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
  • 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
  • C10B49/20—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 in dispersed form
  • C10B49/22—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 in dispersed form according to the "fluidised bed" technique
• • 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
  • C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
  • C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
  • C10B47/22—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form
  • C10B47/24—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge in dispersed form according to the "fluidised bed" technique
• • 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
  • 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
  • C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
  • C10L5/34—Other details of the shaped fuels, e.g. briquettes
  • C10L5/36—Shape
  • C10L5/363—Pellets or granulates
• • 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
• • 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
• • 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

• wood-based charcoal has become the focus of great interest in Europe, China and the USA, as C0 2 emissions of coal-fired power stations and coke plants are tried to be reduced.
• shaft, rotary or multilayer kilns are used in order to produce charcoal.
• woodchips are fed to the apparatus e.g. in a chip size of 2 to 8 cm, dried to the moisture of 10 to 25 %, and charred at a temperature of 200 to 320 °C for approximately 20 to 30 minutes.
• a problem in using wood in the production of energy is that it cannot be fed to large power station boilers in large proportions without significant changes in the devices, e.g. in the carbon boiler and feeder lines.
• the problem in power boilers that produce electricity is often the high ash content of wood fuels and thereby the contamination of the boiler and the increase of the corrosion risk, as well as the after-treatment of ash.
• a functional fluidized-bed charring process and apparatus that are applicable for the production of biocarbon have not been developed before. For example, the fact that it is difficult e.g. to separate a product formed from wood and the fluidized-bed material has been conceived as a problem. Another problem has been the light structure of the product which has disturbed stable operation of a fluidized-bed reactor.
• the invention is based on a process for producing a biocarbon product from bio-based raw stock.
• the bio-based raw stock is sorted by removing in the raw stock the undesired fraction in terms of the production of biocarbon from the desired fraction of the raw stock which is used for the production of biocarbon, the desired fraction of the raw stock is fed to a fluidized-bed reactor in order to produce biocarbon, the undesired fraction of the raw stock is fed to a combustion boiler disposed in connection with the fluidized-bed reactor in order to produce energy fractions, a heat transfer material, preferably solid heat transfer particles, to be used in the fluidized-bed reactor is warmed up, e.g.
• the bio-based raw stock is heated in the fluidized-bed reactor in oxygen-free conditions to a temperature of 220 to 350 °C in the presence of the heat transfer material in order to form a solid biocarbon product, and the heat transfer material is circulated from the fluidized-bed reactor to the combustion boiler in order to warm up, such as heat, and purify the heat transfer material.
• the invention is based on an apparatus corresponding to the process for producing a biocarbon product from bio-based raw stock.
• the apparatus includes a fluidized-bed reactor in order to produce a biocarbon product and a combustion boiler in order to produce energy fractions and warm up a heat transfer material, these two being integrated together, and sorting means for the bio- based raw stock in order to sort the bio-based raw stock into a desired and undesired (19) fraction in terms of the production of biocarbon, feeding means in order to feed the desired fraction of the raw stock to the fluidized-bed reactor, and feeding means in order to feed the undesired fraction of the raw stock to the combustion boiler, means for leading the warmed-up heat transfer material from the combustion boiler to the fluidized-bed reactor, means for separating the heat transfer material from the biocarbon product that has been formed, and means for circulating the heat transfer material back to the combustion boiler in order to warm up and purify the heat transfer material.
• a biocarbon product in this context means a product to be utilized as biocarbon.
• the biocarbon product may be in this context any biocarbon product, biocarbon, biocarbon fraction, biocarbon product fraction or equivalent.
• the biocarbon may be formed from suitable raw stock, and binders and/or additives may or may not be added to it.
• the process according to the invention operates in the temperature range of 220 to 350 °C as an atmospheric pressure process and in oxygen-free state. At higher temperatures, biocarbon grades that only include a small amount of volatile matter may be produced, e.g. for coke plants.
• the biocarbon product being formed is always substantially in a solid state.
• the bio-based raw stock is cured in order to form the biocarbon product.
• the bio-based raw stock may be dried before curing to the moisture of approximately 10 to 15 %. The drying may be performed by utilizing waste heat of the apparatus or the plant .
• the fluidized-bed reactor to be used for the production of biocarbon is combined with the combustion boiler which is used to produce energy and preferably to warm up and/or purify the heat transfer material, to treat the possible residual fractions developed in the production of biocarbon and/or to produce energy from lower-grade starting material.
• the combustion boiler may be a separate combustion boiler for the production of energy or a combustion boiler of the power station or equivalent.
• the fluidized-bed reactor designated for the production of biocarbon is a supplementary apparatus in the boiler of the power station.
• the annual variations of the combustion boiler e.g.
• a traditional CHP power station may be utilized by the integrated fluidized-bed reactor and combustion boiler connection, so that during summer time when low energy demand, such as low steam load, prevails, a large biocarbon production capacity is provided.
• the energy fractions to be formed in the combustion boiler may include heat, electricity, steam, combustion gases or the equivalent.
• the heat may be bound e.g. to the heat transfer material and conducted by the heat transfer material to a desired destination .
• heat is brought to the production of a biocarbon product by the solid heat transfer material.
• heat may be brought to the production of the biocarbon product by fluidizing the fluidized bed with hot oxygen-free or low-oxygen circulating gases or combustion gases of the boiler.
• the use of superheated steam is possible as a heat-bearing material.
• the solid heat transfer material preferably in the form of particles, may be heated to a desired temperature of 300 to 1000 in the combustion boiler and/or outside the boiler, e.g. by guiding the heat transfer material through a separate heat exchanger and warming it up by hot combustion gases.
• the combustion gases may come from the combustion boiler or any suitable thermal reactor.
• the heat transfer material is led into contact with the bio- based raw stock in the fluidized-bed reactor in order to provide direct transfer of heat.
• the heat transfer material acts at the same time as the fluidized-bed material of the fluidized-bed reactor either alone or with another bed material.
• the heat transfer material is led to a heat exchanger provided inside the fluidized-bed reactor.
• suitable bed material is used in the fluidized-bed reactor as the fluidized-bed material, or the fluidized bed is formed only by the bio-based raw stock.
• the heat transfer material is led to a separate heat transfer material bed or heat transfer bed, e.g. a woodchip bed or equivalent, of the fluid- ized-bed reactor.
• the transfer of heat from the heat transfer material to the bio-based raw stock may take place directly by the heat transfer material or indirectly through a heat exchanger or other separate heat transferring means accommodated within the fluidized bed.
• the heat transfer material is separated from the biocarbon product that has been formed, and it is circulated to the combustion boiler.
• a separator may be provided either in the fluidized-bed reactor or thereafter in order to separate the biocarbon product from the heat transfer material and/or the bed material. In one embodiment part of the separated biocarbon product is returned to the bottom of the fluidized-bed reactor .
• the bio- based raw stock is selected from the group of: wood, wood-based raw stock, straw, different herbaceous bio- masses, biosludge, other solid biomass materials and other types of bio-based raw stock and their combinations.
• the combustion boiler produces energy for the fluidized-bed reactor, e.g. from the undesired raw stock and/or other starting materials .
• the bio- based raw stock is heated in the fluidized-bed reactor with a dwell time of less than 30 minutes, more preferably less than 20 minutes, and most preferably less than 5 minutes, in order to form a solid biocarbon product.
• a dwell time of less than 5 min is reached instead of the dwell time of 20 to 30 min of the conventional shaft kilns. This implies smaller and less expensive fluidized-bed reactors for the production of biocarbon.
• the dwell time may be influenced by the particle size of the feed. For example, for the homogeneous carbonization of wood it is required that the inner part of the woodchip particle reaches the desired end temperature.
• the temperature profile of the particle on its surface and inside of it may be described as a func- tion of the particle size and the heat-transfer coefficient .
• bio-based raw stock is crushed to a desired particle size before it is fed to the fluidized-bed reactor.
• the bio- based raw stock is dried before producing the biocar- bon product, preferably with energy obtained from the combustion boiler and/or by energy fractions, e.g. combustion gas or steam, or by the combustion gas developed in the process using direct or indirect transfer of heat.
• energy fractions e.g. combustion gas or steam
• Production i.e. a production step, of biocarbon or a biocarbon product means in this context specifically treatment of the bio-based raw stock in the fluidized-bed reactor in order to form a biocarbon product .
• the apparatus includes sorting means for the bio-based raw stock.
• the best raw stock may be sorted for the production of biocarbon and the undesired raw stock may be sorted for burning in order to form energy.
• the integrated connection of the fluidized-bed reactor to the combustion boiler e.g. a combustion boiler of the power station, gives a possibility to classify the biomaterial coming to the station according to the ash content or the content of harmful materials.
• the intention is to lead only the low-ash, low- alkali and low-chlorine raw stock to the production of biocarbon.
• the less favorable and undesired fraction of the bio-based raw stock e.g. the needles, the bark and the equivalent, may be led directly to the combustion boiler for the production of energy.
• the apparatus includes a classifier in order to sort the bio-based raw stock into a desired and undesired fraction in terms of the production of biocarbon.
• the desired fraction is guided to the production of biocarbon and the undesired fraction is guided to the combustion boiler.
• the operation of the classifier may be based on density, mechanical screening, color difference measurement or determination of the chemical composition, e.g. on an NIR infra-red detector.
• the classifier provides for the production of different bio- carbon grades from different kinds of raw stock according to the end use requirements of the biocarbon. Typically, in power stations that use carbon and have high primary steam values, high ash, alkali or chlorine contents are not allowed.
• the residual and/or minor flows formed in the production of the biocarbon product are burnt in the combustion boiler in order to produce energy fractions.
• the odorous gases and other residual flows of the process may be burnt in the combustion boiler.
• energy fractions are fed from the combustion boiler to the fluidized- bed reactor in the form of the heat transfer material, steam, heat and/or electricity.
• binders and/or additives are added to the biocarbon product that has been formed in order to provide the final biocarbon product.
• suitable binders are added to biocarbon for binding the ash compounds that cause corrosion or scorification and/or in order to form pellets.
• additives that ameliorate the weatherproofness of the product such as olefine plastics that are unqualified for recycling, e.g. f-rom package waste, may be added to the biocarbon in addition to the optional binder. It is also possible to add e.g. lime to the biocarbon product for desulphuri- zation of the power stations.
• biocarbon of a good quality may be formed cost-effectively. Thanks to the invention, it is possible to utilize different types of raw stock and raw stock components which may not have been utilized cost-effectively before.
• the process and the apparatus according to the invention are substantially less expensive in production costs than the known biocarbon production processes, and the obtained product is a granulated biocarbon fuel that is purer and richer in energy than before .
• the apparatus includes a drier 5, wherein the fraction of the bio-based raw stock selected for the production of biocarbon is dried by hot combustion gases 16 to the moisture of approximately 10 to 15 % at a temperature of 40 to 100 °C before feeding the raw stock to the fluidized-bed reactor 1.
• the bio-based raw stock may also be washed, if desired, before the production of the biocarbon product in order to lower . the ash content .
• the apparatus includes means for leading a heat transfer material 6 that has been heated in the combustion boiler from the combustion boiler 2 to the fluidized-bed reactor 1. In this apparatus the heated heat transfer material 6 is led to the raw stock 18 selected for the production of the biocarbon product in the fluidized-bed reactor, i.e.
• the raw stock 18 is heated by the heat transfer material 6 in oxygen-free conditions to a temperature of 220 to 350 °C in order to form a solid biocarbon product.
• the fluidized-bed reactor there may be fluidized-bed sand in addition to the heat transfer material in order to form the fluidized bed, or alternatively the heat transfer material may act alone as the fluidized-bed material, forming the fluidized bed.
• the apparatus includes a separator cyclone 4 in order to separate the biocarbon product 9 and 10 from the heat transfer material 7 and the fluidized- bed material 8 after the formation of the biocarbon product. Part of the separated biocarbon product 9 is returned to the bottom of the fluidized-bed reactor 1. The rest of the biocarbon 10 is led to pelletizing in order to form biocarbon pellets, wherein binders and desired additives may be added to the biocarbon product.
• the apparatus includes means for circulating the heat transfer material 7 back to the combustion boiler 2 in order to heat and purify the heat transfer material.
• a desired type of raw stock 17 may be fed to the combustion boiler 2 in addition to the fraction 19 rejected from the production of biocarbon in order to form energy fractions.
• a possibility to feed air to the combustion boiler may be provided in the combustion boiler.
• the combustion gases 11 are circulated via a filter 12 to the combustion boiler 2 as a combustion gas flow 13 in order to form energy fractions, to the fluidized-bed reactor 1 as a combustion gas flow 15 and/or to the drier 5 as a combustion gas flow 16 in order to dry the raw stock, and/or are led out of the process 14.

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• 2009
  • 2009-10-13 FI FI20096059A patent/FI20096059A0/fi not_active Application Discontinuation
• 2010
  • 2010-10-13 WO PCT/FI2010/050796 patent/WO2011045473A1/en active Application Filing
  • 2010-10-13 CA CA2777339A patent/CA2777339A1/en not_active Abandoned
  • 2010-10-13 EP EP10823103.6A patent/EP2488604A4/de not_active Withdrawn

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