WO2014146206A1 - Procédé et appareil pour la production de charbon de biomasse - Google Patents

Procédé et appareil pour la production de charbon de biomasse Download PDF

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Publication number
WO2014146206A1
WO2014146206A1 PCT/CA2014/050298 CA2014050298W WO2014146206A1 WO 2014146206 A1 WO2014146206 A1 WO 2014146206A1 CA 2014050298 W CA2014050298 W CA 2014050298W WO 2014146206 A1 WO2014146206 A1 WO 2014146206A1
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Prior art keywords
reactor
syn
thermosensor
retort
biomass
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PCT/CA2014/050298
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English (en)
Inventor
Jerry Daniel ERICSSON
Daniel Lennart ERICSSON
Jared Luke Taylor
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Diacarbon Technologies Inc.
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Application filed by Diacarbon Technologies Inc. filed Critical Diacarbon Technologies Inc.
Priority to CA2907725A priority Critical patent/CA2907725A1/fr
Priority to US14/778,938 priority patent/US20160053182A1/en
Publication of WO2014146206A1 publication Critical patent/WO2014146206A1/fr

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    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/008—Details of the reactor or of the particulate material; Processes to increase or to retard the rate of reaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
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    • 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
    • C10B21/00—Heating of coke ovens with combustible gases
    • C10B21/10—Regulating and controlling the combustion
    • 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
    • C10B27/00—Arrangements for withdrawal of the distillation gases
    • C10B27/06—Conduit details, e.g. valves
    • 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
    • C10B37/00—Mechanical treatments of coal charges in the oven
    • C10B37/04—Compressing charges
    • 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
    • C10B41/00—Safety devices, e.g. signalling or controlling devices for use in the discharge of coke
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10B41/00—Safety devices, e.g. signalling or controlling devices for use in the discharge of coke
    • C10B41/08—Safety devices, e.g. signalling or controlling devices for use in the discharge of coke for the withdrawal of the distillation gases
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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    • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
    • C10B47/28—Other processes
    • C10B47/32—Other processes in ovens with mechanical conveying means
    • C10B47/44—Other processes in ovens with mechanical conveying means with conveyor-screws
    • 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
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    • 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
    • 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
    • C10B7/10—Coke ovens with mechanical conveying means for the raw material inside the oven with conveyor-screws
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L5/00—Solid fuels
    • C10L5/40—Solid fuels essentially based on materials of non-mineral origin
    • C10L5/44—Solid fuels essentially based on materials of non-mineral origin on vegetable substances
    • C10L5/447—Carbonized vegetable substances, e.g. charcoal, or produced by hydrothermal carbonization of biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L9/00—Treating solid fuels to improve their combustion
    • C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
    • C10L9/083—Torrefaction
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00058—Temperature measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00193—Sensing a parameter
    • B01J2219/00195—Sensing a parameter of the reaction system
    • B01J2219/002—Sensing a parameter of the reaction system inside the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00191—Control algorithm
    • B01J2219/00222—Control algorithm taking actions
    • B01J2219/00225—Control algorithm taking actions stopping the system or generating an alarm
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2200/00—Components of fuel compositions
    • C10L2200/04—Organic compounds
    • C10L2200/0461—Fractions defined by their origin
    • C10L2200/0469—Renewables or materials of biological origin
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/02—Combustion or pyrolysis
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/08—Drying or removing water
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/30—Pressing, compressing or compacting
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/50—Screws or pistons for moving along solids
    • 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
    • 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
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present disclosure provides a system and method for producing biochar from biomass.
  • the present disclosure provides pyrolytic systems and methods of producing biochar.
  • Pyrolysis is a type of thermal decomposition in which a substance is heated in the absence of oxygen, or under limited oxygen conditions. Pyrolysis may be termed 'fast' or 'slow' depending on the heating rate and residence time of the biomass. In the case of dried biomass, the pyrolysis can result in decomposition into three major products: bio-char (also known as biochar or biocoal), bio-oil, and syn-gas.
  • bio-char also known as biochar or biocoal
  • bio-oil also known as biochar or biocoal
  • syn-gas syn-gas
  • the system may be simple, robust and/or flexible enough to handle a variety of locations, feedstocks and conditions.
  • the disclosure provides, at least in part, a system for producing biochar from biomass.
  • the present systems may be modular comprising, for example, a reactor module and a syn-gas management module.
  • biomass' refers to material derived from non-fossilized organic material, including plant matter such as lignocellulosic material and animal material such as wastes, suitable for conversion into biofuels.
  • the term 'pyrolysis' refers to thermal decomposition in which a substance is heated in the absence of substantial amounts of oxygen.
  • bio-char' or 'biocoal' refers to pyrolyzed biomass.
  • bio-char will have a calorific value of about 15 MJ/Kg or greater, such as about 17 MJ/Kg or greater, or about 19 MJ/Kg or greater, about 21 MJ/Kg or greater, about 23 MJ/Kg or greater, about 25 MJ/Kg or greater, about 27 MJ/Kg or greater, about 29 MJ/Kg or greater.
  • Figure 1 shows a general flow diagram of an exemplary biomass pyrolysis system according to the present disclosure
  • Figure 2 shows a schematic of a biomass pyrolysis system
  • Figure 3 shows the phases of biomass decomposition due to increasing temperature (a) and a typical mass loss profile of biomass undergoing pyrolysis (b).
  • the present disclosure provides, at least in part, a system for pyrolysis of biomass, the system comprising:
  • thermosensor capable of generating a signal when the temperature is above optimal levels
  • a syn-gas management system comprising a syn-gas storage tank having an inlet and an outlet, said inlet in fluid communication with the reactor, and said outlet in fluid communication with the heating system and a syn-gas outlet such as a flare or storage tank wherein the communication is controlled via a valve configurable between at least a first position where flow is directed to the heating system and a second position where flow is directed to the syn-gas outlet; and
  • thermosensor in communication with the thermosensor and the valve; wherein the controller switches the valve from the first position to the second position upon receiving a signal from the thermosensor that the temperature in the reactor is above optimal levels.
  • the present disclosure provides, at least in part, a system for pyrolysis of biomass, the system comprising:
  • thermosensor (a) a reactor having a retort extending therethrough, said retort comprising a suitable conveyor such as, for example, an auger or paddle conveyor, an inlet, and an outlet; the reactor further comprising at least one thermosensor, the thermos ens or capable of generating a signal when the temperature is below optimal levels;
  • a syn-gas management system comprising a syn-gas storage tank having an inlet and an outlet, said inlet in fluid communication with the reactor, and said outlet in fluid communication with the heating system and a syn-gas outlet such as a flare or storage tank wherein the communication is controlled via a valve configurable between at least a first position where flow is directed to the heating system and a second position where flow is directed to the syn-gas outlet; and
  • thermosensor in communication with the thermosensor and the valve; wherein the controller switches the valve from the second position to the first position upon receiving a signal from the thermosensor that the temperature in the reactor is below optimal levels.
  • the present thermosensor may be capable of generating a signal when the temperature is above and below optimal levels.
  • the temperature value at above or below which the thermosensor generates a signal may be predetermined. Such value may be altered depending on a variety of factors such as the needs of a particular production run, the feedstock, the output desired, or the like.
  • the bio-char produced via the present process may have a calorific value of about 18 MJ/Kg or greater, about 22 MJ/Kg or greater, about 24 MJ/Kg or greater, about 26 MJ/Kg or greater, about 28 MJ/Kg or greater, about 30 MJ/Kg or greater.
  • the present bio-char may have an energy density of about 4 MJ/L or greater, about 6 MJ/L or greater, about 8 MJ/L or greater, about 10 MJ/L or greater.
  • the present bio-char may be hydrophobic. For example, if processed at temperatures under about 400°C the bio-char may be hydrophobic.
  • the present bio-char may be hydrophilic. For example, if processed at temperatures above about 400°C the bio-char may be hydrophilic.
  • the present bio-char may have a water contact angle ranging from about 102° to about 20° depending on process temperature.
  • the present biochar preferably is grindable.
  • the coal industry uses the Hardgrove Grindability Index ("HGI") as a standard test to measure grindability where samples are compared to a standard reference sample (“SRS"). For example, if the grindability of a sample was equal to the SRS coal, it would score 50.
  • HGI Hardgrove Grindability Index
  • the present biochar preferably has a HGI of about 50 or greater, about 52 or greater, about 54 or greater, about 56 or greater, about 58 or greater, about 60 or greater.
  • the present disclosure provides a reactor for converting biomass into biochar.
  • the reactor has at least one retort extending through it.
  • the reactor may have two, three, four, or more retorts. It is preferred that the reactor have at least four retorts.
  • the retort may comprise a suitable conveyor such as, for example, an auger or paddle conveyor, an inlet and an outlet. The inlet receives biomass which passes through the reactor on the auger to the outlet.
  • the reactor further comprises a heating system which heats the biomass as it passes through the reactor.
  • the heating system can heat the biomass to a temperature suitable to cause pyrolysis of biomass.
  • the heating system may be any suitable design such as, for example, a plurality of heating elements, heat exchangers, or burners throughout the length of the reactor.
  • the reactor comprises one or more thermosensors.
  • the thermosensors may be used to monitor the temperature of within the reactor enabling the temperature to be kept at the appropriate level to achieve the desired result. Multiple sensors may allow for more accurate assessment of the temperature at different points in the reactor. For example, based on the temperature reading the heating may be increased or decreased.
  • Certain exemplary embodiments of the present disclosure comprise one or more additional sensors such as, for example, a sensor for sensing the speed of the auger. This sensor enables the controller to assess the speed with which the biomass is moving through the retort. If this speed is too slow the controller may cause the speed to increase or if the speed is too fast the controller may cause the speed to decrease.
  • a sensor for sensing the speed of the auger This sensor enables the controller to assess the speed with which the biomass is moving through the retort. If this speed is too slow the controller may cause the speed to increase or if the speed is too fast the controller may cause the speed to decrease.
  • the reactor produces a biochar stream and a gaseous stream.
  • Biochar can have utility as a fuel source, soil additive, or the like.
  • the gaseous stream may comprise condensable and non-condensable components.
  • the condensable components may, for example, be condensed to form pyrolysis oil (bio-oil).
  • Bio-oil may be used as a petroleum substitute.
  • the non-condensable gases (syn-gas) may be combustible and used, for example, to fuel the reactor heating system.
  • the biochar stream may exit the reactor via a biochar delivery system such as described further herein.
  • the gaseous stream may exit the reactor via a gas collection system such as described further herein.
  • the present system may comprise a biochar delivery system for receiving the biochar exiting the reactor.
  • the delivery system receives the biochar stream from the retort via the outlet.
  • the system may include a char cooling means. Any suitable cooling means may be used such as direct contact with a cooling medium, indirect contact with a cooling medium, direct contact fluid quenching, or the like.
  • the means may be an auger which moves the hot biochar through a cooling zone to compaction and/or bagging area.
  • An airlock such as a rotary valve airlock may be positioned between the cooling zone and the compaction/bagging area.
  • the cooling of the biochar may be aided by the application of a liquid such as water.
  • biochar with additives such as nutrients or minerals.
  • additives such as nutrients or minerals.
  • the resultant biochar could derive advantageous properties from such enrichment.
  • nutrients and minerals markedly improves the performance of the product.
  • minerals include, but are not limited to, nitrogen, sulphur, magnesium, calcium, phosphorous, potassium, iron, manganese, copper, zinc, boron, chlorine, molybdenum, nickel, cobalt, aluminum, silicon, selenium, or sodium.
  • nutrients include compost tea, humic and fulvic acids, plant hormones, and other solutions of benefit to plant growth and soil health such as buffers, pH conditioners, and the like.
  • additives may be applied at the biochar delivery system.
  • Additives can be introduced to the cooling liquid and applied to the biochar at the cooling zone. As the cooling liquid boils off the additives can be left behind on the char.
  • Additives may be introduced as a solid and, for example, incorporated through mixing in the cooling zone.
  • Gases may exit the retort(s) via a gas collection system.
  • the system may be in any suitable form but can advantageously be a series of pipes dispersed throughout the reactor such that gas developed in the retort(s) during the pyrolysis process enters the pipes and is carried out of the reactor.
  • the reactor comprises more than one retort it is preferred that each retort have a separate gas collection pipe.
  • Each retort may have more than one gas collection pipe.
  • the separate pipes may feed into a gas collection module but it has been found that having separate pipes running from a section of the retort that has been shown to correspond with a particular biomass temperature and thermochemical stage of decomposition (see Figure 3) to a common gas manifold improves efficiency of gas collection and reduces reactor downtime.
  • the specific positioning of these separate pipes along the retort can improve efficiency.
  • the reactor comprising one or more retorts, one or more thermosensors, and a heating system may be in the form of a module. This can aid in the transportation of the pyrolysis system to various locations.
  • the reactor module may also comprise a gas collection system.
  • the present system comprises a syn-gas management system.
  • the system is adapted to receive the gaseous stream from the reactor, for example via the gas collection system.
  • the gaseous stream may comprise condensable components.
  • the syn-gas management system may comprise a condenser to remove at least some of the condensable components to form bio-oil.
  • the resultant oil may be stored in one or more bio-oil storage tanks.
  • the system may comprise a pump such as, for example, a pump capable of creating at least a partial vacuum.
  • the pump may be positioned downstream of the reactor, but upstream of the syn-gas and bio-oil collection tanks to facilitate gas movement from retort to collection tanks and combustion bumers.
  • the pump may take various forms, but will preferably be capable of conveying a corrosive, and high temperature gas stream.
  • the pump may be a liquid-ring pump, a positive displacement pump, or any other suitable pump or combination of pumps. Preferred are pumps able to tolerate a temperature greater than about 0°C, a temperature greater than about 50°C, a temperature greater than about 100°C. Suitable pumps may be able to tolerate a temperature of less than about 600°C.
  • the pump preferably delivers a pressure greater than about zero (0), but less than about two (2) pounds per square inch when measured at the tank or at the burner.
  • the syn-gas may be stored in a syn-gas tank.
  • the storage tank may have an inlet for receiving the flow of syn-gas from the reactor and an outlet in fluid communication with the heating system and a flare pipe or other means for discharging the syn-gas.
  • the communication may be controlled via a valve, such as a three-way valve, configurable between a first position where flow is directed to the heating system and a second position where flow is directed to the flare pipe or other discharge means. Alternatively the second position may direct the flow of gas to a storage tank for later use.
  • the syn-gas management system comprising the syn-gas storage tank, optionally the condenser and bio-oil storage tank may be in the form of a module. This aids in the transportation of the pyrolysis system to different locations and improves the ease of implementation.
  • the present system may comprise a controller, such as for example a programmable logic controller.
  • the controller may be in communication with the thermosensor and the valve.
  • the controller switches the valve from the first position to the second position upon receiving a signal from the thermosensor that, for example, the temperature in the reactor is above optimal levels.
  • the controller may also switch the valve from the second to the first position upon receiving a signal from the thermosensor that, for example, the temperature in the reactor is below optimal levels.
  • the controller will frequently be a microprocessor.
  • the controller may be a separate module or may be a part of one of the other modules. As a separate module the controller can be located remote from the pyrolysis system.
  • the controller may control more than just the valve.
  • the controller may control a variety of factors such as, for example, the delivery of biomass feedstock from the dryer to reactor, the residence time of biomass in each retort, the speed and/or pressure of vacuum pump(s), the residence time of biochar or bio-coal in any cooling portion of the system, the amount of additive added to biochar or biocoal, the speed of the retort, the speed of the conveyor, or the like, or any combination thereof.
  • the present system may include a biomass dryer module.
  • the drying can receive biomass feedstock and may comprise a moisture sensor.
  • the dryer receives biomass and dries it to reduce the moisture content.
  • the moisture content is about 20% or less, about 18% or less, about 15% or less.
  • the dryer may be, for example, a flash dryer, a belt dryer, or a drum dryer.
  • a rotary valve airlock may be used between the dryer and the reactor in order to control the delivery of the biomass.
  • hot air from the reactor can be used in the dryer thus reducing the need for external heat sources in the dryer and improving the overall efficiency of the system.
  • Any suitable biomass feedstock may be used herein such as, for example, those comprising wood fibre, agricultural fibre, by-products or waste (from plant or animal sources), municipal waste, or the like.
  • the selection of biomass may vary depending on availability, the desired output and the particular application.
  • Softwood-fibre typically comprises three major components: hemicellulose (25-35% dry mass), cellulose (40-50% dry mass), and lignin (25-35% dry mass).
  • the energy content of wood fibre is typically 17-21 GJ/tonne on a dry basis
  • the feedstock may be in particulate form and may have an average particle size of from about 1 mm to about 50 mm, such as from about 5 mm to about 25 mm. It is preferred that the feedstock have a moisture content of about 15% or less, such as about 10 % or less, before commencement of pyrolysis.
  • the present method may comprise a moisture removal step where the feedstock is heated to such a temperature that moisture is driven off.
  • the present method may comprise a hemicellulose decomposition step.
  • the hemicellulose decomposition step may be at a temperature of from about 200 °C to about 280 °C, such as about 220 °C to about 260 °C.
  • the temperature may vary throughout the step or may stay constant. For example, the temperature may be increased at a rate of about 100 °C/min or less, about 50 °C/min or less, about 35 °C/min or less, about 20 °C/min or less, about 15 °C/min or less, about 10 °C/min or less.
  • the step may continue for any suitable length of time such as, about 1 minute or more, about 2 minutes or more, about 3 minutes or more, about 4 minutes or more, about 5 minutes or more, about 10 minutes or more. It is preferred that by the end of the pyrolysis at least about 30%, at least about 40%, at least about 50%, at least about 60%, at least about 70%, at least about 75%, at least about 80%, at least about 85%, of the mass of hemicellulose in the feedstock has been decomposed.
  • the present method may comprise a cellulose decomposition step.
  • the cellulose decomposition step may be at a temperature of from about 240 °C to about 400 °C, such as about 300 °C to about 380 °C.
  • the temperature may vary throughout the step or may stay constant. For example, the temperature may be increased at a rate of about 100 °C/min or less, about 50 °C/min or less, about 35 °C/min or less, about 20 °C/min or less, about 15 °C/min or less, about 10 °C/min or less.
  • the step may continue for any suitable length of time such as, about 1 minute or more, about 2 minutes or more, about 3 minutes or more, about 4 minutes or more, about 5 minutes or more, about 10 minutes or more. It is preferred that by the end of the pyrolysis at least about 30%, at least about 40%, at least about 50%, at least about 60%, at least about 70%, of the mass of cellulose in the feedstock has been decomposed.
  • the present method may comprise a lignin decomposition step.
  • the cellulose decomposition step may be at a temperature of from about 280 °C to about 500 °C, such as about 400 °C to about 500 °C.
  • the temperature may vary throughout the step or may stay constant. For example, the temperature may be increased at a rate of about 100 °C/min or less, about 50 °C/min or less, about 35 °C/min or less, about 20 °C/min or less, about 15 °C/min or less, about 10 °C/min or less.
  • the step may continue for any suitable length of time such as, about 1 minute or more, about 2 minutes or more, about 3 minutes or more, about 4 minutes or more, about 5 minutes or more, about 10 minutes or more. It is preferred that by the end of the pyrolysis at least about 5%, at least about 10%, at least about 15%, at least about 20%, of the mass of lignin in the feedstock has been decomposed.
  • Yields of bio-char, bio-oil, and syn-gas can be altered by varying the process temperatures and/or heat transfer rates. While not wishing to be bound by theory, it is believed that higher temperatures tend to favour the production of bio-oil and/or syn-gas by driving off more of the condensable volatiles produced from decomposition of cellulose. Conversely, slow pyrolysis may favour the production of bio-char by limiting the decomposition of cellulose and reducing the amount of bio-oil produced. Bio-coal production can generally be maximized at temperatures of approximately 285 °C. It is believed that at these temperatures hemicellulose still decomposes into syn-gas while much of the cellulose remains as a solid within the lignin matrix.
  • yields of bio-coal can be increased to around 70%.
  • This type of pyrolysis is known as torrefaction and the resulting bio-char is referred to torrefied bio-char or bio-coal.
  • Producing torrefied bio-char leads to a reduced amount of bio-oil thus reducing the issues associated with storing and handling such oil.
  • many industrial scale kilns are already equipped to handle solid fuels such as bio-coal rather than liquid bio-oil.
  • Certain embodiments according to the present disclosure may provide bio-char yields in the range of from about 20% to about 80%, such as about 25% to about 70%. In general, higher yields are seen with torrefaction than with other types of pyrolysis. Certain embodiments according to the present disclosure may provide bio-oil yields in the range of from about 10% to about 40%, such as about 20% to about 50%.
  • a method for converting biomass to biochar comprises the steps of:
  • additive selected from soil nutrients and/or minerals.
  • minerals include, but are not limited to, nitrogen, sulphur, magnesium, calcium, phosphorous, potassium, iron, manganese, copper, zinc, boron, chlorine, molybdenum, nickel, cobalt, aluminum, silicon, selenium, sodium, compost tea, humic acids, fulvic acids, plant hormones, pH conditioners, buffers, or combinations thereof.
  • Biomass 1 is loaded into a dryer system 2.
  • Biomass may be any suitable such as wood waste, agricultural waste, or any other organic material that can be used to produce bio-char.
  • a rotary valve airlock 3 controls the feeding of the dry biomass feed into a reactor 4.
  • the reactor produces a biochar stream which is fed to a cooling zone 5. Cooling water 6 and additives 7 may be applied to the biochar.
  • a rotary valve airlock 8 controls the movement of the cooled biochar to the compaction 9 and bagging 10 areas.
  • the reactor produces a gaseous stream which passes to a condenser 11 which can condense condensable components such as bio-oil.
  • the condensed bio-oil is collected in a bio-oil collection tank 12.
  • a vacuum pump 13 moves the remain gaseous stream to a oil tank 14, a syn-gas collection tank 15.
  • the gaseous stream is fed to a three-way valve 16.
  • a controller 18 receives a signal from a thermosensor (not shown) in the reactor 4. Depending on the needs of the reactor the controller 18 can direct the valve via a control signal 19 to direct the syn-gas to a flare 17 or to the reactor 4 where the syn-gas can be burnt by a furnace (not shown).
  • Feedstock hopper 1 loads biomass into a cyclone dryer system 2 which has an exhaust 3.
  • Hot flue gas 5 from the furnace 6 can be used in the dryer assembly.
  • a rotary valve airlock 4 controls the feeding of biomass feed into one or more anaerobic retorts 7.
  • Biomass may be wood waste, agricultural waste, or any other organic material that can be burned to produce heat energy.
  • Retorts 7 are tubular and extend through furnace 6. The biomass is advanced through retorts 7 by augers. Heat from furnace 6 and the anaerobic conditions in retorts 7 pyrolize the biomass advancing through retorts 7, converting the organic feed to form a biochar stream and a gaseous stream.
  • At least a portion of the gaseous stream is collected by the gas collection system 8 which comprises pipes leading to a gas collection manifold.
  • the gases are then fed into a condenser 10 which can condense condensable components such as bio-oil.
  • the condensed bio-oil is collected in a bio-oil collection tank 17 which the gaseous stream is fed to a three- way valve 19.
  • the valve can direct the gas to a flare 18 or to syn-gas burners 9 via syn-gas pipe 20.
  • Biochar at the downstream end of retorts 7 is collected and delivered to a cooling retort with a water jacket and auger 13 .
  • the assembly comprises a coolant (water) tank 11 and an additive tank 12.
  • the water and/or additive are applied to the biochar via spray nozzles 14.
  • Cooled and improved biochar is the delivered to a collection bin 16 controlled via a rotary valve airlock 15.

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Abstract

La présente invention concerne, au moins en partie, un système pour la pyrolyse de biomasse, le système comprenant : (a) un réacteur au travers duquel s'étend une cornue, ladite cornue présentant un transporteur, une entrée et une sortie ; le réacteur comprenant en outre au moins un capteur thermique, le capteur thermique pouvant générer un signal lorsque la température est supérieure à des niveaux optimaux ; (b) un système de chauffage conçu pour chauffer le réacteur ; (c) un système de gestion de gaz de synthèse ; le système de gestion comprenant un réservoir de stockage de gaz de synthèse doté d'une entrée et d'une sortie, ladite entrée étant en communication fluidique avec le réacteur et ladite sortie étant en communication fluidique avec le système de chauffage et une sortie de gaz de synthèse, telle qu'une torche ou un réservoir de stockage, la communication étant régulée via une soupape configurable entre au moins une première position dans laquelle l'écoulement est dirigé vers le système de chauffage et une deuxième position dans laquelle l'écoulement est dirigé vers le tuyau de torche ; et (d) un dispositif de commande en communication avec le capteur thermique et la soupape ; le dispositif de commande commutant la soupape de la première position dans la deuxième position lorsqu'il reçoit un signal du capteur thermique indiquant que la température dans le réacteur est supérieure aux niveaux optimaux.
PCT/CA2014/050298 2013-03-20 2014-03-20 Procédé et appareil pour la production de charbon de biomasse WO2014146206A1 (fr)

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WO2017044976A1 (fr) * 2015-09-11 2017-03-16 Enginuity Worldwide, LLC Procédé et produits améliorés au moyen d'une unité de compression rotative
US11034905B2 (en) 2015-09-11 2021-06-15 Ecap Bioenergy, Llc Process and products using a rotary compression unit
WO2017048201A2 (fr) 2015-09-16 2017-03-23 Ghorbel Makram Charbon de bois provenant de résidus agricoles
CN106701130A (zh) * 2017-01-16 2017-05-24 张辉 一种低温干馏提取富里酸的方法
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