WO2008136475A1 - バイオコークス製造装置及び方法 - Google Patents
バイオコークス製造装置及び方法 Download PDFInfo
- Publication number
- WO2008136475A1 WO2008136475A1 PCT/JP2008/058226 JP2008058226W WO2008136475A1 WO 2008136475 A1 WO2008136475 A1 WO 2008136475A1 JP 2008058226 W JP2008058226 W JP 2008058226W WO 2008136475 A1 WO2008136475 A1 WO 2008136475A1
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- WIPO (PCT)
- Prior art keywords
- biomass
- reaction
- reaction vessel
- bio
- pulverized
- Prior art date
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Classifications
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- 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
-
- 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
- C10B47/02—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge
- C10B47/12—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with stationary charge in which the charge is subjected to mechanical pressures during coking
-
- 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
- C10L5/40—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
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- 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
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
Definitions
- the present invention relates to a technology for producing bio-coke using biomass as a raw material, and in particular, a bio-coke production apparatus capable of industrially mass-producing bio-coke that can be effectively used as an alternative fuel for coal-coke, and Regarding the method.
- Background art
- biomass fuels is organic matter resulting from photosynthesis, and includes biomass such as wood, vegetation, crops, and moss. By converting this biomass into fuel, it can be used effectively as an energy source or an industrial raw material.
- Patent Document 1 Japanese Patent Publication No. 61-27473-5
- the water content of the chopped organic fiber material is adjusted to 16 to 28%, and this is compressed in a die and dried to produce a fuel pellet.
- Patent Document 2 Japanese Patent Laid-Open No. 2 003-2 0 6 4 90.
- biomass is heated at 20 to 500 ° C., preferably 25 to 400 ° C. in an oxygen-deficient atmosphere to produce a biomass semi-carbonized consolidated fuel precursor. It has become a way to do.
- biomass is converted into fuel by performing compression molding.
- the generated fuel pellet has a large amount of water and thus generates a small amount of heat, and is not suitable as a fuel.
- An object of the present invention is to provide a bio-coke manufacturing apparatus and method capable of efficiently mass-producing bio-coke in view of the above-mentioned problems of the prior art.
- the raw material biomass used in the bio-coke production apparatus and method according to the present invention may be a biomass raw material resulting from photosynthesis, and examples thereof include woody materials, herbaceous plants, agricultural crops, and potatoes. .
- biomass resulting from photosynthesis is a material that produces organic substances such as sugars, cellulose, and lignin by performing photosynthesis in the sunlight using carbon dioxide in the atmosphere and water sucked up from the roots.
- Bio-coke is produced by holding biomass material under pressure and heating for a certain period of time and then cooling.
- the pressure and heating conditions are set to a pressure range and a temperature range in which hemicellulose in the pulverized biomass is thermally decomposed and induces a lignin thermosetting reaction.
- the following reaction mechanism is established, and pio-coke having high hardness and high heat generation can be produced.
- the reaction mechanism is as follows. Hemicellulose is thermally decomposed to exhibit an adhesive effect, and lignin reacts at a low temperature while maintaining its skeleton by superheated water vapor generated in the reaction vessel, and works synergistically with the compaction effect to achieve high hardness Can produce bio-coke with high calorific value.
- the thermosetting reaction proceeds when reaction active sites are induced between phenolic polymers contained in lignin and the like.
- Figure 7 shows a table comparing the physical properties of bio-coke with other fuels. This table only describes experimentally obtained numerical values, and the present invention is not limited to these numerical values.
- the biocoke has an apparent specific gravity of 1.2 to 1.38, maximum compressive strength of 60 to 200MPa, and calorific value of 18 to 23MJ kg. Excellent hardness and flammability Compared with raw woody biomass, which has a specific gravity of about 0.4 to 0.6, a calorific value of about 17 MJ / kg, and a maximum compressive strength of about 3 OMP a, the calorific value and hardness It can be seen that this is far superior. Compared to physical properties of coal coke, apparent specific gravity of about 1.85, maximum compressive strength of about 15 MPa, and calorific value of about 29 MJ kg, bio-coke has performance comparable to flammability and hardness. Have.
- bio-coke is an effective fuel as an alternative to coal-coke and has a high utility value as a material material.
- the present invention proposes an apparatus and a method for efficiently producing the above-described biocokes.
- the present invention relates to a bio-coke production process in which a biomass raw material resulting from photosynthesis is pulverized and moisture-adjusted to a predetermined moisture content is subjected to pressure molding while heating in a reaction vessel to produce bio-coke.
- the reaction vessel has a pressure range and a temperature range in which hemicellulose in the pulverized biomass is thermally decomposed and lignin induces a thermosetting reaction, and pressurizing means for pressurizing to the pressure range; Heating means for heating to a temperature range; A cooling means for cooling after being held for a certain period of time in a pressurized and heated state, and a discharging means for discharging the generated bio-coke after the cooling,
- a plurality of the reaction containers are provided, and a powder material transport path for transporting the biomass crushed material is provided above the reaction containers, and the plurality of reaction containers are connected to the powder material transport path via a connecting pipe.
- the connecting pipe is provided with pulverized material charging means for charging a predetermined amount of biomass pulverized material from the powder material transporting path in accordance with the timing of charging the powdered material into the reaction vessel.
- bio-coke that can be used as an alternative to coal-coke can be efficiently produced.
- Large powder feeders such as pulverizers and powder hoppers can also be configured by transferring biomass powder through a powder dust transport path and charging biomass powder into multiple reaction vessels as needed. Can be fixed and installed without moving the reaction container on the receiving side, so that the apparatus can be simplified and miniaturized.
- At least two reaction sequences in which the plurality of reaction vessels are arranged in a straight line are provided, and the pulverized material conveyance path is installed in a straight line along the reaction sequence, and an end portion thereof It is characterized in that a circulation path is formed by connecting with adjacent lines.
- the installation area of the apparatus can be reduced. It can be made small and space can be saved.
- the said powdered material conveyance path is a closed-type pipe-shaped conveyor, so that even a fluid pulverized material can be reliably conveyed, and the powdered material is a closed system. Can be prevented from scattering.
- the pulverized material charging means includes an upper gate and a lower gate which are provided at different positions in the vertical direction of the connection pipe and are opened and closed according to the charging timing, and a biomass powdered material provided between these gates.
- Position detection sensor that detects quantity Narana
- the upper gate and the lower gate are controlled to open and close based on the detected amount of pulverized biomass, and the amount of biomass pulverized material charged into the reaction vessel and the timing of charging are adjusted.
- the biomass pulverized material charging means has a double gate structure equipped with a position detection sensor, and the gate is controlled to open and close based on the biomass pulverized material amount detected by the position detection sensor. By doing so, it becomes possible to feed a predetermined amount of biomass powder into the reaction vessel at an accurate charging timing with a simple configuration.
- the pulverized material charging means includes a weight sensor disposed at the bottom of the reaction vessel, and the weight of the biomass powder detected by the weight sensor, It is characterized by comprising input amount adjusting means for adjusting the input amount.
- the input amount is adjusted based on the weight detected by the weight sensor, so that a predetermined amount of biomass powder can be obtained with a simple configuration as in the above-described invention. It is possible to put the product into the reaction vessel.
- reaction vessel has a double-pipe structure, a biomass pulverized product is introduced into the inner cylinder, and a cooling / heating medium passage through which a heat medium or refrigerant flows is provided between the inner cylinder and the outer cylinder.
- the cooling medium passage is connected to a heating medium circuit that heats the heating medium and a refrigerant circuit that includes a heat exchanger that cools the refrigerant with cooling water,
- a refrigerant tank having a volume for cooling the refrigerant to a boiling point of water or less is provided upstream of the heat exchanger in the refrigerant circuit.
- the present invention it is possible to prevent the cooling water supplied to the heat exchanger of the refrigerant circuit from boiling, to operate safely and smoothly, and to operate with a minimum amount of cooling water. It becomes possible.
- a biomass raw material resulting from photosynthesis is pulverized, and a biomass pulverized product whose water content is adjusted to a predetermined moisture content is pressurized while being heated in a reaction vessel.
- a biocokes production method for producing bio-coke by molding, wherein a plurality of the reaction vessels are installed and a crushed material conveyance path for conveying the biomass crushed material is provided,
- a pressure range and a temperature range in which hemicellulose in the biomass powder is thermally decomposed and lignin induces a thermosetting reaction are set in advance,
- a series of treatment steps are performed in which the biomass pulverized product is pressurized and heated to the pressure range and the temperature range in each reaction vessel, held for a certain period of time, then cooled, and the generated bio-coke is discharged.
- a predetermined amount of the pulverized biomass is introduced into the corresponding reaction vessel from the powdery soot conveyance path in accordance with the timing of the powdery soy sauce in the process.
- the heating step and the pressurizing step in the reaction vessel may be started at the same time, or the start timing may be shifted. In other words, it includes all cases where heating and pressurization are started at the same time to maintain this heating / pressurization state, heating and holding after pressurization, and holding after pressurization and pressurization.
- the heating is performed by supplying a heat medium to the reaction vessel, and the cooling is performed by supplying a refrigerant,
- At least the timing of the heating and the cooling is different for each reaction vessel.
- the processing steps are performed in a plurality of reaction vessels with a time difference, and the load on the heat transfer medium circuit and the refrigerant circuit is reduced by changing the supply timing of the heat transfer medium or the refrigerant for each reaction vessel. It is possible to reduce the size of the cooling medium circuit.
- bio-coke having high hardness and high calorific value that can be used as an alternative to coal coke.
- a large supply device such as a pulverizer or powder hopper, and multiple reactions on the receiving side Containers can be fixedly installed, simplifying and downsizing the equipment Is possible.
- the reaction vessel is heated and cooled by a cooling medium, and a refrigerant tank having a volume for cooling the refrigerant to the boiling point of water or less is provided upstream of the heat exchanger of the refrigerant circuit that supplies the refrigerant.
- a refrigerant tank having a volume for cooling the refrigerant to the boiling point of water or less is provided upstream of the heat exchanger of the refrigerant circuit that supplies the refrigerant.
- FIG. 1 is a plan view of a bio-coke production apparatus according to an embodiment of the present invention.
- FIG. 2 is a side sectional view of the bio-coke production apparatus shown in FIG.
- FIG. 3 is a perspective view showing the powdered material conveying apparatus of the present embodiment.
- FIG. 4 is a diagram showing the internal structure of the pulverized material conveying apparatus of this example.
- FIG. 5 is a side sectional view showing the reaction vessel of this example.
- FIG. 6 is an equipment system diagram including the cooling medium circuit of the present embodiment.
- Fig. 7 is a table comparing the physical properties of bio-coke. BEST MODE FOR CARRYING OUT THE INVENTION
- FIG. 1 is a plan view of a bio-coke production apparatus according to an embodiment of the present invention
- FIG. 2 is a side sectional view of the bio-coke production apparatus shown in FIG. 1
- FIG. 4 is a diagram showing the internal structure of the powdered material transfer device of the present embodiment
- FIG. 5 is a side sectional view showing the reaction container of the present embodiment
- FIG. 6 includes a cooling medium circuit of the present embodiment. It is an equipment system diagram.
- the biomass that is the raw material for bio-coke is organic matter resulting from photosynthesis, such as wood, grass, crops, and potatoes.
- organic matter resulting from photosynthesis such as wood, grass, crops, and potatoes.
- waste wood, thinned wood, pruned branches, etc. Plants, agricultural wastes, and coffee wastes such as coffee and tea.
- the biomass is adjusted in advance so that the biomass has a predetermined moisture content
- the raw material is a pulverized biomass that has been pretreated so as to be powdered to a predetermined particle size or less.
- the bio-coke apparatus of the present embodiment is to produce bio-coke by cooling the biomass powder after pressing and heating under a predetermined pressure and temperature conditions for a certain period of time.
- the pressure and temperature conditions described above are the pressure range and temperature range that induce thermal decomposition or thermo-rich reaction of hemicellulose and lignin in the biomass powder. That is, the hemicellulose in the biomass pulverized product is thermally decomposed and the lignin is in a pressure range and a temperature range in which a thermo-rich reaction is induced.
- the main components of the bio-coke production apparatus are as follows: a reaction vessel 1 for producing bio-coke by carrying out the above-mentioned reaction with biomass powder, and a crushed material conveyor 2 for conveying the pulverized biomass to be charged into the reaction vessel 1
- a plurality of the reaction vessels 1 are installed, and a crushed material transport conveyor 20 is provided above them.
- two reaction sequences in which a plurality of reaction vessels 1 are arranged in a straight line are provided in parallel, and the pulverized material conveyor 20 is arranged in a straight line along the reaction sequence.
- the end of the crushed material conveyor 20 is connected to the adjacent line.
- a pulverized material hopper 22 is provided on one end side of the pulverized material conveyance conveyor, and the biomass powder in the conveyor 20 is supplied and discharged.
- FIG. 3 and 4 show a specific configuration example of the powdered material transfer conveyor 20.
- a closed pipe-shaped conveyor is used as the powdered material transfer conveyor 20.
- Figure 4 shows the internal structure of the pipe conveyor.
- the conveyor 20 includes a cylindrical casing 20 1, a chain 2 0 2 threaded in the casing 2 0 1, and a chain 2 0 2 fixed to the shaft of the casing 2 0 1
- a plurality of blades 203 provided so as to partition the inside of the casing 20 1 on a substantially vertical cross section with respect to the direction.
- the chain 20 2 is moved by the driving device 21 and the blade 20 3 is moved accordingly. Biomass powder supplied between the blades 20 3 is conveyed through the casing 20 1 as being pushed by the blades 20 3.
- the pulverized material transport conveyor 20 is provided with a powder supply unit 2 1 a and a pulverized material discharge unit 2 1 b at a position corresponding to the pulverized product hopper 2.
- a predetermined amount of biomass powder is supplied to the conveyor from the pulverized material hopper 22 at the material supply unit 21a, and the biomass pulverized material remaining in the conveyor is discharged at the powder material discharge unit 21b. ing.
- an opening (not shown) is provided at the position corresponding to the reaction container 1 on the powder container conveyor 20 to put the biomass powder into the reaction container 1, and the powder material conveyor 2 A plurality of reaction vessels 1 are connected to 0 via a connecting pipe 4 shown in FIG.
- FIG. 5 shows a specific configuration example of the reaction vessel 1.
- the reaction vessel 1 has a cylindrical reaction cylinder 2 into which biomass powder is charged, and the reaction cylinder 2 and the powder carrier conveyor 20 are connected by a connecting pipe 4.
- Connection pipe 4 is extended vertically, but installed at a position deviated from the central axis of reaction cylinder 2.
- the lower part of the connecting pipe 4 and the upper opening of the reaction cylinder 2 are connected by a connecting part ⁇ .
- the upper part of the connecting pipe 4 is connected to a powdered material conveying path 20 extending in the 7K flat direction, and the biomass powdered material conveyed in the pulverized material conveying path 20 is appropriately supplied into the connecting pipe 4. It has come to be.
- the connecting pipe 4 is provided with pulverized material charging means for appropriately charging a predetermined amount of biomass powder into the reaction cylinder 2.
- the pulverized material charging means includes an upper gate 5A and a lower gate 5B provided at different positions with respect to the vertical direction of the connecting pipe 4, and position detection sensors 6a and 6b installed between these gates. It consists of.
- the upper gate 5A and the lower gate 5B are opened and closed by a control device (not shown).
- Position detection sensors 6a and 6b are provided between the upper gate 5A and the lower gate 5B to detect the amount of pulverized biomass.
- two position detection sensors are provided at different positions with respect to the vertical direction, but this configuration is particularly suitable if the number and position can detect the amount of biomass powder filled between the gates. Not limited.
- the pulverized material charging means operates in accordance with the timing of charging the powdered material into the reaction vessel 1. That is, before the pressurization and heating process in the reaction cylinder 2, first, the lower gate 5B is closed and the upper gate 5A is opened, and the biomass powder is dropped onto the lower gate 5B from the powder conveyance path 20. Let When the pulverized material accumulates on the lower gate 5B, the amount of accumulation is detected by the position detection sensors 6a and 6b. When it is detected that the dust has accumulated up to the position detection sensor 6a located above, the upper gate 5A is closed and the lower gate 5B is opened. As a result, a predetermined amount of biomass powder is introduced into the reaction cylinder 2.
- This operation is performed while the reaction process is being performed in the reaction cylinder 2 to prepare biomass pulverized material to be used for the next reaction process. As soon as the coatus is discharged, it is preferable to open the lower gate 5 B and put the biomass powder into it, so that the operation time can be shortened.
- a configuration may be adopted in which a weight sensor (not shown) is disposed at the bottom of the reaction vessel 1.
- the amount of biomass powder in the reaction vessel 1 is adjusted based on the weight of the pulverized biomass detected by the weight sensor. To do.
- the adjustment of the input amount is performed, for example, by providing a gate between the pulverized material conveyance path 20 and the connection pipe 4 and opening and closing the gate.
- the pressurizing means includes a pressurizing hydraulic cylinder 8 and a pressurizing piston 9 reciprocated by the hydraulic cylinder 8. These are arranged coaxially with the reaction cylinder 2.
- the pressurizing piston 9 preferably has a movable range up to the bottom surface of the reaction cylinder 2.
- the pressurizing piston 9 is configured to be able to maintain this pressurized state for a predetermined time.
- the reaction cylinder 2 includes heating means for heating the contents to a predetermined temperature, and cooling means for cooling after the heating.
- the heating means and the cooling means may be the same temperature adjusting means.
- the temperature adjusting means has a double pipe structure in which a jacket is provided in the reaction cylinder 2 and a cooling medium passage 3 is provided between the inner cylinder and the outer cylinder.
- a heating medium or refrigerant (hereinafter referred to as a cooling / heating medium) flows through the cooling / heating medium passage 3, and heat energy is applied to the biomass powder filled in the cylinder inner cylinder by the cooling / heating medium.
- a cooling medium inlet 3 a is provided below the cooling medium passage 3, and a cooling medium outlet 3 b is provided above the cooling medium passage 3.
- the cooling medium inlet 3 a and the cooling medium outlet 3 b are connected to a cooling medium circuit described later (see FIG. 6). Furthermore, a discharge device 10 for discharging the contents is provided on the bottom surface of the reaction cylinder 2.
- the discharge device 10 includes a bottom cover portion 11 that seals the bottom opening of the reaction cylinder 2, an extrusion piston 12 that moves the bottom cover portion 11 in the horizontal direction, and a discharge device that drives the extrusion piston. It consists of hydraulic cylinders 1 and 3. After the cooling process is completed in the reaction cylinder 2, the discharge device 10 moves the bottom cover portion 11 by the extrusion piston 1 2 to open the bottom opening of the reaction cylinder 2, and biocoke in the cylinder 2 is dropped and discharged. At the time of brewing, the biocoke may be pushed out from above by the pressurized piston 9 and dropped.
- the discharged bio-coke is placed on the product conveyor 23 shown in FIGS. 1 and 2 and conveyed.
- the product conveyor 2 3 may be provided directly under the reaction vessel 1, or as shown in the present example, installed between the two reaction sequences and dropped from each reaction vessel 1.
- the operation of the bio-coke production apparatus having the above configuration will be described including the operation method.
- the numerical ranges such as temperature, pressure, moisture content, size, etc. described here are suitable examples in this apparatus, but are not limited thereto.
- biomass powder As a pretreatment of biomass powder as a raw material, moisture adjustment is performed to dry the moisture content of the biomass to 5 to 10%, and the dried biomass is a particle size of 3 mm or less, preferably 0.1 mm or less. Grind into. Some types of biomass are conditioned after drying and flouring. As a result, when the biomass is filled into the reaction cylinder 2, the bulk density is improved and uniform filling becomes possible, the contact between the biomass is increased in the thermoforming, and the hardness after the molding is also improved.
- the pulverized biomass is put into the powdered rice cake 2 2 2.
- the biomass pulverized material stored in the pulverized material hopper 22 is appropriately supplied to the pulverized material transport conveyor 20.
- the pulverized biomass is transported while circulating in the powder conveyor 20.
- a predetermined amount of pulverized biomass is introduced into the reaction vessel 1 through the connecting pipe 4 as necessary from the powdered material conveyor 20.
- the pressurizing piston 9 is driven by the pressurizing cylinder 8, and the pressurizing piston 9 adds the biomass powder in the reaction cylinder 2 to 8 to 25 MPa. Press to compress.
- a heating medium is passed through the cooling medium passage 3 of the reaction cylinder 2 and the biomass powder in the cylinder 2 is heated to 115 to 30 ° C.
- the inside of the reaction cylinder 2 may be heated in advance and then pressurized, or conversely, it may be heated after being pressurized, and heating and pressurization are performed almost simultaneously.
- the temperature, pressure, and water content described above are set within a range in which the hemicellulose and lignin in the biomass powder are thermally decomposed or a thermosetting reaction is induced.
- the hemicellulose in the biomass of the biomass is thermally decomposed and lignin induces a thermosetting reaction.
- the moisture content is in a range sufficient for moisture to form a subcritical state in the cylinder.
- the biomass powder in the reaction cylinder 2 maintains the above-mentioned pressurization and heating state for a certain period of time. For example, if the cylinder diameter is 50 mm, the holding time is 10 to 20 minutes, In the case of 1 50 mm, it is 30 to 60 minutes.
- thermosetting reaction proceeds when reaction active sites are induced between phenolic polymers contained in lignin and the like.
- the heat medium is removed from the cooling medium passage 3 of the reaction cylinder 2 and the refrigerant is allowed to flow.
- silicon oil and steam are preferably used as the heat medium
- silicon oil, water, or air is preferably used as the refrigerant.
- the push-out piston 12 is driven by the discharge hydraulic cylinder 13 to open the bottom cover portion 11 of the reaction cylinder 2, and the content is pushed out from above by the pressure piston 9 and discharged.
- the discharged content is a bio-coke product, and the bio-coke product is transported by a product conveyor 23 and collected.
- bio-coke production apparatus and method of the present embodiment it is possible to efficiently produce high-hardness and high calorific bio-coke that can be used as an alternative to coal coke.
- the bio-cox produced in this example can be used as a heat source / reducing agent in cubora, blast furnaces, etc. It can also be used as a material material by taking advantage of its high compressive strength and other characteristics.
- the present embodiment it is possible to operate continuously by installing a plurality of reaction vessels 1, and it becomes possible to industrially mass-produce biocoke.
- a large-sized supply device such as 2 and a plurality of reaction vessels 1 on the receiving side can be fixedly installed, and the device can be simplified.
- reaction vessels 1 are arranged close to each other in a straight line, and the pulverized material transfer conveyor 2 is arranged in a straight line along the line to circulate, thereby reducing the installation area of the apparatus and saving space. Is possible.
- a double gate structure equipped with position detection sensors 6a and 6b is used, and the gate is controlled to open and close based on the amount of biomass powder detected by the position detection sensor.
- a weight sensor provided at the bottom of the reaction cylinder 2 is used to detect the weight of the dust in the cylinder and adjust the input based on this weight. With the configuration, a predetermined amount of pulverized biomass can be charged into the reaction vessel 1.
- a metal material having high thermal conductivity for at least one of the upper and lower surfaces of the reaction vessel 1.
- a metal material having high thermal conductivity is used for the pressure pistons 9 and Z or the bottom cover 11.
- copper and silver are preferably used.
- the high thermal conductivity material is disposed so as to contact the outer periphery of the reaction cylinder 2.
- cooling medium circuit of the present embodiment will be described with reference to FIG.
- the method of switching between heating and cooling of the reaction cylinder 2 is performed.
- a temperature adjusting means having a step is an essential component. Therefore, by providing a cooling medium circuit as shown in FIG. 6, it is possible to provide temperature control means with high thermal efficiency and high safety.
- silicon oil is used as a refrigerant and a heat medium will be described.
- the cooling medium inlet 3 a and the outlet 3 b of the reaction cylinder 2 are connected to a cooling medium circuit 30 shown in FIG.
- the cooling medium circuit 30 is configured by combining a refrigerant circuit and a heating medium circuit.
- the cooling medium outlet 3 b is connected to the cooling medium discharge line 4 1 and branches to the heating medium return line 4 2 and the refrigerant return line 4 3 via the three-way valve 4 5 on the discharge line 4 1. Yes.
- the heat medium return line 4 2 is connected to the heat medium tank 3 1.
- the heat medium tank 31 includes a heater 3 1 a and a stirrer 3 1 b so as to raise the temperature of the cooled heat medium.
- N 2 Bonn Bekara N 2 gas is supplied, it is preferable to ensure safety holds the tank in an inert atmosphere.
- the outlet side of the heating medium tank 31 is connected to the cooling medium supply line 40 via a three-way valve 46.
- the heat medium circulates to the heat medium tank 3 1 side by the three-way valves 4 5 and 4 6, and the heat medium tank 3 1 and the cooling medium supply line 4 0, a cooling medium passage 3 (reaction cylinder 2), a cooling medium discharge line 41, and a heating medium return line 42 are formed.
- the refrigerant return line 4 3 is connected to the refrigerant heat exchanger 3 6.
- the refrigerant heat exchanger 36 is configured to exchange heat between cooling water such as clean water and the refrigerant to cool the refrigerant.
- a refrigerant tank 35 is provided upstream of the refrigerant heat exchanger 36 in the refrigerant return line 43.
- This refrigerant tank 35 has an ability to cool at least the refrigerant temperature to the boiling point of water or lower, preferably 80 ° C. or lower.
- the refrigerant tank 35 has a capacity for cooling to the above temperature.
- the refrigerant tank 35 includes a stirrer 35 a, which improves the cooling capacity.
- the temperature when the reaction cylinder 2 is heated is as high as 1 15 to 2 30 ° C, and a high-temperature cooling medium can be introduced into the refrigerant heat exchanger 36 when the cooling medium is switched. There is sex. As a result, the cooling water of the refrigerant heat exchanger 36 will boil, which may cause problems such as equipment failure. Although it is possible to adopt a configuration in which the cooling water does not boil depending on the design conditions of the refrigerant heat exchanger 36, in that case, it is necessary to increase or pressurize the cooling water flow rate, which is not efficient.
- the refrigerant heat exchanger 3 is provided by providing a refrigerant tank 35 having an ability, preferably a volume, to cool the refrigerant to the boiling temperature or lower on the upstream side of the refrigerant heat exchanger 36. It is possible to prevent the cooling water from boiling 6 and to operate safely and smoothly, and to operate with a minimum amount of cooling water.
- At least the timing of the heating step and the cooling step among the treatment steps in the plurality of reaction vessels 1 is different for each reaction vessel. That is, when the heating process is performed in one reaction vessel, the cooling process is performed in the other reaction container.
- bio-coke production apparatus and method it is possible to efficiently produce high-hardness and high calorific bio-coke that can be used as an alternative to coal coke.
- bio-cooks produced in this example can be used as a heat source, reducing agent, etc. in cubora and blast furnaces in the manufacture of steel and iron making, and by utilizing the characteristics such as high compressive strength, It can also be used.
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP08740912.4A EP2143780A4 (en) | 2007-04-27 | 2008-04-22 | BIOCOKE PRODUCTION EQUIPMENT AND METHOD THEREOF |
US12/597,662 US8460515B2 (en) | 2007-04-27 | 2008-04-22 | Biocoke producing apparatus and process therefor |
CN2008800135088A CN102015977B (zh) | 2007-04-27 | 2008-04-22 | 生物炭生产设备及用于生产生物炭的工艺 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2007-119268 | 2007-04-27 | ||
JP2007119268A JP2008274108A (ja) | 2007-04-27 | 2007-04-27 | バイオコークス製造装置及び方法 |
Publications (1)
Publication Number | Publication Date |
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WO2008136475A1 true WO2008136475A1 (ja) | 2008-11-13 |
Family
ID=39943582
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2008/058226 WO2008136475A1 (ja) | 2007-04-27 | 2008-04-22 | バイオコークス製造装置及び方法 |
Country Status (5)
Country | Link |
---|---|
US (1) | US8460515B2 (ja) |
EP (1) | EP2143780A4 (ja) |
JP (1) | JP2008274108A (ja) |
CN (1) | CN102015977B (ja) |
WO (1) | WO2008136475A1 (ja) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2011143718A1 (en) * | 2010-05-21 | 2011-11-24 | Errol John Smith | Biochar-coke produced in an energy efficient manner |
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JP5547420B2 (ja) * | 2008-10-27 | 2014-07-16 | 学校法人近畿大学 | バイオコークス製造方法及び製造装置 |
JP5458219B2 (ja) * | 2011-05-23 | 2014-04-02 | Jfeエンジニアリング株式会社 | 廃棄物溶融処理方法及び廃棄物溶融炉の石炭コークス使用量削減方法 |
CA2838470C (en) * | 2011-06-21 | 2019-08-06 | Commonwealth Scientific And Industrial Research Organisation | Apparatus and process for continuous carbonisation of wood chips or wastes and other charring organic materials |
US10364393B2 (en) | 2011-06-23 | 2019-07-30 | Commonwealth Scientific And Industrial Research Organisation | Process and apparatus for continuous production of densified charcoal |
JP5811501B2 (ja) * | 2011-11-17 | 2015-11-11 | Jfeエンジニアリング株式会社 | 廃棄物溶融処理方法 |
JP5335062B2 (ja) * | 2011-12-20 | 2013-11-06 | 株式会社ナニワ炉機研究所 | 燃焼装置 |
JP5437403B2 (ja) * | 2012-01-13 | 2014-03-12 | 株式会社ナニワ炉機研究所 | 流体加熱装置 |
JP2013184175A (ja) * | 2012-03-06 | 2013-09-19 | Chugai Ro Co Ltd | 加圧加熱成形装置 |
CN103509621A (zh) * | 2012-06-15 | 2014-01-15 | 北京泛欧瑞得科技有限公司 | 一种先炭化后成型高效生物质燃料的制备工艺 |
KR101315522B1 (ko) * | 2012-09-19 | 2013-10-08 | 주식회사 유니바이오 | 커피박을 이용한 저흡수성 연료용 분탄 및 그 제조방법 |
JP5611424B2 (ja) * | 2013-07-29 | 2014-10-22 | 株式会社ナニワ炉機研究所 | 燃焼装置 |
CN104164243A (zh) * | 2014-08-08 | 2014-11-26 | 广东省宜华木业股份有限公司 | 木材加工剩余物生产木质成型炭的方法 |
JP2018080295A (ja) * | 2016-11-18 | 2018-05-24 | 株式会社トーセン | ホッパー付き燃料用木材チップの製造装置 |
CN107746736B (zh) * | 2017-09-15 | 2020-06-16 | 太原理工大学 | 一种光固化型煤的制备方法 |
CN114160078A (zh) * | 2021-12-03 | 2022-03-11 | 威海职业学院(威海市技术学院) | 一种水解自动化控制装置 |
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Also Published As
Publication number | Publication date |
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US8460515B2 (en) | 2013-06-11 |
CN102015977A (zh) | 2011-04-13 |
US20100162618A1 (en) | 2010-07-01 |
JP2008274108A (ja) | 2008-11-13 |
CN102015977B (zh) | 2013-09-11 |
EP2143780A1 (en) | 2010-01-13 |
EP2143780A4 (en) | 2013-05-15 |
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