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WO1987001719A1 - Gazeificateur de biomasse a faible vitesse du gaz d'admission et a debit eleve - Google Patents

Gazeificateur de biomasse a faible vitesse du gaz d'admission et a debit eleve Download PDF

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Publication number
WO1987001719A1
WO1987001719A1 PCT/US1986/001922 US8601922W WO8701719A1 WO 1987001719 A1 WO1987001719 A1 WO 1987001719A1 US 8601922 W US8601922 W US 8601922W WO 8701719 A1 WO8701719 A1 WO 8701719A1
Authority
WO
WIPO (PCT)
Prior art keywords
bed
gasifier
gas
entrained
sand
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/US1986/001922
Other languages
English (en)
Inventor
Herman F. Feldmann
Mark A. Paisley
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Battelle Development Corp
Original Assignee
Battelle Development Corp
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 Battelle Development Corp filed Critical Battelle Development Corp
Priority to DE8686905659T priority Critical patent/DE3670507D1/de
Priority to AT86905659T priority patent/ATE52103T1/de
Priority to JP61504942A priority patent/JPH0794669B2/ja
Publication of WO1987001719A1 publication Critical patent/WO1987001719A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C10J3/46—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 en ⁇ trained bed combustors particularly as applied to biomass gasification for the production of a medium 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 reac ⁇ tions.
  • the exothermic combustion reactions can take place in or near the combustor while the endothermic gasifi ⁇ cation reactions take place in the gasifier.
  • This separ ⁇ ation 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 en ⁇ trained 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 en ⁇ trained 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.
  • the novelty and unexpectedness of the present invention can be readily ascertained by an examination of existing fluidization design equations and published lit ⁇ erature information on the rates of biomass conversion to gas, particularly as regards the prediction of the design of a conceptual biomass gasifier operating at the con- ditions taught by the present invention.
  • AJJ cross sectional area of the fluid bed, 20 ft 2 .
  • the sand feed rate is given by
  • W S (Ibs/hr) W So (lbs/ft 2 -hr) A B (ft 2 ) .
  • Wso is the specific sand throughput and de ⁇ termines the fluid-bed cross sectional area required to
  • the pres- ent invention is able to gasify 2000 lbs/ft 2 -hr and even exceed 4500 lb/ft 2 -hr through a unit of 10 inch (0.83 ft) diameter and length of 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.
  • 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 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 6 ft/sec minimum velocity recommended by Squires based on finer particles to the coarser particles of this in- vention, one would estimate a minimum velocity of 30 ft/sec would be required to achieve fast fluid-bed conditions. Both entrained and fluidized gasification pres ⁇ ents a variety of advantages including low capital equip ⁇ ment costs, low maintenance, flexibility, ease of control and high conversion efficiency. There are few moving parts thus design and assembly are greatly simplified.
  • 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 en ⁇ trained mode.
  • Figs. 1A, IB, and 1C are sketches of gasifier systems according to the prior art.
  • Fig.2 is a sketch of a gasifier system according to this invention depicted coupled with a typical parallel entrained bed pyrol sis unit.
  • Fig.3 is a graph of biomass throughput via inlet gas velocity. The graph highlights the present inven ⁇ tion's unique capability of operating in the region termed "Region IV" corresponding to high biomass throughput and low inlet gas velocity.
  • Fig. 4 is a sketch of a gasifier useful in the process according to this invention.
  • the depicted cyclone separator can inertially remove entrained solids, thus the gasifier optionally can be coupled to various made combustors including fast fluid, bubbling fluidized, multi-solid fluidized and entrained solid.
  • This invention comprises the unexpected dis ⁇ covery 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 inter ⁇ related varibles including particle size, density, uni- formity of particles, column diameter, baffling, bed depth, but primariy it was believed on high inlet gas velocity.
  • the gasifier according to our invention is ba ⁇ sically 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 at 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 recir ⁇ culating particulate phase and at inlet gas velocities in the range required to fluidize the sand or other re ⁇ circulating particulate phase. For example, a velocity of 0.8 to 2 ft/sec with a 20 x 50 mesh sand has allowed smooth stable operation. Velocities of 0.5 to 7 ft/sec can be used.
  • the biomass gasifier operates at wood feed rates that exceed 3000 lbs/hr of dry biomass per square foot of reactor cross .sectional area. Throughputs of 4400 lbs— ft 2 /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 200 and prefer ⁇ ably 500-4400 lb/ft 2 -hr but with inlet gas velocities of 0.5-7 ft/sec. This operating range corresponds approxi ⁇ mately 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 2000 lb/ft 2 -hr and a minimum inlet velocity of 10-12 ft/sec up to approximately 30 ft/sec.
  • Region II 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 veloc ⁇ ities commonly used in vertical pneumatic conveying of particulate material. This is the typical operating re ⁇ gion of entrained systems regardless of the wood through- put.
  • Region III illustrates the operating region of conventional fluid-beds. Such beds do not operate in the entrained mode. Experience at throughputs above 200 lb/- 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 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 fluid ⁇ ized bed at a rate from 200 and preferably 500-4400 lbs/- ft -hr and endothermal pyrolysis of the carbonaceous ma ⁇ terial 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 gasi ⁇ fier 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.
  • 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 to first heat the inert particles.
  • it can be advan- tageous to route the entire entrained mixture absent prod ⁇ uct gas through the 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 light ⁇ er 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 highest concentration of entrained wood and char would be found at the top of the densely fluidized zone within the gasifier vessel.
  • Entrained hot sand circulates through the entrained wood and char.
  • the carbonaceous particles pyrolyze, they generate gas forming a high velo- city region above the fluidized bed. Despite a low gas inlet velocity below the bed the gas velocity above the fluidized bed becomes high enough to actually remove par ⁇ ticles from the bed.
  • 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.
  • 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 dis ⁇ engagement height or free board space.
  • the present invention teaches how to use en- trainment to beneficial advantage to obtain high carbon ⁇ aceous 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 char, carbonaceous material and inert material.
  • the system of the present invention is versatile and could be combined with any type of combustor, fluid ⁇ ized, 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 inert materi ⁇ als" 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 10 inch I.D. gasifier coupled to 5 a 40 inch I.D. combustor.
  • the gasifier and all connecting piping was constructed without refractory linings to re ⁇ cute 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 0 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 conver- 5 sions. 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 1600 F and 5 psig. Entrained sand and char are separated from the product gas in a disengager and returned to the 0 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 1900 F.
  • Typical as-received or partially dried wood chips are charged to a feed hopper.
  • a bed of silica sand 5 is placed in the conventional fluid bed combustor and fluidized with air at a linear velocity of about 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 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 50 to in excess of 2500 lb/hr. Larger commercial systems readily achieve significantly higher wood feed rates.
  • lb/ft 2 -hr 2500 lb/hr through a circu ⁇ lar 10" I.D. gasifier is the same as 2500 lb/hr through an area [( ⁇ rr 2 ) i.e., ⁇ (5/12) 2 ] of 0.545 sq. ft.
  • Design specifications for the PRU system are:
  • Combustor Type Fluidized bed
  • Feed Rate Wood 50-2500 lb/hr i.e.,
  • Heating Value of Product 475 Btu/SCF (dry)
  • Heat Carrier silica sand Gasifying Medium: steam or inert gas Fuels Utilized Thus Far:
  • start-up of the gasifier for example coupled to a combustor would involve the stages of heat-up and initi ⁇ ation 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 pro ⁇ **d 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 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)

Abstract

Nouveau procédé de fonctionnement d'un gazéificateur pour la production de gaz combustible à partir de combustibles carbonés. Le procédé ci-décrit permet le fonctionnement en mode entraîné utilisant des vitesses du gaz d'admission inférieures à 7 pieds par seconde, tout en obtenant des débits de la charge extraordinairement élevés, dépassant 4000 livres/pied2-heure.
PCT/US1986/001922 1985-09-20 1986-09-15 Gazeificateur de biomasse a faible vitesse du gaz d'admission et a debit eleve Ceased WO1987001719A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
DE8686905659T DE3670507D1 (de) 1985-09-20 1986-09-15 Vergaser mit hohem durchfluss fuer biomasse bei schwacher gasgeschwindigkeit.
AT86905659T ATE52103T1 (de) 1985-09-20 1986-09-15 Vergaser mit hohem durchfluss fuer biomasse bei schwacher gasgeschwindigkeit.
JP61504942A JPH0794669B2 (ja) 1985-09-20 1986-09-15 低導入ガス速度および高処理量バイオマスガス化機

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US77834585A 1985-09-20 1985-09-20
US778,345 1985-09-20

Publications (1)

Publication Number Publication Date
WO1987001719A1 true WO1987001719A1 (fr) 1987-03-26

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ID=25113028

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US1986/001922 Ceased WO1987001719A1 (fr) 1985-09-20 1986-09-15 Gazeificateur de biomasse a faible vitesse du gaz d'admission et a debit eleve

Country Status (6)

Country Link
EP (1) EP0239589B1 (fr)
JP (1) JPH0794669B2 (fr)
AU (1) AU591714B2 (fr)
CA (1) CA1271634A (fr)
DE (1) DE3670507D1 (fr)
WO (1) WO1987001719A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1601614A4 (fr) * 2002-09-10 2008-02-13 Mfg & Tech Conversion Int Inc Processus et appareil de reformage a la vapeur
ES2327019A1 (es) * 2008-04-21 2009-10-22 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
EP2007855A4 (fr) * 2006-03-24 2011-03-30 Silvagas Corp Système de gazéification de biomasse
US8197764B2 (en) 2007-03-05 2012-06-12 Stichting Energieonderzoek Centrum Nederland Device for producing a product gas from a fuel, such as biomass
CN103740386A (zh) * 2013-12-30 2014-04-23 广州迪森热能技术股份有限公司 生物质双级反应器系统

Families Citing this family (3)

* Cited by examiner, † Cited by third party
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
DE19736867C2 (de) * 1997-08-25 2003-01-16 Montan Tech Gmbh Verfahren zur allothermen Vergasung von organischen Stoffen und Stoffgemischen
NL1016411C2 (nl) * 2000-10-16 2002-04-18 Stichting Energie Werkwijze en inrichting voor het vergassen van biomassa.

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2654665A (en) * 1950-02-21 1953-10-06 Consolidation Coal Co Gasification of carbonaceous solids
US4026679A (en) * 1975-03-21 1977-05-31 Stora Kopparbergs Bergslags Aktiebolag Apparatus for and process of converting carbonaceous materials containing sulphur to an essentially sulphur-free combustible gas
DE2643298A1 (de) * 1976-09-25 1978-04-06 Davy Bamag Gmbh Verfahren zur kontinuierlichen vergasung von feinteiligem, kohlenstoffhaltigem material
EP0003117A2 (fr) * 1978-01-12 1979-07-25 Battelle Development Corporation Lit fluidisé à deux zones pour la combustion ou la gazéification
DE2802132A1 (de) * 1978-01-19 1979-07-26 Bergwerksverband Gmbh Verfahren zur gleichzeitigen erzeugung von schwelprodukten und synthesegas
GB2058829A (en) * 1979-09-21 1981-04-15 Monsanto Co Gasification of carbon- containing materials

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3853498A (en) * 1972-06-28 1974-12-10 R Bailie Production of high energy fuel gas from municipal wastes
US4032305A (en) * 1974-10-07 1977-06-28 Squires Arthur M Treating carbonaceous matter with hot steam

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2654665A (en) * 1950-02-21 1953-10-06 Consolidation Coal Co Gasification of carbonaceous solids
US4026679A (en) * 1975-03-21 1977-05-31 Stora Kopparbergs Bergslags Aktiebolag Apparatus for and process of converting carbonaceous materials containing sulphur to an essentially sulphur-free combustible gas
DE2643298A1 (de) * 1976-09-25 1978-04-06 Davy Bamag Gmbh Verfahren zur kontinuierlichen vergasung von feinteiligem, kohlenstoffhaltigem material
EP0003117A2 (fr) * 1978-01-12 1979-07-25 Battelle Development Corporation Lit fluidisé à deux zones pour la combustion ou la gazéification
DE2802132A1 (de) * 1978-01-19 1979-07-26 Bergwerksverband Gmbh Verfahren zur gleichzeitigen erzeugung von schwelprodukten und synthesegas
GB2058829A (en) * 1979-09-21 1981-04-15 Monsanto Co Gasification of carbon- containing materials

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1601614A4 (fr) * 2002-09-10 2008-02-13 Mfg & Tech Conversion Int Inc Processus et appareil de reformage a la vapeur
EP2007855A4 (fr) * 2006-03-24 2011-03-30 Silvagas Corp Système de gazéification de biomasse
EP2610327A1 (fr) * 2006-03-24 2013-07-03 Rentech, Inc. Système de gazéification de biomasse
US8197764B2 (en) 2007-03-05 2012-06-12 Stichting Energieonderzoek Centrum Nederland Device for producing a product gas from a fuel, such as biomass
ES2327019A1 (es) * 2008-04-21 2009-10-22 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
ES2327019B1 (es) * 2008-04-21 2010-08-10 Jose Grau Almirall Procedimiento de pirolisis de una carga de biomasa y posterior gasificacion del carbon obtenido mediante dicha pirolisis y reactor para llevarlo a cabo.
CN103740386A (zh) * 2013-12-30 2014-04-23 广州迪森热能技术股份有限公司 生物质双级反应器系统

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DE3670507D1 (de) 1990-05-23
JPH0794669B2 (ja) 1995-10-11
EP0239589A1 (fr) 1987-10-07
JPS63501511A (ja) 1988-06-09
CA1271634A (fr) 1990-07-17
AU591714B2 (en) 1989-12-14
AU6400286A (en) 1987-04-07
EP0239589B1 (fr) 1990-04-18

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