the upper end of the gasifier vessel.
  • the carbonaceous material fed to the gasifier has upwards of 60% of the available carbon converted upon a single pass through the gasifier system.
  • the remainder of the carbon is burned in the combustor to generate heat for the pyrolyses reaction. If other fuel is used in the combustor, then additional carbon can be converted in the gasifier.
  • the inlet air fed to the gasifier typically can be steam, combustion by-product gas, recycled product gas, nitrogen, air or other gas known in the art for yielding specific products.
  • An associated oxygen plant is not required for the gasifier unit operated according to this invention.
  • entrainment of particles to the cyclone is considered deleterious to performance of the system. Loss by entrainment is sought to be avoided or, if unavoidable, minimized as much as possible.
  • a typical fluidized bed is designed such that enough space above the bed is provided to allow lifted particles to settle in the vessel. This space must be provided for in the height of the gasifier vessel and is referred to as transport disengagement height or free board space.
  • the present invention teaches how to use entrainment to beneficial advantage to obtain high carbonaceous feedstock throughput.
  • Commercial advantage of this invention becomes immediately apparent as more throughput means higher production levels through the same or smaller sized equipment, thus a significant reduction in capital costs results from this technology.
  • entrained material exits the vessel near the top of the gasifier to a cyclone or other inertial settling device for separating the product gas from the chart, carbonaceous material and inert material.
  • the system of the present invention is versatile and could be combined with any type of combustor, fluidized, entrained, or non-fluidized, for heating the inert material.
  • the inert material can be heated by passage through an exothermic reaction zone of a combustor to add heat.
  • the inert material is understood to mean relatively inert as compared to the carbonaceous material and could include sand, limestone, and other calcites or oxides such as iron oxide.
  • Some of these "relatively linert materials" actually could participate as reactants or catalytic agents, thus “relatively inert” is used as a comparison to the carbonaceous materials and is not used herein in a strict or pure qualitative chemical sense as commonly applied to the noble gases.
  • limestone is useful as a means for capturing sulfur to reduce sulfate emissions.
  • Limestone might also be useful in catalytic cracking of tar in the gasifier.
  • a process research unit was assembled.
  • the system consisted of a 25,4 cm (10 inch) I.D. gasifier coupled to a 1 m (40 inch) I.D. combustor.
  • the gasifier and all connecting piping was constructed without refractory linings to reduce start-up and cool down time as well as the time required to reach steady state. All the components of a commercial-scale system are included in the PRU allowing the system to be operated in a completely integrated fashion.
  • the PRU combustor is oversized to ensure that the gasifier, which receives all its heat from the circulating entrained solids phase, can be maintained at a temperature sufficient to achieve the desired gasification conversions. Natural gas is added to help balance the large heat losses inherent in a small-scale system.
  • the gasifier reactor is designed to operate up to 870°C (1600°F) and 3,5 kPa (5 psig). Entrained sand and char are separated from the product gas in a disengager and returned to the combustor. Char produced in the gasifier is consumed in the combustor to heat the sand phase.
  • the combustor is a conventional fluid bed designed to operate at 1040°C (1900°F).
  • Typical as-received or partially dried wood chips are charged to a feed hopper.
  • a bed of silica sand is placed in the conventional fluid bed combustor and fluidized with air at a linear velocity of about 45.7 cm/sec (1.5 ft/sec).
  • a startup natural gas burner is ignited. This burner serves as an air heater and is used to preheat the bed to a temperature sufficient to combust char.
  • the startup burner has a total heat input of 290 kw (1 million Btu/hr).
  • the wood feed rate is controlled by four metering screws located below the wood feed hopper. These screws empty into another larger horizontal conveying screw which, in turn, empties into a vertical conveying screw. The wood chips then fall into the gasifier.
  • Adjustments to gas flows or system pressure are made remotely from the control room.
  • the PRU system can be operated at wood feed rates from 23 (50) to in excess of 1134 kg/h (2500 Ib/hr). Larger commercial systems readily achieve significantly higher wood feed rates. Expressed as kg/m 2- h 1 134 kg/h (Ib/ft 2 -hr 2500 Ib/hr) through a circular 25,4 cm (10") LD. gasifier, is the same as 1134 kg/h (2500 Ib/hr) through an area [(nr 2 ) i.e., ⁇ (5/12) 2 ] of 0,0507 m 2 (0.545 sq ft).
  • Design specifications for the PRU system are:
  • start-up of the gasifier for example coupled to a combustor would involve the stages of heat-up and initiation of gasification. These stages could be comprised as follows:
  • the feed gas to the gasifier is switched from air to steam and then, if desired, to recycle product gas.
  • Wood feed is initiated and the wood feed rate gradually increased.
  • char is produced which is transported to the combustor where it is burned to replace the start-up fuel.
  • the feed gas (steam or recycle product gas) to the gasifier is gradually reduced until the system is operating in the range of gas velocities not exceeding 2,1 m/s (7 ft/sec).

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Claims (7)

1. Verfahren zum Betreiben eines Vergasers, dadurch gekennzeichnet, daß ein Eintrittsgas mit einer Gasgeschwindigkeit nicht über 2,1 m pro s (7 ft/sec) zum Fluidisieren eines Bettes in einem Vergaserbehälter eingeleitet wird,
daß das Bett in einem ersten Raumabschnitt mittels des Eintrittsgases zu einem Fließbett ausgebildet wird, wobei das Fließbett eine zirkulierende, heiße, relativ feine und inerte, feste Betteilchenkomponente enthält,
daß kohlenstoffhaltiges Material in den ersten Raumabschnitt mit dem Fließbett in einer Geschwindigkeit von 2450 bis 21500 kg/ml-h (500-4400 Ibs/ft2-hr) eingebracht wird,
daß das kohlenstoffhaltige Material mittels der zirkulierenden, heißen, inerten Teilchenkomponente endotherm pyrolisiert wird, um so ein Produktgas zu bilden,
daß mit Eintritts- und Produktgas anschließend an und oberhalb zum Fließbett ein Raumabschnitt mit geringerer mittlerer Dichte gebildet wird, der eine Mischung von inerten, festen Teilchen, Kohle und kohlenstoffhaltigem Material enthält,
daß schrittweise und kontinuierlich Teile der Mischung und des Eintritts- und Produktgases aus dem Raumabschnitt des Vergasers zu einem Separator entfernt werden,
daß die Mischung vom Eintritts- und Produktgas abgetrennt wird,
daß die inerten, festen Teilchen zur Zufuhr von Wärme durch eine Zone exothermer Reaktion geführt werden und
daß wenigstens die inerten festen Teilchen in den ersten Raumabschnitt rückgeführt werden.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die inerte, feste Bett-Teilchenkomponente Teilchen von einem mittleren Durchmesser von 300 bis 800 um aufweist.
3. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß das kohlenstoffhaltige Material in den ersten Raumabschnitt mit dichtem Fließbett in einer Geschwindigkeit über 14650 kg/m2-h (3000 Ib/ft2-hr) eingebracht wird.
4. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die relativ inerte feste Bett-Teilchenkomponente aus der Gruppe bestehend aus Sand, Kalk, Metalloxyden und Calzit ausgewählt wird.
5. Verfahren nach Anspruch 4, dadurch gekennzeichnet, daß die inerte feste Bett-Teilchenkomponente Teilchen mit einem mittleren Durchmesser von 20 bis 1000 um enthält.
6. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß nach der Trennung der Mischung vom Produktgas die Mischung durch eine Zone mit exothermer Reaktion einer Verbrennungseinrichtung geführt wird.
7. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Trennung der Mischung vom Produktgas unter Verwendung eines Zyklonseparators durchgeführt wird.
EP19860905659 1985-09-20 1986-09-15 Vergaser mit hohem durchfluss für biomasse bei schwacher gasgeschwindigkeit Expired - Lifetime EP0239589B1 (de)

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Application Number Priority Date Filing Date Title
AT86905659T ATE52103T1 (de) 1985-09-20 1986-09-15 Vergaser mit hohem durchfluss fuer biomasse bei schwacher gasgeschwindigkeit.

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Application Number Priority Date Filing Date Title
US77834585A 1985-09-20 1985-09-20
US778345 1985-09-20

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EP0239589A1 EP0239589A1 (de) 1987-10-07
EP0239589B1 true EP0239589B1 (de) 1990-04-18

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EP (1) EP0239589B1 (de)
JP (1) JPH0794669B2 (de)
AU (1) AU591714B2 (de)
CA (1) CA1271634A (de)
DE (1) DE3670507D1 (de)
WO (1) WO1987001719A1 (de)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19736867A1 (de) * 1997-08-25 1999-03-04 Dmt Gmbh Verfahren zur allothermen Vergasung von organischen Stoffen und Stoffgemischen

Families Citing this family (7)

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Publication number Priority date Publication date Assignee Title
HU9201539D0 (en) * 1990-09-11 1992-08-28 Kortec Ag Method and device for gasifying gasifiable materials and/or transforming gas as well as heat exchanger of high temperature for executing said method
NL1016411C2 (nl) * 2000-10-16 2002-04-18 Stichting Energie Werkwijze en inrichting voor het vergassen van biomassa.
AU2003266006A1 (en) * 2002-09-10 2004-04-30 Manufacturing And Technology Conversion International, Inc. Steam reforming process and apparatus
US7763088B2 (en) * 2006-03-24 2010-07-27 Rentech, Inc. Biomass gasification system
NL2000520C2 (nl) 2007-03-05 2008-09-08 Stichting Energie Inrichting voor het vervaardigen van een productgas uit een brandstof, zoals biomassa.
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DE19736867C2 (de) * 1997-08-25 2003-01-16 Montan Tech Gmbh Verfahren zur allothermen Vergasung von organischen Stoffen und Stoffgemischen

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EP0239589A1 (de) 1987-10-07
DE3670507D1 (de) 1990-05-23
AU6400286A (en) 1987-04-07
JPH0794669B2 (ja) 1995-10-11
WO1987001719A1 (en) 1987-03-26
AU591714B2 (en) 1989-12-14
CA1271634A (en) 1990-07-17
JPS63501511A (ja) 1988-06-09

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