WO2014145198A1 - Boucle de pyrolyse ou de gazéification employant une vis sans fin - Google Patents

Boucle de pyrolyse ou de gazéification employant une vis sans fin Download PDF

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Publication number
WO2014145198A1
WO2014145198A1 PCT/US2014/029920 US2014029920W WO2014145198A1 WO 2014145198 A1 WO2014145198 A1 WO 2014145198A1 US 2014029920 W US2014029920 W US 2014029920W WO 2014145198 A1 WO2014145198 A1 WO 2014145198A1
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WO
WIPO (PCT)
Prior art keywords
auger
reactor
return
pyrolysis gasification
outlet
Prior art date
Application number
PCT/US2014/029920
Other languages
English (en)
Inventor
Zia Abdullah
Original Assignee
Battelle Memorial Institute
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 Memorial Institute filed Critical Battelle Memorial Institute
Publication of WO2014145198A1 publication Critical patent/WO2014145198A1/fr

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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
    • C10J3/007—Screw type gasifiers
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/02—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
    • 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
    • C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
    • C10J3/60—Processes
    • C10J3/62—Processes with separate withdrawal of the distillation products
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
    • C10B57/04—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition
    • C10B57/06—Other carbonising or coking processes; Features of destructive distillation processes in general using charges of special composition containing additives
    • 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
    • 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
    • C10J2300/094—Char
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0986—Catalysts
    • 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
    • C10J2300/0983—Additives
    • C10J2300/0993—Inert particles, e.g. as heat exchange medium in a fluidized or moving bed, heat carriers, sand
    • 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
    • C10J2300/1671—Integration of gasification processes with another plant or parts within the plant with the production of electricity
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/10—Biofuels, e.g. bio-diesel

Definitions

  • Biomass may be subjected to pyrolysis to create a hot pyrolysis vapor.
  • Bio oil may be extracted from the hot pyrolysis vapor.
  • biomass may be subjected to gasification to create a syn gas.
  • a single pyrolysis gasification loop for pyrolyzing a biomass material comprising: a reactor auger operatively connected to at least one of a biomass inlet and a vapor outlet; and a return auger; wherein the reactor auger and the return auger are operatively connected by at least one of a reactor outlet and a return outlet; wherein the reactor auger is operable to advance the biomass material to the return auger via the reactor outlet; wherein the return auger is operable to advance the biomass material to the reactor auger via the return outlet; and wherein the reactor auger is operable to pyrolyze the biomass material.
  • a single pyrolysis gasification loop for gasifying a char material comprising: a reactor auger operatively connected to at least one of a heat inlet and a gas outlet; and a return auger; wherein the reactor auger and the return auger are operatively connected by at least one of a reactor outlet and a return outlet; wherein the reactor auger is operable to advance the char material to the return auger via the reactor outlet; wherein the return auger is operable to advance the char material to the reactor auger via the return outlet; and wherein the reactor auger is operable to gasify the char material.
  • FIG. 1 illustrates an example arrangement of a single pyrolysis gasification loop ("PGL") operating in a pyrolysis mode.
  • PTL pyrolysis gasification loop
  • FIG. 2 illustrates an example arrangement of a single PGL operating in a gasification mode.
  • the processing of biomass to extract bio oil therefrom may involve the pyrolysis of biomass to create a hot pyrolysis vapor.
  • Pyrolysis processes may include fast pyrolysis of biomass material at temperatures of about 500 °C.
  • three groups of components may be created, including: non-condensable gases, vapor that may be quenched into bio oil, and solids known as char and coke.
  • Char and coke may be gasified utilizing a gasification process to generate a produce, such as a syn gas product, and energy in the form of heat.
  • FIG. 1 illustrates an example arrangement of a PGL 100 operating in a pyrolysis mode.
  • PGL 100 may comprise a series of augers, including a reactor auger 102 and a return auger 104.
  • PGL 100 may be configured to intake biomass material via a biomass inlet 106.
  • PGL 100 may be configured to outlet a pyrolysis vapor via a vapor outlet 108.
  • Biomass inlet 106 may be operatively connected to at least one of reactor auger 102 and return auger 104.
  • Vapor outlet 108 may be operatively connected to at least one of reactor auger 102 and return auger 104.
  • PGL 100 may comprise a 1-3 ton waste to energy conversion ("WEC") system comprising two separate modules.
  • a first module may be configured for feed pretreatment (such as sizing) and/or thermochemical conversion, while a second module may be configured for production of fuels and/or electric power.
  • Each of the first module and the second module may be configured to fit in containers having dimensions of about 8 ft. by about 8 ft. by about 20 ft.
  • PGL 100 may be configured to fit entirely in a container having dimensions of about 8 ft. by about 8 ft. by about 20 ft.
  • PGL 100 may be configured to fit entirely in a container having dimensions less than about 8 ft. by about 8 ft. by about 20 ft.
  • PGL 100 may be operatively connected to upstream and downstream components, such as dryers, size attrition devices, and electrical generator sets.
  • PGL 100 is configured to be very compact. PGL 100 may not require fluidization gas. PGL 100 may not require the associated auxiliary equipment required for conventional thermochemical conversion technologies. PGL 100 may not require a separate continuous heating system. PGL 100 may include minimal parasitic loss. PGL 100 may include thermal storage and temperature control via phase change media. PGL 100 may exceed 50% net energy recovery. PGL 100 may be configured to simultaneously produce both a low oxygen bio oil and a syn gas.
  • the low oxygen bio oil generated by PGL 100 may be a stable product.
  • the low oxygen bio oil may be stored for later use.
  • the low oxygen bio oil may be used in a modified diesel engine.
  • the low oxygen bio oil may be converted to a hydrocarbon fuel that can be used by a vehicle.
  • the syn gas generated by PGL 100 may be used to produce electricity during operation of PGL 100.
  • the syn gas may be utilized in an electrical generation system.
  • the biomass material may comprise any of a variety of lignocellolosic feed materials.
  • the biomass material may comprise a wood or plant material.
  • the biomass material may comprise waste.
  • PGL 100 may operate in parallel with additional PGL systems.
  • a plurality of PGL systems, including PGL 100 may be oriented inside an insulated container.
  • a plurality of PGL systems, including PGL 100 may be oriented with a phase change material in an insulated container.
  • a plurality of PGL systems, including PGL 100 may be substantially surrounded by a phase change material in an insulated container.
  • a plurality of PGL systems, including PGL 100 may be oriented with a phase change material in an insulated container, wherein at least one of reactor auger 102 and return auger 104 may be substantially surrounded by a phase change material.
  • Biomass may be introduced to PGL 100 via biomass inlet 106.
  • Biomass may first be introduced into reactor auger 102.
  • Reactor auger 102 may comprise an auger device within a substantially cylindrical housing. The auger device may be configured to advance material longitudinally along the interior of the substantially cylindrical housing. Biomass may be pyrolyzed within the cylindrical housing of reactor auger 102. Biomass may be exposed to temperatures of about 500 °C within reactor auger 102.
  • Reactor auger 102 may contain granular heating media. Biomass may be contacted with granular heating media within reactor auger 102. Biomass may be pyrolyzed by contact with granular heating media within reactor auger 102.
  • Biomass within reactor auger 102 may undergo flash pyrolysis creating at least one of a vapor and a char (e.g., a fixed carbon).
  • the vapor may exit PGL 100 via vapor outlet 108.
  • the char may exit reactor auger 102 via a reactor outlet 110.
  • Reactor outlet 110 may be operatively connected to return auger 104.
  • Reactor outlet 110 may be configured to transfer char from reactor auger 102 to return auger 104.
  • Char may be transferred from reactor auger 102 to return auger 104 along with granular heating media. Char may be mixed with granular heating media and transferred from reactor auger 102 to return auger 104.
  • Return auger 104 may comprise an auger device within a substantially cylindrical housing.
  • the auger device may be configured to advance material longitudinally along the interior of the substantially cylindrical housing. Material advancing through return auger 104 may be returned to reactor auger 102 via a return outlet 112. Return outlet 112 may be operatively connected to reactor auger 102. Return outlet 112 may be configured to transfer material, including char or granular heating media, from return auger 104 to reactor auger 102.
  • PGL 100 comprises reactor auger 102 and return auger 104 oriented in a continuous loop.
  • the continuous loop may be formed by at least reactor auger 102, reactor outlet 110, return auger 104, and return outlet 112.
  • Reactor auger 102 and return auger 104 may comprise heating media, including granular heating media.
  • reactor auger 102 is operatively connected to a reactor motor 114.
  • Reactor motor 114 may comprise any motor capable of causing the auger device within reactor auger 102 to rotate.
  • Reactor motor 114 may be configured to cause the auger device within reactor auger 102 to rotate at any of a variety of rotational velocities.
  • Reactor motor 114 may be a stepper motor configured to cause the auger device within reactor auger 102 to rotate in a number of equal steps.
  • return auger 104 is operatively connected to a return motor 116.
  • Return motor 116 may comprise any motor capable of causing the auger device within return auger 104 to rotate.
  • Return motor 116 may be configured to cause the auger device within return auger 104 to rotate at any of a variety of rotational velocities.
  • Return motor 116 may be a stepper motor configured to cause the auger device within return auger 104 to rotate in a number of equal steps.
  • PGL 100 may operate for a fixed time period of operation in pyrolysis mode, after which PGL operation may be switched to gasification mode (illustrated in FIG. 2).
  • PGL 100 may operate for any of a variety of desired time periods, including a period of time on the order of minutes.
  • a user may establish and adjust the time period of operation of the PGL system in pyrolysis mode or gasification mode.
  • FIG. 2 illustrates an example arrangement of a PGL 200 operating in a gasification mode.
  • PGL 200 may comprise a series of augers, including reactor auger 102 and return auger 104.
  • Reactor auger 102 may be operatively connected to reactor motor 114, while return auger 104 may be operatively connected to return motor 116.
  • Reactor auger 102 and return auger 104 may be operatively connected by reactor outlet 110 and return outlet 112.
  • PGL 200 may be configured to intake steam or heated air via a heat inlet 206.
  • PGL 200 may be configured to outlet a gas, such as syn gas, via a gas outlet 208.
  • PGL 200 gasifies a char or coke in reactor auger 102.
  • Reactor auger 102 may comprise a temperature greater than about 500 °C.
  • reactor auger 102 comprises a temperature greater than about 660 °C.
  • Gasification of a char or coke in reactor auger 102 may yield a syn gas, which may exit PGL 200 via gas outlet 208.
  • Heat inlet 206 may be operatively connected to at least one of reactor auger 102 and return auger 104.
  • Gas outlet 208 may be operatively connected to at least one of reactor auger 102 and return auger 104.
  • PGL 200 comprises the same system and components as PGL 100. In another embodiment, PGL 200 comprises a wholly separate system from PGL 100. PGL 200 may comprise the same system and components as PGL 100, with the exception of the addition of heat inlet 206 and gas outlet 208.
  • PGL 200 comprises the same system and components as PGL 100, wherein biomass entering PGL 100 via biomass inlet 106 is replaced with hot air or steam entering PGL 200 via heat inlet 206. Biomass inlet 106 and heat inlet 206 may be the same inlet tasked for different purposes when the PGL is operating in different modes.
  • PGL 200 may comprise the same system and components as PGL 100, wherein vapor exiting PGL 100 via vapor outlet 108 is replaced with syn gas exiting PGL 200 via gas outlet 208. Vapor outlet 108 and gas outlet 208 may be the same outlet tasked for different purposes when the PGL is operating in different modes.
  • PGL 200 may be configured to gasify char and coke. The char or coke may be left over from pyrolysis performed in PGL 100. PGL 200 may be configured to gasify and partially combust char or coke. PGL 200 may be configured to generate a gas, such as syn gas, from the gasification of char. PGL 200 may gasify at least a portion of the char or coke and leave noncombustible ash. The noncombustible ash may exit PGL 200 via gas outlet 208 with a gas.
  • a gas such as syn gas
  • PGL 200 may be configured to generate energy in the form of heat from the gasification of char.
  • the energy generated by PGL 200 may be sufficient to provide at least a portion of the process heat and at least partially maintain the necessary reaction temperature in PGL 100 during pyrolysis, and/or in PGL 200 during gasification.
  • a plurality of PGL systems are configured to operate simultaneously, with some operating in pyrolysis mode (e.g., PGL 100) and others operating in gasification mode (e.g., PGL 200).
  • a plurality of PGL systems may be oriented within a container and thermally coupled via phase change media.
  • a plurality of PGL systems may be operatively connected and share headers for biomass feed, heated air, syn gas, and pyrolysis vapor.
  • the headers may comprise dampers configured to control the flow of biomass feed, heated air, syn gas, and pyrolysis vapor.
  • the dampers may be controlled by at least one computer.
  • switching between pyrolysis mode (e.g., PGL 100) and gasification mode (e.g., PGL 200) includes the use of dampers.
  • the operation of PGL 100 and gasification 200 may include the use of dampers.
  • the dampers may be controlled by a computer.
  • the dampers may be configured to manage desired reactor temperature.
  • Phase change media may be selected, and thermal coupling between the PGL systems (e.g., PGL 100 or PGL 200) may be designed, such that the absorption and release of the latent heat of fusion is at an appropriate temperature.
  • Phase change media may be selected, and thermal coupling between the PGL systems (e.g., PGL 100 and PGL 200) may be designed, such that sufficient temperature gradients are allowed in the solid and liquid phase of phase change media so that the PGL systems operate at the required temperatures in the pyrolysis mode (e.g., PGL 100) and the gasification mode (e.g., PGL 200). If more energy than necessary is generated by PGL 200 (gasification mode), phase change media may melt and an excessive temperature increase within PGL 200 may be prevented.
  • phase change media may solidify, providing the necessary heat for PGL 100.
  • Phase change media may comprise a metal, such as aluminum.
  • Phase change media may comprise a binary metal, such as Al-Cu.
  • Phase change media may comprise binary salts, such as nitrate salts (e.g., a 03-K Os) with a temperature range between about 220 °C and about 540 °C.
  • a control system (not shown) may monitor temperatures of the PGL systems to determine the mode of operation of individual PGL systems.
  • a control system may monitor any of various process parameters of the PGL systems to determine the mode of operation of individual PGL systems.
  • Granular heating media may comprise an inert substance.
  • Granular heating media may comprise sand.
  • Granular heating media may comprise an acidic catalyst.
  • Granular heating media may comprise zeolites (e.g., HZSM-5, H-Beta, H-Mordenite, or the like).
  • Granular heating media may comprise metal oxides (e.g., Zr0 2 , Ti0 2 , CaO, ZnO, Dolomite, or the like).
  • Granular heating media may comprise FCC catalysts, including spent FCC catalysts.
  • Catalysts may be used during pyrolysis for effectively converting carboxylic acids to ketones, deoxygenating reactive compounds such as aldehydes and ketones, or depolymerizing heavy components. Catalysts may also be used during pyrolysis for effective depolymerization of pyrolysis vapor with relatively modest increase in reaction temperature.
  • Selection of the catalyst used as heating media, as well as selection of the reaction temperature, may enable selective operation of PGL 100 or PGL 200 for either pyrolysis or low temperature gasification of the biomass feed.
  • Low temperature gasification may reduce heat loss from PGL 100 or PGL 200 and increase the thermal efficiency of the pyrolysis or gasification processes.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Materials Engineering (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne des systèmes et des appareils de pyrolyse et de gazéification d'un matériau de biomasse.
PCT/US2014/029920 2013-03-15 2014-03-15 Boucle de pyrolyse ou de gazéification employant une vis sans fin WO2014145198A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201361801147P 2013-03-15 2013-03-15
US61/801,147 2013-03-15

Publications (1)

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WO2014145198A1 true WO2014145198A1 (fr) 2014-09-18

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108003907A (zh) * 2018-01-09 2018-05-08 上海电气集团股份有限公司 一种生物质气化系统的内循环强化热解筒及其使用方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4823712A (en) * 1985-12-18 1989-04-25 Wormser Engineering, Inc. Multifuel bubbling bed fluidized bed combustor system
EP1323810A1 (fr) * 2001-12-12 2003-07-02 von Görtz & Finger Techn. Entwicklungs Ges.m.b.H. Installation de gazéification à tubes doubles
DE102006013617A1 (de) * 2006-03-22 2007-09-27 Universität Kassel Biomassevergaser
EP1865045A1 (fr) * 2006-06-07 2007-12-12 ILW - Ingeneurbüro Reformeur à vapeur pour biomasse
US20080149471A1 (en) * 2006-12-26 2008-06-26 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4823712A (en) * 1985-12-18 1989-04-25 Wormser Engineering, Inc. Multifuel bubbling bed fluidized bed combustor system
EP1323810A1 (fr) * 2001-12-12 2003-07-02 von Görtz & Finger Techn. Entwicklungs Ges.m.b.H. Installation de gazéification à tubes doubles
DE102006013617A1 (de) * 2006-03-22 2007-09-27 Universität Kassel Biomassevergaser
EP1865045A1 (fr) * 2006-06-07 2007-12-12 ILW - Ingeneurbüro Reformeur à vapeur pour biomasse
US20080149471A1 (en) * 2006-12-26 2008-06-26 Nucor Corporation Pyrolyzer furnace apparatus and method for operation thereof

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN108003907A (zh) * 2018-01-09 2018-05-08 上海电气集团股份有限公司 一种生物质气化系统的内循环强化热解筒及其使用方法
CN108003907B (zh) * 2018-01-09 2023-12-29 上海电气集团股份有限公司 一种生物质气化系统的内循环强化热解筒及其使用方法

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