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WO2025073011A1 - Système de pyrolyse de biomasse - Google Patents

Système de pyrolyse de biomasse Download PDF

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Publication number
WO2025073011A1
WO2025073011A1 PCT/AU2024/051059 AU2024051059W WO2025073011A1 WO 2025073011 A1 WO2025073011 A1 WO 2025073011A1 AU 2024051059 W AU2024051059 W AU 2024051059W WO 2025073011 A1 WO2025073011 A1 WO 2025073011A1
Authority
WO
WIPO (PCT)
Prior art keywords
biomass
gas
pyrolysis system
section
feed
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.)
Pending
Application number
PCT/AU2024/051059
Other languages
English (en)
Inventor
Chad Sheppeard
Kannappar Mukunthan
John MELLOWES
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.)
Biocarbon Pty Ltd
Original Assignee
Biocarbon Pty Ltd
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
Priority claimed from AU2023903214A external-priority patent/AU2023903214A0/en
Application filed by Biocarbon Pty Ltd filed Critical Biocarbon Pty Ltd
Publication of WO2025073011A1 publication Critical patent/WO2025073011A1/fr
Pending legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B11/00—Coke ovens with inclined chambers
    • 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
    • C10B49/02—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • 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
    • C10B49/02—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
    • C10B49/04—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
    • C10B49/06—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 hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated according to the moving bed type
    • 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
    • C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
    • C10B57/10—Drying
    • 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
    • C10B57/18—Modifying the properties of the distillation gases in the oven
    • 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
    • C10B7/00—Coke ovens with mechanical conveying means for the raw material inside the oven
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10C—WORKING-UP PITCH, ASPHALT, BITUMEN, TAR; PYROLIGNEOUS ACID
    • C10C5/00—Production of pyroligneous acid distillation of wood, dry distillation of organic waste
    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • 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
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
    • F27B9/14—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment
    • F27B9/147—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity characterised by the path of the charge during treatment; characterised by the means by which the charge is moved during treatment the charge moving on an inclined floor
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F27—FURNACES; KILNS; OVENS; RETORTS
    • F27B—FURNACES, KILNS, OVENS OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
    • F27B9/00—Furnaces through which the charge is moved mechanically, e.g. of tunnel type; Similar furnaces in which the charge moves by gravity
    • F27B9/30—Details, accessories or equipment specially adapted for furnaces of these types
    • F27B9/3005—Details, accessories or equipment specially adapted for furnaces of these types arrangements for circulating gases
    • 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

  • the present invention relates to a biomass pyrolysis system.
  • the present invention seeks to provide a biomass pyrolysis system, which will overcome or substantially ameliorate at least one or more of the deficiencies of the prior art, or to at least provide an alternative.
  • gas can flow in a pathway on top and up the step grate, through the incoming feed material to a condenser and is condensed and liquids, known as pyroligneous acid, are collected, and wherein the reciprocating grate urges infeed biomass along the steps and conversion of the biomass to carbon material collected at the reactor exit.
  • part of the gas after condensing the liquids out can be injected back into the reactor system near the char exit to enhance thermal efficiency and drying of biomass, particularly for high moisture feeds.
  • the method uses high temperature combustion conveying equipment (moving grate furnaces) which can be easily scaled to large capacity compared to currently available pyrolysis equipment (e.g., auger based) and changing its internal gas pathway.
  • high temperature combustion conveying equipment moving grate furnaces
  • pyrolysis equipment e.g., auger based
  • Fig. 1 is a reciprocating step grate furnace of the prior art showing limited gas flow and thereby controlled thermochemical transformation of biomass.
  • Fig 4 is a diagrammatic view of the key process parameters for control of biomass material and gas flow, and for temperature and pressure control, of the modified reciprocating step grate furnace for conducting thermochemical transformation of biomass of Fig 2 in accordance with the present invention.
  • Fig 9 is a diagrammatic block view of the steps of a method of pyrolysis for improved scaling and efficiency in accordance with a preferred embodiment of the present invention.
  • Syngas burner not operating - could be secondary fuel burner to help with emissions and peak heat requirements
  • the feed travels down the vertical section to the top of a moving floor furnace mechanism.
  • This feed is fed into a sealed reactor section through a variable cross section area and feeding mechanism such as augers or pusher rod.
  • the feed rate is controlled by PLC software, independently of the floor speed.
  • the reciprocating grate is shown at 3, 4 and 5, wherein at 3 the feed travels down the moving floor furnace in a suitably dimensioned and sealed reaction chamber at a variably controlled speed to control “residence time” and increase material temperature.
  • the material is heated by hot gases/air injected through the floor section and from radiant heat of the reaction chamber walls and roof.
  • the reciprocating grate approaches 4 the material is heated to 400-800C and by the time it gets towards the end of the step the material is fully carbonised, typically with 90-95% Fixed Carbon content.
  • Air is injected under the grate section at 6.
  • the rate is controlled through the PLC software to maintain pre-determined processing conditions required for the feed properties and product specifications.
  • the syngas travels from the sealed reaction chamber section through variable geometry at section 2 and then vertically up the full feed column by way of a vacuum pump.
  • the vertical feed column is designed (large enough) to cool the gases sufficiently and the dimensions and angles in section 8 help settle any dust components contained within the gas and a further condensate system is injected into the gas stream.
  • the step grate section is modified by the uniqueness of changing the feeding section, reaction chamber and gas pathway built "on top" of this step grate which is different to all other step grate furnaces. This is different to the current running grate stoker furnaces in that our plant operates in pyrolysis mode (not gasification/combustion) and incorporates countercurrent material/gas flows and all of these allowing for easy scale-up. All existing "new pyrolysis technologies" have major constraints regarding scaling.
  • Fig 4 there are key process parameters for control of biomass material and gas flow, and for temperature and pressure control, of the modified reciprocating step grate furnace for conducting thermochemical transformation of biomass of Fig 2 and Fig 3.
  • [63]“AT21 ” is a CO meter measuring and alarming for any escaping gases from the reactor as feed is entering through the lock hopper.
  • Oxygen reacts with the volatile gases coming out of the heated material and travels upwards towards the feed material entry region and through the gas exit settler where “PUMP2” acts as a spray cooler and collects the condensables out of the gas while cooling it further.
  • the condensed wood vinegar product is weighed by load cell “WT026”.
  • the reactor system allows independent varying of feed rate and “residence time”. This also allows for control of injection volumes and combustion of gas within the reactor independent of feed material.
  • the primary control variables in our biomass pyrolysis system were - material feed rate into the reactor, residence time (in step grate) and air injection rate and locations in the reactor. These variables were controlled to perform pyrolysis at different temperatures, with the aims of achieving complete charring, characterising char yield (the percentage char produced from dry feed) and other product yields, and characterising product qualities.
  • Examples A and B show two different temperature profiles and residence times (with the corresponding graphs showing real time data) noting that these examples are not the limitation of what the invention can do.
  • Fig 7 shows Example 2 for hardwood chips (25% moisture) - 400 to 450°C reactor temperature (gas phase) and 13 min residence time and 25% char yield (dry basis).
  • the reactor system of the present invention can handle high moisture feed materials (e.g., 40% moisture content) without the need for pre-drying or external energy sources. This was not possible in prior art systems that required a drying step prior to pyrolysis and/or external energy input to sustain the process.
  • FIG 8 this is a pyrolysis system using three different sections combined in series, a. A vertical drying and gas scrubbing section, 2, b. A transitional section 3, and c. An extended horizontal high temperature reactor zone 4 based on top of a step grate furnace.
  • the system is to efficiently convert various biomass materials into high Fixed Carbon material, clean syngas and valuable condensates.
  • This dried feed is fed at transitional section 3 into a separate sealed reactor section through a variable cross section area and feeding mechanism such as augers or pusher rod.
  • the feed rate is controlled by PLC software independently of the grate floor speed to adjust material bed height.
  • the feed travels down the moving step grate furnace 4 in a suitably dimensioned and sealed reaction chamber at a variably controlled speed to control residence time and increase the material temperature.
  • the reactor system has no external energy input to drive the process, and all energy requirements (drying, pyrolysis and heat losses) are provided by the feed material itself (depending on the feed and processing conditions this could be in the range of 5 to 20% of the feed energy).
  • Our unique design allows for low processing temperatures (e.g., 450°C) on wet feed materials (e.g., 40% moisture content) without external energy input.
  • a liquid can be injected at this point into the char at exit 6 to change the gas composition through the water gas reaction.
  • a combination of pre-heated syngas/oxygen containing gas (gas/air) is injected under the grate, through the material and above the material at section 5.
  • the rate and mixture ratio is controlled through the PLC software to maintain pre-determined processing conditions required for feed properties and product specifications.
  • This burner 10 temperature can be controlled through the PLC to assist with faster cold start and additional heat load required for various processing conditions. It can minimise the amount of nitrogen (air) injected into the system for a higher energy density syngas product.
  • Fig 9 there is shown method of forming a biomass pyrolysis system including the steps of” a. provide reciprocating grate b.
  • the reaction chamber is formed by a channel above the stepped grate causing reaction gases to flow adjacent and up and above the stepped grate to be fed off from an upper section c.
  • the reciprocating grate urges infeed biomass along the steps and conversion of the biomass to carbon material collected at the reactor exit e. part of the gas after condensing the liquids out can be injected back into the reactor system near the char exit to increase drying of high moisture feeds.
  • the invention provides one or a combination of one or more benefits of: a. the ability to make low volatile, high Fixed Carbon (95%) char from high moisture biomass in a single process without external energy sources. This is achieved by the modified process of pyrolysis and conducted at a relatively low temperature by limiting air injection - unlike gasification - and making a much higher char yield than a gasification process. b. Continuous char making processes of the prior art using wet feed material typically have lower char yields due to increased gasification or require additional external energy sources to remove the moisture in the feed material before pyrolysis. c.
  • Gas flow is controlled by a blower to keep the reactor at a slightly negative pressure compared to the ambient environment.
  • k The ability to automatically change process controls to cater for various types of biomass material, size and moisture contents on a continual basis.
  • l. Recirculating of dry gas at varying rates to allow for extra drying capacity.
  • m. Capturing the specific heat in char before exit by direct injection and contact of dried and cooled syngas for further beneficial use in the vertical section.
  • n Highly thermally efficient process with all products exiting below 100°C (thereby using the majority of heat in the process).
  • o The ability to change gas composition and calorific value based on various air, syngas, liquid injection rates alongside external radiant heat sources.
  • the vertical feed column also allows for scrubbing of gas as heavy molecules are deposited on the cooler incoming feed. Balster Hugo does not have the same level of interaction between hot dirty gas and packed bed of incoming feed.
  • the reactor of the present invention can run from 400-800°C - the disclosed prior art can’t go below 650°C.
  • the present invention chars a bed of material at a set thickness and speed, whereas these shaft style furnaces do not have the same degree of control over the furnace or pyrolysis zone. • A vertical reactor with counter flow of gases and solids. But much restricted in scope and possibilities for scaling up and required multiple units.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un système de pyrolyse utilisant trois sections différentes combinées en série, une section de séchage vertical et d'épuration de gaz, 2, une section de transition 3, et une zone de réacteur à haute température horizontale étendue 4 basée sur une partie supérieure d'un four à grille étagée. Le système est destiné à convertir efficacement divers matériaux de biomasse en un matériau à teneur en carbone fixe élevée, en un gaz de synthèse propre et en des condensats recyclables par commande de l'alimentation vers le bas de la section verticale de séchage et de lavage de gaz dans un agencement d'échange de chaleur à écoulement à contre-courant à lit tassé où le temps de séjour et le volume de gaz peuvent être régulés par l'intermédiaire d'un débit d'alimentation 3, d'une injection d'air 5, d'une injection de gaz de recirculation 6 & 14. La chaleur rayonnante au niveau de la section 12 fournit de l'énergie supplémentaire pour sécher le matériau d'alimentation humide.
PCT/AU2024/051059 2023-10-06 2024-10-07 Système de pyrolyse de biomasse Pending WO2025073011A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
AU2023903214 2023-10-06
AU2023903214A AU2023903214A0 (en) 2023-10-06 A biomass pyrolysis system

Publications (1)

Publication Number Publication Date
WO2025073011A1 true WO2025073011A1 (fr) 2025-04-10

Family

ID=95284058

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/AU2024/051059 Pending WO2025073011A1 (fr) 2023-10-06 2024-10-07 Système de pyrolyse de biomasse

Country Status (1)

Country Link
WO (1) WO2025073011A1 (fr)

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4109590A (en) * 1976-12-03 1978-08-29 Mansfield Carbon Products, Inc. Apparatus and method for producing gas
DE2930256A1 (de) * 1979-07-26 1981-02-19 Balster Hugo Dr Verfahren und vorrichtung zur direkten herstellung von biogas aus organischen stoffen mit hilfe eines rost-waermetauschers
US20120079762A1 (en) * 2009-04-17 2012-04-05 European Charcoal Ag Continuously Converting Biomass
WO2012154133A2 (fr) * 2011-05-09 2012-11-15 KIV KOVINSKA INDUSTRIJA VRANSKO d.d. Dispositif et procédé de gazéification
US20180208852A1 (en) * 2015-07-21 2018-07-26 British Columbia Biocarbon Ltd. Biocoal fuel product and processes and systems for the production thereof
KR102181822B1 (ko) * 2019-06-15 2020-11-24 홍영기 바이오매스를 포함하는 가연성 재생 연료를 이용한 열분해가스화 시스템
CN113897203A (zh) * 2021-09-08 2022-01-07 华中农业大学 生物质半气化强化自热式炭化装置及控制方法与应用
WO2022193537A1 (fr) * 2021-03-15 2022-09-22 佛山市华洁源热能与环境工程技术有限公司 Dispositif de pyrolyse à commande d'oxygène à déchets solides à pression négative fermée

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4109590A (en) * 1976-12-03 1978-08-29 Mansfield Carbon Products, Inc. Apparatus and method for producing gas
DE2930256A1 (de) * 1979-07-26 1981-02-19 Balster Hugo Dr Verfahren und vorrichtung zur direkten herstellung von biogas aus organischen stoffen mit hilfe eines rost-waermetauschers
US20120079762A1 (en) * 2009-04-17 2012-04-05 European Charcoal Ag Continuously Converting Biomass
WO2012154133A2 (fr) * 2011-05-09 2012-11-15 KIV KOVINSKA INDUSTRIJA VRANSKO d.d. Dispositif et procédé de gazéification
US20180208852A1 (en) * 2015-07-21 2018-07-26 British Columbia Biocarbon Ltd. Biocoal fuel product and processes and systems for the production thereof
KR102181822B1 (ko) * 2019-06-15 2020-11-24 홍영기 바이오매스를 포함하는 가연성 재생 연료를 이용한 열분해가스화 시스템
WO2022193537A1 (fr) * 2021-03-15 2022-09-22 佛山市华洁源热能与环境工程技术有限公司 Dispositif de pyrolyse à commande d'oxygène à déchets solides à pression négative fermée
CN113897203A (zh) * 2021-09-08 2022-01-07 华中农业大学 生物质半气化强化自热式炭化装置及控制方法与应用

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