WO2019239915A1 - 水熱処理装置及びバイオマス燃料製造プラント並びに水熱処理方法及びバイオマス燃料製造方法 - Google Patents
水熱処理装置及びバイオマス燃料製造プラント並びに水熱処理方法及びバイオマス燃料製造方法 Download PDFInfo
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- WO2019239915A1 WO2019239915A1 PCT/JP2019/021605 JP2019021605W WO2019239915A1 WO 2019239915 A1 WO2019239915 A1 WO 2019239915A1 JP 2019021605 W JP2019021605 W JP 2019021605W WO 2019239915 A1 WO2019239915 A1 WO 2019239915A1
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- processing container
- hydrothermal treatment
- biomass
- steam
- heat
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Images
Classifications
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- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C02F11/13—Treatment of sludge; Devices therefor by de-watering, drying or thickening by heating
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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
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10L9/08—Treating solid fuels to improve their combustion by heat treatments, e.g. calcining
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- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
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- C10J2300/0979—Water as supercritical steam
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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
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- C10L2200/04—Organic compounds
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- C10L2200/0469—Renewables or materials of biological origin
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/06—Heat exchange, direct or indirect
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/08—Drying or removing water
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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
- C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
- C10L2290/24—Mixing, stirring of fuel components
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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
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- 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
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
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- C10L3/08—Production of synthetic natural gas
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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
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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
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the present invention relates to a hydrothermal treatment apparatus, a biomass fuel production plant, a hydrothermal treatment method, and a biomass fuel production method.
- biomass fuel is attracting attention due to international carbon dioxide emission regulations, but wood pellets, which are representative examples of biomass fuel, are expensive, so various biomass including cost reduction Fuel production means are being studied.
- As one of the means for producing biomass fuel there is a method for producing biomass fuel from high water content biomass such as sewage sludge.
- biomass with a high moisture content is incapable of self-combustion, and there is a problem that it is difficult to utilize as a fuel for combustion unless a drying treatment is performed as a pretreatment.
- a drying treatment is performed as a pretreatment.
- high moisture content biomass is made into fuel, a large amount of water is dehydrated for drying, so that a large amount of energy is required for drying, which requires treatment of impurities contained in the dehydrated moisture, resulting in an increase in cost.
- the high water content biomass has a problem that moisture is constrained in the cell walls derived from living organisms and the drying efficiency is low.
- the present invention has been made in view of such circumstances, and reduces the water content of the processed product after hydrothermal treatment, and reduces the energy required for separating and removing moisture from the processed product after hydrothermal treatment.
- An object is to provide a hydrothermal treatment apparatus, a biomass fuel production plant, a hydrothermal treatment method, and a biomass fuel production method that can be reduced.
- a hydrothermal treatment apparatus is a hydrothermal treatment apparatus that performs hydrothermal treatment by heating high moisture content biomass, and includes a treatment container that stores the high moisture content biomass, and a vertical upper portion of the treatment container.
- a first supply unit for supplying the high moisture content biomass to the inside of the processing container, and the high water content so as to generate a flow in a predetermined direction.
- An agitation unit for agitating the high rate biomass, and at least one heat transfer tube that is arranged inside the processing vessel so as to intersect the predetermined direction and that heats the high water content biomass by the heat of steam flowing through the inside.
- the steam flowing through the heat transfer tube and the high water content biomass stored in the processing vessel are heat-exchanged to heat the high water content biomass, thereby generating a hydrolysis reaction, Hydrothermal treatment of moisture content biomass.
- Hydrothermal treatment moisture confined in the cell walls of the high water content biomass is released.
- the released water and the high water content biomass are mixed together, thereby improving the fluidity of the high water content biomass in the processing container.
- stirring in a stirring part can be performed suitably. Therefore, since the high water content biomass in the processing container can be uniformly hydrolyzed, hydrothermal treatment can be suitably performed.
- heat exchange between steam and high water content biomass is performed via a heat transfer tube. That is, the high water content biomass is hydrothermally treated by heating the high water content biomass indirectly through the heat transfer tubes without directly contacting the high water content biomass and the steam.
- the moisture necessary for fluidizing the high moisture content biomass is provided by effectively utilizing the moisture contained in the high moisture content biomass. In this way, the amount of moisture such as steam supplied to the high water content biomass for hydrothermal treatment can be reduced.
- the water content of a processed product hereinafter simply referred to as “processed product” obtained by hydrothermally treating high moisture content biomass can be reduced. Therefore, when water is separated / removed from the processed material after the hydrothermal treatment, energy required for water separation / removal can be reduced.
- a space is formed in the upper part in the vertical direction in the processing container, a desired pressurized space can be formed in the processing container. Therefore, hydrothermal treatment can be stably performed in the processing container.
- the space formed in the upper part in the vertical direction of the processing container efficiently mixes the newly introduced high water content biomass and the high water content biomass stored in the processing container. Thereby, a hydrolysis reaction can be accelerated
- the agitation unit is agitated so that a flow in a predetermined direction is generated in the high moisture content biomass, and the heat transfer tubes are arranged so as to intersect the flow in the predetermined direction of the high moisture content biomass.
- the high moisture content biomass can be efficiently brought into contact with the heat transfer tube and heated. Thereby, a hydrolysis reaction can be accelerated
- the stirring unit includes a blade portion arranged to be inclined with respect to a horizontal plane, and the blade portion has an axial direction extending in a vertical vertical direction. It rotates as a center, the tip of the blade part in the radial direction is arranged so as to be close to the inner peripheral surface of the processing container, and the heat transfer tube may extend in the horizontal direction.
- the blade portion When the blade portion rotates about the axial direction extending in the vertical vertical direction, the high water content biomass stored in the processing container is pressed by the blade portion. Since the blade portion is inclined with respect to the horizontal plane, the high moisture content biomass that has been pressed is moved in the processing vessel by a force that moves vertically upward or vertically downward, so that the high moisture content biomass is It is preferably stirred.
- the heat exchanger tube is arrange
- the blade portion can be arranged such that the tip in the radial direction is close to the inner peripheral surface of the processing container, thereby preventing sludge from adhering to the inner peripheral surface of the processing container and solidifying. .
- the locus region of the blade portion is formed to extend in the horizontal direction.
- the heat transfer tube extends in the horizontal direction.
- the stirring unit includes a plurality of blade portions that rotate about an axial direction extending in a vertical vertical direction, and the plurality of blade portions are the centers of rotation. Are arranged at equal intervals along the circumferential direction in the axial direction at positions spaced apart from the axial direction by a predetermined distance in the radial direction, and each inclined at a predetermined angle with respect to the horizontal plane in the rotational direction.
- the heat transfer tube extends in the horizontal direction, and the flow in the predetermined direction may be a counter flow including a vertical upward direction and a vertical downward direction.
- the heat transfer tubes so as to reliably cross the counter flow of the high water content biomass circulating in the vertical vertical direction. Accordingly, it is possible to reliably heat a large amount of high water content biomass in contact with the heat transfer tube. Therefore, since the high water content biomass in the processing container can be uniformly hydrolyzed, hydrothermal treatment can be suitably performed.
- the hydrothermal treatment apparatus includes a second supply unit that supplies water or steam to the processing container so that at least a part of the storage in the processing container maintains a predetermined moisture content. You may have.
- the fluidity of the stored material in the processing container may be reduced.
- water or steam is supplied to the processing container so that at least a part of the storage in which the high water content biomass in the processing container is stored maintains a predetermined moisture content.
- liquidity of a storage thing can be suppressed. Therefore, since fluidity can always be maintained and suitable stirring can be performed, a uniform hydrolysis reaction can be caused and hydrothermal treatment can be suitably performed.
- liquidity is maintained, the storage thing which hydrothermal treatment advanced can be discharged
- the processing container includes at least one of the outer shell having a main body portion forming a side surface and a bottom surface and a ceiling portion forming a vertical upper surface, and the heat transfer tube.
- the ceiling part may be detachably fixed to the main body part, and the fixing part may be detachably fixed to the main body part.
- the ceiling part can be opened, and the fixing part for fixing the heat transfer tube can be removed from the main body part of the processing container.
- the heat transfer tube can be accessed by removing the fixing portion from the main body portion. Therefore, maintenance and repair of the inside of the processing container and the heat transfer tube can be easily performed.
- the hydrothermal treatment apparatus includes a supply chamber that supplies the high-moisture content biomass to the processing container, a discharge chamber that discharges a reservoir stored in the processing container, and the supply
- the temperature difference depending on the position of the high water content biomass in the treatment container is within a predetermined temperature difference range during the hydrothermal treatment in the treatment container.
- the rotation speed of the stirring unit can be adjusted by the control unit so that the temperature difference depending on the position of the high water content biomass in the processing vessel is within a predetermined temperature difference.
- a hydrolysis reaction can be accelerated
- a biomass fuel production plant is a biomass fuel production plant including any one of the hydrothermal treatment apparatuses described above, wherein the high water content biomass hydrothermally treated by the hydrothermal treatment apparatus is dehydrated.
- a dehydrating unit that performs the separation, a first separation water channel that guides the separated water separated from the high water content biomass in the dehydrating unit, and the steam generated in the processing vessel is discharged to the outside of the processing vessel.
- a separation processing unit that separates impurities from the steam discharged from the steam discharge unit.
- the steam generated in the processing vessel contains volatile components (CH4, benzene, HmSn compounds, etc.) and impurities contained in the high water content biomass. For this reason, the process which isolate
- separation water evaporates in a processing container, becomes a vapor
- the separation water and the steam generated in the processing vessel are processed by one separation processing unit, so the structure of the biomass fuel production plant is simplified compared to the configuration in which the separation processing unit is provided for each. can do. Therefore, space saving can be achieved and the installation cost can be reduced.
- the biomass fuel production plant includes a plurality of branch pipes in which the first separation water flow path branches, and the plurality of branch pipes communicate with different positions in the vertical vertical direction of the processing container. You may do it.
- the branch pipe communicates with different positions in the vertical vertical direction of the processing container, so that the separated water can be used for purging the stored material stored in the processing container. Therefore, for example, when a branch pipe is connected near the upper surface of the stored substance stored in the processing container, the separated water is ejected to the heat transfer pipe arranged near the upper surface to thereby produce a high water content biomass. Can be purged, so that the high moisture content biomass can be prevented from sticking to the heat transfer tubes arranged near the upper surface. Also, for example, when a branch pipe is connected in the vicinity of the processing container take-out port, the water can be taken out by injecting separated water into the take-out port that may clog the stored product and purging the stored product. Mouth obstruction can be suppressed.
- the biomass fuel production plant may include a blow pipe that discharges a predetermined proportion of the separated water separated by the dehydration unit to the outside.
- impurity components contained in the separated water for example, sodium (Na), potassium (K), phosphorus (P), and the like are supplied and accumulated in the processing container so that the concentration of the impurity components does not increase.
- impurity components contained in the separated water for example, sodium (Na), potassium (K), phosphorus (P), and the like are supplied and accumulated in the processing container so that the concentration of the impurity components does not increase.
- impurity components contained in the separated water for example, sodium (Na), potassium (K), phosphorus (P), and the like are supplied and accumulated in the processing container so that the concentration of the impurity components does not increase.
- the biomass fuel production plant generates steam with the combustion heat of the input fuel, the boiler that supplies the generated steam to the heat transfer tube, and the hydrothermally treated device with the hydrothermal treatment device.
- the 1st heat exchange part which heat-exchanges high moisture content biomass and the boiler waste gas discharged
- heat treatment is performed on the high moisture content biomass hydrothermally treated with exhaust gas by exchanging heat between the boiler exhaust gas that generates steam used in the hydrothermal treatment device and the hydrothermally treated product. are doing.
- the heat of the boiler exhaust gas can be effectively used and the hydrothermally treated product can be dried, the energy efficiency of the entire biomass fuel production plant is compared with a configuration that does not use the heat of the boiler exhaust gas. Can be improved.
- the biomass fuel production plant includes a digestion tank into which the high water content biomass before being supplied to the processing vessel is introduced, and a separation separated from the high water content biomass in the dehydration unit Hydrothermally treated by the second separation water flow path for guiding water to the digestion tank, an internal combustion engine driven by burning fuel gas for an internal combustion engine including fuel gas discharged from the digestion tank, and the hydrothermal treatment apparatus You may provide the 2nd heat exchange part which heat-exchanges the said high moisture content biomass and the internal combustion engine waste gas discharged
- the fuel gas is taken out from the high water content biomass before being supplied to the processing container in the digestion tank, and the internal combustion engine is driven by the fuel gas for the internal combustion engine including the taken out fuel gas. Further, the processed product is heated with the exhaust gas from the internal combustion engine by exchanging heat between the exhaust gas of the internal combustion engine and the processed product obtained by hydrothermally treating the high water content biomass. As described above, the heat of the exhaust gas of the internal combustion engine can be effectively used to dry the hydrothermally treated product, so that the biomass fuel production plant is compared with a configuration that does not use the heat of the exhaust gas of the internal combustion engine. Overall energy efficiency can be improved.
- fever required in a digestion tank is provided by guide
- the energy efficiency of the entire biomass fuel production plant can be improved as compared with the configuration not using the heat of the separated water. .
- the biomass fuel production plant generates steam with the combustion heat of the input fuel, the boiler supplying the generated steam to the heat transfer tube, and the high before the supply to the processing container.
- a digestion tank into which moisture content biomass is introduced, a second separation water passage for guiding separated water separated from the high moisture content biomass in the dehydration unit to the digestion tank, and a fuel gas discharged from the digestion tank
- a third heat exchanging part that exchanges heat with each other.
- the biomass fuel production plant includes a fourth heat exchange unit that exchanges heat between the high water content biomass hydrothermally treated by the hydrothermal treatment apparatus and the steam discharged from the heat transfer tubes. May be.
- the processed material can be heated by the heat of the steam discharged from the heat transfer tube.
- the retained heat of the steam discharged from the heat transfer tube is used effectively, the energy efficiency of the biomass fuel production plant as a whole is improved compared to a configuration that does not use the heat of the steam discharged from the heat transfer tube. Can be made.
- the biomass fuel production plant may include a fifth heat exchange unit that exchanges heat between the steam discharged from the heat transfer tube and the separated water discharged from the dehydration unit. .
- the separated water can be heated by the heat of the steam discharged from the heat transfer tube.
- the energy efficiency of the biomass fuel production plant as a whole is improved compared to a configuration that does not use the heat of the steam discharged from the heat transfer tube. Can be made.
- the biomass fuel manufacturing plant which concerns on 1 aspect of this invention is a high moisture content biomass tank which stores the said high moisture content biomass supplied to the said processing container, the vapor
- the high moisture content biomass supplied to the processing vessel can be heated by the heat of the steam discharged from the heat transfer tube.
- the energy efficiency of the biomass fuel production plant as a whole is improved compared to a configuration that does not use the heat of the steam discharged from the heat transfer tube. Can be made.
- a hydrothermal treatment method is a hydrothermal treatment method in which hydrothermal treatment is performed by heating biomass having a high water content, wherein the treatment vessel is formed so that a space is formed in an upper part in a vertical direction of the treatment vessel.
- a supply step of supplying the high moisture content biomass therein, an agitation step of stirring the high moisture content biomass so that a flow in a predetermined direction is generated by an agitation unit provided in the treatment vessel; and the treatment vessel A heating step of heating the high moisture content biomass by steam flowing through the inside of at least one heat transfer tube arranged to cross the predetermined direction.
- the biomass fuel production method according to one embodiment of the present invention produces biomass fuel using the hydrothermal treatment method described above.
- the water content of the processed product after the hydrothermal treatment can be reduced, and the energy required for separating and removing the water from the processed product after the hydrothermal treatment can be reduced.
- FIG. 2 is a schematic diagram showing a schematic cross section of the hydrothermal treatment apparatus of FIG. 1 and an outline of connection between the hydrothermal treatment apparatus and another apparatus. It is a typical front view which shows the stirrer of FIG. It is a figure which shows the flow of the stored matter in the processing container of FIG. It is a schematic diagram which shows the horizontal end surface of the processing container of FIG. It is a time chart which shows the opening-and-closing state of a valve
- the biomass fuel production plant 1 uses, for example, a boiler 2 that generates steam and the heat of steam from the boiler 2 to hydrothermally process sludge (high moisture content biomass).
- a hydrothermal treatment apparatus 3 for dehydrating a dehydrator (dehydration unit) 4 for dehydrating sludge hydrothermally treated by the hydrothermal treatment apparatus 3 (hereinafter referred to as “processed product”), and a processed product dehydrated by the dehydrator 4 being dried.
- the first dryer (fourth heat exchange unit) 5 and the second dryer (first heat exchange unit) 6 to be processed, and the processed product dried by the first dryer 5 and the second dryer 6 are formed into biomass fuel. And a molding machine 7 to be used.
- the biomass fuel production plant 1 temporarily stores the sludge dehydrated by the sludge dehydrator 9 and the sludge dehydrated by the sludge dehydrator 9 before introducing the sludge from the sewage treatment facility 8 into the hydrothermal treatment apparatus 3. And a sludge storage tank (high moisture content biomass tank) 17.
- the separated water separated by the sludge dehydrator 9 is subjected to separation and removal of impurities and volatile components (CH4, benzene, HmSn compounds, etc.) contained in the separated water at the treatment plant.
- impurities and volatile components CH4, benzene, HmSn compounds, etc.
- the raw material processed in the biomass fuel manufacturing plant 1 is not limited to sewage sludge. Any high water content biomass (wet fuel) may be used.
- the boiler 2 includes a furnace (not shown) by supplying fuel and air (not shown) supplied from the fuel supply pipe 10 and a burner (not shown) that forms a flame in the furnace.
- the feed water is heated by the combustion heat combusted by the steam to generate steam.
- a steam supply pipe 11 is connected to the boiler 2.
- the steam generated in the boiler 2 is supplied to the heat transfer pipe 24 of the hydrothermal treatment apparatus 3 through the steam supply pipe 11.
- a thermometer 12 for measuring the temperature of the steam flowing inside is provided on the outlet side of the boiler 2 or the inlet side of the heat transfer pipe 24 of the steam supply pipe 11 (see FIG. 2). When the temperature of the steam measured by the thermometer 12 is lower than a predetermined value, the fuel supplied to the burner is increased to increase the temperature of the steam.
- a boiler exhaust gas pipe 13 is connected to the boiler 2.
- the boiler exhaust gas discharged from the boiler 2 is supplied to the second dryer 6 via the boiler exhaust gas pipe 13.
- the boiler exhaust gas discharged from the boiler 2 is, for example, about 300 ° C. to 400 ° C.
- the boiler exhaust gas used as the heat source for drying the processed product in the second dryer 6 is discharged from the second dryer 6.
- the boiler exhaust gas discharged from the second dryer 6 is deodorized by the deodorizer 14, then impurities such as dust are removed by the dust remover 15, and then released from the chimney 16 to the atmosphere.
- the hydrothermal treatment apparatus 3 includes a treatment vessel 21 that performs hydrothermal treatment therein, a sludge supply unit (first supply unit) 22 that introduces sludge from the sewage treatment facility 8 into the treatment vessel 21, and A stirrer (stirring unit) 23 that stirs the sludge stored in the processing container 21 and disposed in the processing container 21, and at least one of the steam that is disposed in the processing container 21 and in which the steam flows.
- a heat transfer tube 24 and a processed material discharge unit 25 for discharging a processed material from the processing container 21 are provided.
- Some high-moisture biomass such as sludge has a moisture content confined in a cell wall derived from living organisms, and the constrained moisture is difficult to evaporate, so that the drying efficiency is low.
- the moisture restrained in the cells is released by destroying the cell walls of the high moisture content biomass by a hydrolysis reaction using the heat of the steam generated in the boiler 2. That is, in the hydrothermal treatment apparatus 3, the sludge is hydrothermally treated.
- the high water content biomass is boosted and raised so that the temperature becomes a predetermined temperature (150 degrees to 230 degrees) under a predetermined pressure (0.5 Mpa to 3 Mpa). It is suitably performed by warming.
- the processing vessel 21 is, for example, a substantially cylindrical pressure vessel with the vertical vertical direction as an axis, and a lower end portion serving as a bottom surface is curved in a hemispherical shape.
- the processing container 21 includes a main body portion 21b and a ceiling portion 21a that form a lower end portion that is a side surface and a bottom surface of the outer shell.
- the ceiling portion 21a of the processing vessel 21 is formed in a flat shape and fixed so as to be removable from the main body portion 21b.
- the ceiling portion 21a has a first steam discharge pipe 26 and a third sludge pipe which will be described later. 35 is connected.
- An extraction port (not shown) for discharging the stored material in the processing container 21 to the outside is formed at the curved lower end, and is connected to the processed material discharge unit 25.
- the processing container 21 is provided with the main-body part 21b which makes an outer shell, and the nozzle (fixed part) 21c which fixes the heat exchanger tube 24 with respect to the main-body part 21b (refer FIG. 5).
- the nozzle 21c is fixed to the main body 21b, the nozzle 21c and the main body 21b are configured separately and can be detached from the main body 21b.
- ⁇ Sludge is stored inside the processing vessel 21. Specifically, sludge having a moisture content of about 70% to 90% (more preferably 80% to 85%) is stored in the middle region to the lower region in the vertical vertical direction of the space in the processing container 21. A space S that does not store sludge is formed in the upper region.
- the inside of the processing vessel 21 is maintained at a pressure (about 0.5 Mpa to 3 Mpa) that can suitably perform hydrothermal treatment on sludge. Further, the processing container 21 is provided with a pressure gauge 27 for measuring the pressure in the processing container 21, and the measured value is transmitted to the control unit 18.
- the control unit 18 includes, for example, a CPU (Central Processing Unit), a RAM (Random Access Memory), a ROM (Read Only Memory), and a computer-readable storage medium.
- a series of processes for realizing various functions is stored in a storage medium or the like in the form of a program as an example, and the CPU reads the program into a RAM or the like to execute information processing / arithmetic processing.
- the program is preinstalled in a ROM or other storage medium, provided in a state stored in a computer-readable storage medium, or distributed via wired or wireless communication means. Etc. may be applied.
- the computer-readable storage medium is a magnetic disk, a magneto-optical disk, a CD-ROM, a DVD-ROM, a semiconductor memory, or the like.
- a first steam discharge pipe (steam discharge unit) 26 that discharges steam to the outside of the process container 21 is connected to the ceiling portion 21 a of the process container 21.
- the first steam discharge pipe 26 is provided with a flow rate adjusting valve 26 a that adjusts the flow rate of the steam flowing through the inside.
- the flow rate adjusting valve 26a is controlled by the control unit 18 so that the pressure in the processing vessel 21 measured by the pressure gauge 27 is equal to or higher than a threshold value (for example, a predetermined pressure (0.5 Mpa to 3 Mpa) for performing hydrothermal treatment).
- the flow rate adjustment valve 26a is opened, and excess steam in the processing container 21 is discharged to the outside, so that the pressure in the hydrothermal treatment is maintained with the pressure in the processing container 21 being a predetermined threshold value or less.
- the first steam discharge pipe 26 is provided with a condenser 28 on the downstream side of the flow rate adjustment valve 26 a, and the steam discharged from the processing container 21 is condensed in the condenser 28.
- Condensed condensed water is separated and removed from impurities and volatile components (CH 4, benzene, HmSn compound, etc.) contained in the condensed water in a treatment plant (separation processing unit) 29.
- the treatment plant 29 into which the condensed water is introduced may be the same facility as the treatment plant into which the separated water separated from the sludge dehydrator 9 is introduced, or may be a different facility.
- the sludge supply unit 22 includes a supply chamber 31 that temporarily stores sludge, a feeder 32 that adjusts the amount of sludge supplied into the processing container 21, a first sludge pipe 33 that supplies sludge to the supply chamber 31, A second sludge pipe 34 for supplying the sludge discharged from the supply chamber 31 to the feeder 32 and a third sludge pipe 35 for introducing the sludge from the feeder 32 into the processing container 21 are provided.
- the first sludge pipe 33 has a sludge circulating therein and a downstream end connected to the supply chamber 31.
- the first sludge pipe 33 is provided with a first supply side valve 22a.
- the first supply-side valve 22a is, for example, a ball valve, and has a sealing performance so that sludge can pass in the open state and the pressure in the supply chamber 31 can be increased in the closed state. It is a high valve.
- the supply chamber 31 is a pressure vessel capable of adjusting the internal pressure, and the sludge is supplied from the first sludge pipe 33.
- the pressure in the supply chamber 31 is increased by supplying a pressurized gas (not shown) such as compressed air.
- a leak channel 31 a is connected to the supply chamber 31.
- the leak passage 31a is provided with a leak valve 31b, and the inside of the supply chamber 31 can be decompressed by opening the leak valve 31b.
- the second sludge pipe 34 connects the supply chamber 31 and the feeder 32. That is, the sludge discharged from the supply chamber 31 is supplied to the feeder 32 via the second sludge pipe 34.
- the second sludge pipe 34 is provided with a second supply side valve (first switching means) 22b and a third supply side valve (first switching means) 22c in order from the upstream side.
- the second supply side valve 22b and the third supply side valve 22c are, for example, ball valves, and can pass sludge in the open state and increase the pressure in the supply chamber 31 in the closed state.
- the valve has a high sealing performance as possible.
- the second supply side valve 22b and the third supply side valve 22c can switch between a state in which the supply chamber 31 and the processing container 21 are in communication with each other and a state in which the supply chamber 31 and the processing container 21 are isolated. it can.
- the third supply side valve 22c is provided as a reserve for the second supply side valve 22b and prevents the entire hydrothermal treatment apparatus 3 from being stopped due to a failure of the second supply side valve 22b.
- the feeder 32 is configured to be able to adjust the amount of sludge supplied to the processing container 21. Further, a third sludge pipe 35 is connected to the feeder 32, and a predetermined amount of sludge is introduced into the processing container 21 through the third sludge pipe 35.
- the operations of the first supply side valve 22a, the leak valve 31b, the second supply side valve 22b, the third supply side valve 22c, and the feeder 32 are controlled by the control unit 18.
- the stirrer 23 includes a rotation shaft 41 extending so as to be centered on an axial direction extending in the vertical vertical direction, a plurality of rod portions 42 extending in the horizontal direction from the rotation shaft 41, and tip portions of the respective rod portions 42. , And a blade portion 43 provided in the.
- the rotation shaft 41 extends so as to coincide with the central axis of the cylindrical processing container 21 over substantially the entire vertical direction of the processing container 21, and rotates counterclockwise when viewed from above.
- the upper part of the rotation shaft 41 passes through the ceiling 21 a of the processing container 21. That is, the upper end portion of the rotation shaft 41 is disposed outside the processing container 21.
- the upper end portion of the rotary shaft 41 is connected to a rotary drive device (not shown) such as a motor, and the rotary shaft 41 rotates at a predetermined rotational speed by the driving force of the rotary drive device such as a motor.
- the operation of the rotary drive device is performed by the control unit 18.
- the rotational drive device may be configured to measure a rotational load (current value, etc.) with respect to the rotational speed.
- a portion where the rotary shaft 41 penetrates the ceiling portion 21a has a seal structure 44, and the gas in the processing container 21 does not leak from the penetration portion.
- the seal structure 44 include a structure in which a pressurized gas is introduced from an external opening of the labyrinth seal by providing a lip seal made of an elastic resin or a labyrinth seal.
- the rod portion 42 is a rod-shaped member extending a predetermined distance in the horizontal direction from the rotating shaft 41.
- the bar portion 42 is fixed at a plurality of locations in the extending direction of the rotating shaft 41 (in this embodiment, three locations as an example), and as shown in FIG.
- the fixed portion has a predetermined radial distance (for example, 30% to 80% of the distance from the rotary shaft 41 to the inner peripheral surface of the processing vessel 21 at intervals of 180 degrees along the circumferential direction of the outer peripheral surface of the rotary shaft 41. %), Two rod portions 42 of the same length are provided. That is, in the present embodiment, two rod portions 42 are provided at three locations in the extending direction of the rotating shaft 41, so that six rod portions 42 are formed in total.
- a plate-like blade portion 43 is provided at the radial tip of all the rod portions 42.
- the plate-like blade portion 43 is provided such that the surface portion is inclined with respect to the horizontal plane at a predetermined angle (for example, 5 degrees to 40 degrees) toward the rotation direction.
- a predetermined angle for example, 5 degrees to 40 degrees
- the front part in the traveling direction of the blade part 43 that is, the rotational direction of the rotary shaft 41
- the blade portion 43 is arranged so that the radial tip (that is, the end portion opposite to the end portion fixed to the rod portion 42) is close enough not to contact the inner peripheral surface of the processing vessel 21. Is done.
- the flow of the stored matter in the processing container 21 will be described with reference to FIG.
- the blade part 43 rotates around the rotation shaft 41, the blade part 43 presses the stored matter stored in the processing container 21. More specifically, out of the storage stored in the processing container 21, the storage in the outer region is pressed in the radial direction from the rotation shaft 41 in the processing container 21. Since the blade part 43 is inclined so that the front part in the traveling direction is located above the rear part, a force that moves downward acts on the pressed reservoir. Therefore, as shown in FIG. 4, the storage pressed by the blade portion 43 moves downward (see also the arrow in FIG. 3) along the inner peripheral surface of the processing container 21.
- the storage that has moved downward is folded back in a substantially U shape in the vicinity of the bottom surface of the processing vessel 21 and moves upward along the central axis.
- a counter flow of the reservoir circulating in the vertical direction is generated in the processing container 21.
- the counter flow is formed in the entire region in the processing container 21 so as to be substantially symmetric with respect to the rotation axis 41. Due to this counter flow, the stored material stored in the processing container 21 is efficiently stirred.
- the flow of the reservoir generated in the processing container 21 may be another flow.
- a counterflow that moves downward along the rotation shaft 41 and moves upward along the inner peripheral surface of the processing container 21 may be generated.
- the blade portion 43 may be inclined so that the front portion in the rotation direction is positioned below the rear portion, or the rotation direction of the rotation shaft 41 may be reversed. .
- an elastic buffer 45 (for example, a brush or the like) is provided at the tip of the blade portion 43.
- the blade part 43 is disposed so that the tip in the radial direction is close enough not to contact the inner peripheral surface of the processing container 21, so that sludge adheres to the inner peripheral surface of the processing container 21 and solidifies. Suppress.
- the elastic buffer body 45 is arranged so as to be close to or in contact with the inner peripheral surface of the processing container 21.
- wing part 43 is not limited to the number of the said description.
- the configuration in which the portions for fixing the rod portion 42 are provided at three locations in the extending direction of the rotating shaft 41 has been described. Multiple locations other than locations may be used.
- FIG. 1 the example which provides the bar part 42 and the blade
- the number of the bar portions 42 to be fixed to the fixing portion is not limited to the number described above. In the above description, the example in which the two rod portions 42 are provided at intervals of 180 degrees has been described.
- the number of the rod portions 42 to be provided may be, for example, a single rod portion 42 or a plurality of three or more rods.
- the part 42 may be provided.
- the heat transfer pipe 24 is connected to the steam supply pipe 11, and the steam generated by the boiler 2 is supplied through the steam supply pipe 11.
- at least one of the heat transfer tubes 24 is fixed to the nozzle 21c, and is detachably fixed to the main body 21b of the processing vessel 21 via the nozzle 21c.
- the heat transfer tube 24 formed in the shape of a spiral coil for example, to increase the heat transfer area, it becomes difficult to fix to the main body portion 21b of the processing vessel 21 via the nozzle 21c. You may provide near the bottom face in the container 21. In the present embodiment, as shown in FIG.
- the heat transfer tubes 24 include a plurality of (in the present embodiment, four as an example) horizontal heat transfer tubes 51 extending in the horizontal direction and a plurality of horizontal heat transfer tubes 51. And a vertical heat transfer pipe 52 extending in the vertical direction, which is connected in series, and configured to supply steam as a single continuous pipe.
- the plurality of horizontal heat transfer tubes 51 include a plurality of horizontal heat transfer tubes 51 and heat transfer tube headers by connecting the plurality of horizontal heat transfer tubes 51 in parallel to each other and including a heat transfer tube header capable of supplying and collecting steam.
- An adjustment valve (not shown) may be provided between (not shown) and the steam supply balance between the plurality of horizontal heat transfer tubes 51 may be adjusted.
- the horizontal heat transfer tube 51 is arranged so as to intersect this flow.
- the plurality of horizontal heat transfer tubes 51 are arranged in a layered manner with a predetermined interval in the vertical direction. Specifically, the plurality of horizontal heat transfer tubes 51 are arranged such that the horizontal heat transfer tubes 51 and the blade portions 43 of the stirrer 23 are alternately arranged in the vertical direction. As shown in FIG. 5, each of the plurality of horizontal heat transfer tubes 51 extends from the nozzle 21c to the opposite side with the rotary shaft 41 interposed therebetween, and is formed in a shape that is folded back a plurality of times. In other words, the horizontal heat transfer tube 51 is formed in a W shape in a top view.
- the horizontal heat transfer tube 51 is disposed at a position where it does not interfere with the stirrer 23 and is disposed at a position where the horizontal heat transfer tube 51 and the stirrer 23 do not physically contact even when the stirrer 23 rotates around the rotation shaft 41.
- the horizontal heat transfer tube 51 arranged at the lowest stage is not sandwiched between the blade portions 43 because of the vicinity of the bottom surface of the processing vessel 21, and thus hardly interferes with the stirrer 23. Therefore, it may be formed in a spiral coil shape. By doing in this way, since a heat-transfer area increases, the heat-transfer efficiency of the heat-transfer tube 24 can be improved.
- the vertical heat transfer tubes 52 connect adjacent horizontal heat transfer tubes 51 to each other.
- the vertical heat transfer tube 52 may be connected to the horizontal heat transfer tube 51 fixed to the nozzle 21c outside the processing vessel 21. Further, the gap formed between the tip of the blade portion 43 and the inner peripheral surface of the processing vessel 21 may be arranged so as not to interfere with the stirrer 23.
- the downstream end of the heat transfer tube 24 is connected to a second steam discharge pipe 53.
- the second steam discharge pipe 53 is connected to the first heat exchanger 5a disposed in the first dryer 5, and the steam discharged from the heat transfer tube 24 and the warm water partially drained are first dried. Leads to machine 5.
- the first heat exchanger 5a provided in the first dryer 5 performs heat exchange between the steam discharged from the heat transfer tube 24 and the drained warm water and the processed product carried out from the processing container 21, and the processed product is While heating, cool the steam and drained hot water. At this time, most of the cooled steam is condensed, and the temperature of the hot water is lowered and mixed with the condensed water.
- the condensed condensed water is supplied to the boiler 2 as feed water through a feed water supply pipe 54 that connects the first dryer 5 and the boiler 2. Indirect heat exchange is performed both in the processing vessel 21 and in the first dryer 5, so that impurities and volatile components (CH4, benzene, HmSn compound, etc.) are not mixed in the feed water.
- the feed water supply pipe 54 is provided with a flow meter 55 (see FIG. 2) for measuring the flow rate of the feed water (condensed water) flowing inside. Further, a pipe 57 connected to the water supply tank 56 joins at a midway position of the water supply supply pipe 54. When the flow rate measured by the flow meter 55 is smaller than a predetermined amount, water is added from the water supply tank 56.
- the processed product discharge unit 25 includes a discharge chamber 61 that temporarily stores a processed product, a processed product tank 62 that stores a processed product to be supplied to the dehydrator 4, and a processed product discharged from the processing container 21.
- the first processed product pipe 63 supplied to the processing chamber, the second processed product piping 64 for supplying the processed product discharged from the discharge chamber 61 to the processed product tank 62, and the processed product from the processed product tank 62 are introduced into the dehydrator 4.
- a third processed product pipe 65 is introduced into the dehydrator 4.
- the first processed product pipe 63 has a processed product flowing therein, an upstream end connected to the take-out port of the processing vessel 21, and a downstream end connected to the discharge chamber 61.
- the first processed product pipe 63 is provided with a first discharge side valve (second switching means) 25a and a second discharge side valve (second switching means) 25b in order from the upstream side.
- the first discharge side valve 25a and the second discharge side valve 25b are, for example, ball valves, and allow sludge to pass in the open state and increase the pressure in the discharge chamber 61 in the closed state.
- the valve has a high sealing performance as possible.
- the first discharge side valve 25a and the second discharge side valve 25b can switch between a state in which the discharge chamber 61 and the processing container 21 are in communication and a state in which the supply chamber 31 and the processing container 21 are isolated. it can.
- the second discharge side valve 25b is provided as a reserve for the first discharge side valve 25a, and prevents the entire hydrothermal treatment apparatus 3 from being stopped due to the failure of the first discharge side valve 25a.
- the discharge chamber 61 is a pressure vessel capable of adjusting the internal pressure, and the processed material is supplied from the processing container 21 through the first processed material pipe 63.
- a leak channel 61 a is connected to the discharge chamber 61.
- the leak passage 61a is provided with a leak valve 61b, and the inside of the discharge chamber 61 can be decompressed by opening the leak valve 61b.
- the second processed material pipe 64 connects the discharge chamber 61 and the processed material tank 62.
- the second treated product pipe 64 is provided with a third discharge side valve 25c.
- the third discharge side valve 25c is, for example, a ball valve, and has a sealing performance so that sludge can pass in the open state and the pressure in the supply chamber 31 can be increased in the closed state. It is a high valve.
- the third processed material pipe 65 connects the processed material tank 62 and the dehydrator 4.
- the dehydrator 4 dehydrates the sludge (that is, the treated product) whose cell wall has been destroyed by the hydrolysis reaction in the hydrothermal treatment apparatus 3 into a solid content and a liquid content (separated water).
- sludge that is, the treated product
- a liquid content separated water
- the dehydrator 4 can efficiently perform the dehydration process. In the dehydrator 4, for example, dehydration is performed until the moisture content of the processed product is about 50% or less.
- the dehydrator 4 dehydrates the processed material by, for example, pressing the processed material with a press machine (not shown).
- the dehydrator 4 may dehydrate the processed material by other methods.
- the processed product may be dehydrated with a centrifuge.
- the operations of the first discharge side valve 25a, the second discharge side valve 25b, the leak valve 61b, the third discharge side valve 25c, and the dehydrator 4 are performed by the control unit 18.
- the separated water separated by the dehydrator 4 is discharged to a separated water pipe (second supply unit, first separated water flow path) 71, and passes through a separated water tank 73, most of which is a processing vessel. 21 and a part thereof is discharged from a blow pipe 72 described later.
- the separated water pipe 71 branches into a plurality of positions at a midpoint. In the present embodiment, for example, the separated water pipe 71 branches into two pipes, a first branch pipe 71a and a second branch pipe 71b. They are connected to different positions in the direction and are ejected into the processing container 21.
- the first branch pipe 71a is located near the upper surface of the storage stored in the processing container 21 (an appropriate position of 0% to 50% of the height distance from the upper surface to the lower end of the processing container 21, for example, the processing container 21
- the sludge introduced into the inside is connected to the vicinity of the uppermost horizontal heat transfer pipe 51 where the sludge is easily fixed. By connecting in this way, the separation water can be ejected to the uppermost horizontal heat transfer tube 51 and the sludge can be purged, thereby preventing the sludge from sticking.
- the first branch pipe 71a is provided with a first flow rate adjusting valve 71c that adjusts the flow rate of the separated water flowing inside.
- the second branch pipe 71b is connected to, for example, the vicinity of the outlet of the processing container 21. By connecting in this way, it is possible to prevent the clogging of the extraction port by injecting separated water to the extraction port that may clog the storage material and purging the storage material that has settled and accumulated at the lower end. it can.
- the second branch pipe 71b is provided with a second flow rate adjusting valve 71d that adjusts the flow rate of the separated water flowing inside. If there is a part other than the uppermost horizontal heat transfer tube 51 and the outlet to supply separated water for the purpose of cleaning or the like, two separated water pipes 71 are provided as shown by broken lines in FIG. You may make it branch above.
- the blow pipe 72 is branched on the upstream side of the branch point of the first branch pipe 71a and the second branch pipe 71b.
- the blow pipe 72 has a pipe diameter etc. so that 1% to 10% (more preferably 1% to 5%) of the separated water discharged from the dehydrator 4 always flows as a predetermined ratio. Is set. In other words, the remaining separated water that has not branched to the blow pipe 72 is supplied to the processing container 21. Further, the blow pipe 72 is provided with a flow rate adjusting valve 72a for adjusting the flow rate of the separated water flowing inside.
- the flow regulating valve 72a is an impurity component contained in the separated water, for example, plant fibers (plant cell walls and cell membranes) are destroyed by sludge hydrolysis reaction, so that sodium (Na) and potassium (K) in the plant cells are destroyed.
- the opening degree is adjusted according to the concentration of phosphorus (P), etc., and the flow rate of the separated water flowing through the blow pipe 72 is adjusted. Therefore, the impurity component contained in the separated water supplied to the processing vessel 21 can be prevented from accumulating in the processing vessel 21 to increase the concentration of the impurity component and crystallize.
- the processed product from which the separated water has been dehydrated by the dehydrator 4 is supplied to the first dryer 5 via the fourth processed product pipe 76.
- the first dryer 5 dries the processed material dehydrated by the dehydrator 4 using the heat of the steam discharged from the processing container 21 by the first heat exchanger 5a provided inside. .
- the processed product dried by the first dryer 5 is supplied to the second dryer 6 through the fifth processed product pipe 77.
- the second dryer 6 uses the heat of the exhaust gas from the boiler 2 to treat the product dried in the first dryer 5 by the second heat exchanger 6a provided therein, for example, with a water content of 10%. % To 20% or less.
- the processed product dried by the second dryer 6 is supplied to the molding machine 7 through the sixth processed product pipe 78.
- the molding machine 7 molds the processed material dried by the second dryer 6 into biomass fuel.
- Biomass fuel molded by the molding machine 7 is supplied to the supply destination.
- a part of the molded biomass fuel may be supplied to the boiler 2 as a part of the fuel of the boiler 2 as shown by the broken line in FIG.
- FIG. 6A shows the open / close state of the first supply side valve 22a
- FIG. 6B shows the open / close state of the second supply side valve 22b and the third supply side valve 22c.
- (c) shows the amount of sludge filling in the supply chamber 31
- (d) shows the pressure in the supply chamber 31
- (e) shows the amount of sludge (stored amount) in the processing vessel 21.
- (F) shows the open / close state of the first discharge side valve 25a and the second discharge side valve 25b
- (g) shows the open / close state of the third discharge side valve 25c.
- the supply chamber 31 and the processing container 21 are separated (separated).
- the first supply side valve 22a is opened (see (a)).
- sludge is supplied into the supply chamber 31, so that the filling amount of the supply chamber 31 increases from T1 to T2 (see (c)).
- T2 which is the timing when the supply chamber 31 is sufficiently filled with sludge, the first supply side valve 22a is closed (see (a)).
- the pressure inside the supply chamber 31 is increased from T2 to T3 (see (d)).
- the pressure in the supply chamber 31 is increased by supplying a pressurized gas such as compressed air.
- the pressure increase is stopped and the second supply side valve 22b and the third supply side valve 22c are opened ( (See (b)).
- the second supply side valve 22b and the third supply side valve 22c are closed, and the supply chamber 31 and the processing container 21 are separated.
- the processing container 21 is sealed, and the inside of the processing container 21 is maintained at a predetermined temperature and pressure.
- the leak valve 31b provided in the leak flow path 31a is opened, and the pressure in the supply chamber 31 is reduced to be equal to the atmospheric pressure (( d)).
- the discharge chamber 61 and the processing container 21 are separated.
- the first discharge side valve 25a and the second discharge side valve 25b are opened (see (f)).
- the discharge chamber 61 and the processing container 21 are in communication with each other, and the processing object at the bottom in the processing container 21 moves to the discharge chamber 61.
- the amount of storage in the processing container 21 decreases from T5 to T6 (see (e)).
- T6 which is the timing when a predetermined amount of processed material is discharged from the processing container 21, the first discharge side valve 25a and the second discharge side valve 25b are closed (see (f)).
- the discharge chamber 61 and the processing container 21 are separated.
- the third discharge side valve 25c is opened, and the processed material is discharged from the discharge chamber 61 (see (g)).
- T8 which is the timing when the discharge of the processed material is finished, the third discharge side valve 25c is closed.
- the hydrothermal treatment apparatus 3 operates. In this way, in the hydrothermal treatment apparatus 3, the supply chamber 31 and the discharge chamber 61 can be brought into a state in which the supply chamber 31 and the discharge chamber 61 are in communication with the processing container 21 and separated from each other. It can be said that the supply of sludge and the discharge of the processed material are continuously performed while maintaining the pressure.
- the predetermined time that can be regarded as the completion of the hydrothermal treatment of the processed material to be discharged is previously set with respect to the hydrolysis conditions (temperature and pressure in the processing container 21), the supply amount of new sludge and the discharged amount of the processed material It is preferable to check by a test or the like, and to manage the supply timing of sludge and the discharge timing of the processed material in the confirmed predetermined time.
- the amount of sludge introduced at a time is set to, for example, 20% of the amount of stored matter in the processing container 21 is described. That is, when the amount of stored matter in the processing container 21 is V, the amount of sludge introduced at a time is 0.2V.
- the cycle time T which is the time from the introduction of the sludge into the processing container 21 until the introduction of the next sludge (the time from T3 to T9 in FIG. 6), is set to 5 minutes, for example. Therefore, the time required for the entire storage in the processing container 21 to be replaced is derived from the following formula (1) and is 25 minutes. In other words, it takes 25 minutes for the sludge introduced into the processing vessel 21 to be hydrothermally treated and discharged from the processing vessel 21 as a processed product to the outside, which is suitable as a general hydrolysis reaction time. Time can be secured. (V / 0.2V) ⁇ T (1)
- the supply timing of the sludge and the discharge timing of the processed material may be managed by a change in rotational load with respect to the rotational speed provided in the rotational drive device of the stirrer 23.
- the viscosity of the stored material decreases. Therefore, by monitoring the decrease in the rotational load (current) with respect to the rotational speed of the rotational drive device of the agitator 23 from the predetermined value, the sludge supply timing and the processed material
- the discharge timing may be managed. Measurement and operation of the rotational speed and rotational load (current value, etc.) of the rotational drive device of the agitator 23 may be performed by a rotational speed control unit provided in the control unit 18.
- the hydrothermal treatment performed by the hydrothermal treatment apparatus 3 is a so-called continuous treatment.
- the hydrothermal treatment a continuous process it becomes possible to discharge the processed material without lowering the temperature in the processing container 21, so that energy loss due to the temperature decrease of the processing container 21 of the hydrothermal treatment device 3 and the processed material is reduced. Can be suppressed.
- the second supply side valve 22b and the third supply side valve 22c have been described as performing the same operation, but the second supply side valve 22b and the third supply The side valve 22c may not perform the same operation. Since the third supply side valve 22c is provided as a reserve for the second supply side valve 22b, the third supply side valve 22c is basically kept open so that only the second supply side valve 22b is maintained. You may switch opening and closing of a flow path. And when abnormality arises in the 2nd supply side valve
- the sludge supplied from the sewage treatment facility 8 to the treatment container 21 of the hydrothermal treatment apparatus 3 is heated in the treatment container 21 through heat transfer tubes 24 with the heat of steam from the boiler 2 under a predetermined pressure.
- heat transfer tubes 24 By being indirectly heated (heating step), a hydrothermal treatment is performed, and the cell wall is destroyed by a hydrolysis reaction.
- the storage in the processing container 21 is stirred and subdivided by the stirrer 23 (stirring step).
- the control unit 18 sets the pressure in the processing container 21 to a predetermined pressure (0.5 Mpa to 3 Mpa), and the temperature in the processing container 21 is set to a predetermined temperature (150 ° C.). ⁇ 230 ° C).
- the temperature distribution in the processing container 21 is measured by a plurality of thermometers 12 a and 12 b provided in the vertical direction in the processing container 21. The temperature measured by the thermometer 12a that measures the temperature of the upper part (near the middle part of the processing container 21) stored in the processing container 21 and the temperature of the lower part (near the bottom of the processing container 21) are measured.
- the rotational speed of the stirrer 23 is adjusted so that the temperature difference from the temperature measured by the thermometer 12b is within a predetermined temperature difference (5 ° C. to 10 ° C.).
- the pressure in the processing container 21 is increased by the vapor pressure generated from the sludge by heating the sludge. After reaching a predetermined pressure (0.5 Mpa to 3 Mpa), the opening degree of the flow rate adjustment valve 26a provided in the first steam discharge pipe 26 is adjusted to keep the pressure constant.
- the treated product that has been subjected to hydrothermal treatment in the hydrothermal treatment apparatus 3 and discharged from the hydrothermal treatment apparatus 3 is dehydrated by the dehydrator 4 to separate a liquid component (separated water).
- the water content of the processed material dehydrated by the dehydrator 4 is about 50%.
- the processed product dehydrated by the dehydrator 4 is supplied to the first dryer 5 and dried by the heat discharged from the heat transfer tube 24 of the hydrothermal treatment device 3 and the heat of the partially drained hot water by the first dryer 5. Is done.
- the processed product dried by the first dryer 5 is then supplied to the second dryer 6 and dried by the heat of the boiler exhaust gas from the boiler 2.
- the moisture content of the processed product dried by the second dryer 6 is 10% to 20%.
- the processed material dried by the second dryer 6 is supplied to the molding machine 7 and molded into biomass fuel, whereby biomass fuel is produced.
- Biomass fuel molded by the molding machine 7 is supplied to the supply destination.
- a part of the molded biomass fuel may be supplied to the boiler 2 as a part of the fuel of the boiler 2 as shown by the broken line in FIG.
- the separated water separated by the dehydrator 4 is discharged from the dehydrator 4 and is supplied to the processing vessel 21 through the separated water tank 73 (mostly about 90% to 99% of the whole separated water). 1% to 10%) is discharged from the blow pipe 72.
- the moisture content for example, about 80% to 85%
- the separated water is supplied to the processing vessel 21. More specifically, the amount of the separated water supplied to the processing container 21 is made equal to the amount of surplus steam discharged from the first steam discharge pipe 26 when steam is generated by the heating of sludge.
- the water content of the stored matter in 21 can be maintained at a desired value.
- a part of the separated water separated by the dehydrator 4 (1% to 10% of the whole separated water, more preferably 1% to 5%) is always circulated through the blow pipe 72 and blown into the boiler 2. Burned. In addition, you may perform the process which removes impurities etc. with a processing facility, without supplying to the boiler 2.
- FIG. 1 A part of the separated water separated by the dehydrator 4 (1% to 10% of the whole separated water, more preferably 1% to 5%) is always circulated through the blow pipe 72 and blown into the boiler 2. Burned. In addition, you may perform the process which removes impurities etc. with a processing facility, without supplying to the boiler 2.
- the steam generated in the boiler 2 is supplied to the heat transfer tube 24 through the steam supply pipe 11.
- the supply of steam from the boiler 2 to the heat transfer tube 24 is, for example, saturated steam or superheated steam of about 0.8 MPa to 10 MPa, and the hydrolysis temperature (maintenance temperature in the processing vessel 21) is equal to the supply energy equivalent temperature (20 degrees to The temperature is controlled by the temperature measured by the thermometer 12 provided at the steam supply pipe 11 (for example, at the boiler outlet) as 50 degrees, which is set to the amount of sludge to be used up to the latent heat of the steam and introduced into the processing vessel 21).
- the feed water flow rate returned from the heat transfer tube 24 is adjusted by a feed water pump or the like so that the temperature in the processing vessel 21 can be maintained at a predetermined temperature (preferably a temperature capable of causing a hydrolysis reaction, for example, 150 to 230 degrees). Good.
- the steam supplied to the heat transfer tube 24 circulates in the heat transfer tube 24 and indirectly heats the storage in the processing container 21 through the heat transfer tube 24.
- the steam discharged from the heat transfer tube 24 and the partially drained warm water are introduced into the first heat exchanger 5 a disposed in the first dryer 5 through the second steam discharge pipe 53.
- the steam and hot water introduced into the first heat exchanger 5a indirectly heat the processed product by exchanging heat with the processed product in the first heat exchanger 5a, and the steam is cooled and condensed, Decreases in temperature and is mixed with condensed water.
- the condensed condensed water is discharged from the first dryer 5. Indirect heat exchange is performed both in the processing vessel 21 and in the first dryer 5, so that impurities and volatile components (CH4, benzene, HmSn compound, etc.) are not mixed in the feed water.
- the condensed water discharged from the first dryer 5 is supplied again to the boiler 2 as feed water through the feed water supply pipe 54.
- the flow of steam or the like in the biomass fuel production plant 1 according to this embodiment is as described above.
- the steam flowing through the heat transfer tube 24 and the sludge stored in the processing vessel 21 are heat-exchanged to heat the sludge, thereby causing a hydrolysis reaction and hydrotreating the sludge. are doing.
- the hydrothermal treatment moisture confined in the cell walls of the high water content biomass is released.
- the released water and the high water content biomass are mixed with each other, thereby improving the fluidity of the high water content biomass in the processing vessel 21.
- stirring in a stirring part can be performed suitably. Therefore, since the sludge in the processing container 21 can be uniformly hydrolyzed, hydrothermal treatment can be suitably performed.
- heat exchange between steam and sludge is performed via the heat transfer tube 24. That is, the sludge is hydrothermally treated by indirectly heating the sludge through the heat transfer tube 24 without directly contacting the sludge with the steam. Further, the water necessary for fluidizing the stored matter in the processing container 21 is provided by effectively utilizing the water contained in the sludge. In this manner, the amount of moisture such as steam supplied to the sludge for hydrothermal treatment can be reduced. Compared with the method in which the vapor is directly contacted, the water content of the processed product after the hydrothermal treatment can be reduced. Therefore, when water is separated / removed from the processed material after the hydrothermal treatment, energy required for water separation / removal can be reduced.
- a space is formed in the upper part of the processing container 21 in the vertical direction, a desired pressurized space can be formed in the processing container 21. Therefore, hydrothermal treatment can be stably performed in the processing vessel 21.
- the space S formed in the upper part of the processing container 21 in the vertical direction efficiently mixes the newly introduced sludge and the sludge stored in the processing container 21. Thereby, a hydrolysis reaction can be accelerated
- the horizontal heat transfer tubes 51 of the heat transfer tubes 24 are arranged so as to extend in the horizontal direction. Therefore, the heat transfer tubes 24 are arranged so as to intersect with the opposite flow of the high water content biomass circulating in the vertical direction. Therefore, it is possible to heat a larger amount of stored material in contact with the heat transfer tube 24. Thereby, a hydrolysis reaction can be accelerated
- the locus region of the blade portion 43 is formed to extend in parallel to the horizontal plane.
- the horizontal heat transfer tube 51 extends in the horizontal direction. That is, the trajectory region of the blade portion 43 and the horizontal heat transfer tube 51 are parallel, and the trajectory region of the blade portion 43 and the horizontal heat transfer tube 51 do not overlap with each other, thereby preventing interference between the blade portion 43 and the horizontal heat transfer tube 51. Can do.
- the vertical heat transfer tube 52 is provided between the tip of the blade portion 43 and the inner peripheral surface of the processing container 21, interference between the blade portion 43 and the vertical heat transfer tube 52 can also be prevented.
- Steam is generated by heating the sludge by the heat transfer tube 24 in the processing container 21, and the pressure in the processing container 21 is maintained at a predetermined pressure by the steam pressure, and surplus steam is discharged.
- the hydrothermal treatment is performed at 220 ° C. and under the condition of 2.5 Mpa, 15% to 30% of the moisture in the sludge is discharged as steam. In this way, the moisture content of the stored material may be lower than when it is introduced into the processing container 21, and the moisture content of the stored product may be reduced to about 50%.
- the separation water is supplied to the processing container 21 so that the stored matter in the processing container 21 maintains a predetermined moisture content.
- liquidity of a storage thing can be suppressed. Therefore, fluidity can always be maintained and suitable stirring can be performed, so that a uniform hydrolysis reaction can occur.
- liquidity is maintained, a stored material can be discharged
- the nozzle 21c that fixes the ceiling 21a and the heat transfer tube 24 can be detached from the main body 21b of the processing vessel 21. In this manner, the heat transfer tube 24 can be accessed by removing the nozzle 21c from the main body 21b. Moreover, since the ceiling part 21a can be open
- the controller 18 may adjust the rotation speed of the stirrer 23 so that the temperature difference depending on the position of the stored matter in the processing container 21 is within a predetermined temperature difference (5 ° C. to 10 ° C.). it can. Thereby, the temperature distribution of the stored substance in the processing container 21 can be suppressed, the hydrolysis reaction can be promoted, and the hydrothermal treatment can be suitably performed. Therefore, the hydrothermal treatment time can be shortened.
- the steam generated in the processing vessel 21 contains volatile components (CH4, benzene, HmSn compounds, etc.) and impurities contained in the sludge. For this reason, the process which isolate
- separation water evaporates in the processing container 21, becomes a vapor
- the structure of the biomass fuel production plant 1 is compared with the configuration in which the separation processing unit is provided for each. It can be simplified. Therefore, space saving can be achieved and the installation cost can be reduced.
- the processed product is heated by exchanging heat between the exhaust gas of the boiler 2 that generates steam used in the hydrothermal treatment apparatus 3 and the processed product that has been hydrothermally treated.
- the heat-treated product can be dried using the heat of the exhaust gas of the boiler 2, the biomass fuel production plant 1 as a whole is compared with a configuration that does not use the heat of the exhaust gas of the boiler 2. Energy efficiency can be improved.
- the process of filling the sludge into the treatment container 21 of the hydrothermal treatment apparatus 3 the process of raising the temperature and pressurizing the treatment container 21 filled with sludge, and maintaining the state Energy and time have been required because of complicated processes such as a hydrothermal treatment process, a process container 21 pressure reduction process, and a process product discharge process.
- the ratio of the “holding step” in which hydrothermal treatment is performed is small, but there is a problem of the processing speed that the time of other accompanying processes becomes long.
- the hydrothermal treatment performed by the hydrothermal treatment apparatus 3 is a so-called continuous treatment.
- the processed material sludge whose cell wall has been destroyed by hydrothermal treatment
- the processed material can be carried out without lowering the temperature in the processing container 21.
- the loss of the input energy by the process container 21 of the hydrothermal treatment apparatus 3 and the temperature fall of a processed material can be suppressed.
- the steps of increasing the temperature, increasing the pressure, reducing the pressure, and the like can be reduced, so that the hydrothermal treatment can be performed efficiently.
- a blow pipe 72 is provided so that 1% to 10% (more preferably 1% to 5%) of the separated water discharged from the dehydrator 4 is always discharged. Yes. Thereby, the accumulation concentration of the impurity in the processing container 21 can be suppressed, and the viscosity rise of a stored matter can be suppressed.
- the steam discharge pipe 82 is connected to the supply chamber 31 and the separation water tank 73 in order from the upstream side. Specifically, the steam discharge pipe 82 is connected to a heat exchanger provided in the supply chamber 31 and a heat exchanger provided in the separation water tank 73. The steam discharged from the processing vessel 21 flows through the steam discharge pipe 82 and exchanges heat with sludge in the supply chamber 31 in a heat exchanger provided in the supply chamber 31. Through this heat exchange, the sludge can be heated by the heat of the steam and the steam can be cooled.
- the steam that has heated the sludge in the supply chamber 31 exchanges heat with the separated water in the heat exchanger provided in the separated water tank 73.
- the separated water can be heated by the heat of the steam, and the steam can be further cooled.
- Steam obtained by heating the separated water is introduced into the condenser 28. Since the steam is being cooled, the cooling capacity of the condenser 28 can be reduced.
- the heat of the steam discharged from the processing container 21 can be used to preheat the sludge supplied to the processing container 21 and the preheated separation water supplied to the processing container 21. . Therefore, the energy efficiency of the biomass fuel production plant 81 as a whole can be improved as compared with a configuration that does not use the heat of steam.
- the steam discharged from the processing container 21 may be guided to another device to use the heat of the steam.
- the sludge may be preheated by exchanging heat between the steam discharged from the processing container 21 and the sludge dehydrated by the sludge dehydrator 9.
- the biomass fuel production plant includes a temperature difference measuring unit that measures a temperature difference between the steam temperature at the inlet of the heat transfer tube 24 and the steam temperature at the outlet of the heat transfer tube 24, and the temperature measured by the temperature difference measuring unit. It differs from 1st Embodiment by the point provided with the rotational speed change means which changes the rotational speed of the rotating shaft 41 of the stirrer 23 based on a difference.
- the same components as those in the first embodiment are denoted by the same reference numerals, and detailed description thereof is omitted.
- the temperature difference measuring means includes, for example, an inlet-side thermometer 12 that measures the steam temperature at the inlet of the heat transfer tube 24, an outlet-side thermometer (not shown) that measures the steam temperature at the outlet of the heat-transfer tube 24, and the inlet side. And a calculation unit that calculates a temperature difference based on the temperature measured by the thermometer 12 and the temperature measured by the outlet side thermometer. In addition, for example, when the temperature difference calculated by the calculation unit is equal to or less than a predetermined value, the rotation speed changing means does not favorably perform heat exchange in the heat transfer tube 24, and dirt adheres to the heat transfer tube 24. And a rotation speed control section that increases the rotation speed of a rotary drive device such as a motor that drives the rotation shaft 41 based on information from the determination section.
- the determination unit and the rotation speed control unit may be provided in the control unit 18.
- the heat transfer tube 24 may have reduced heat transfer performance due to the burning and adhesion of sludge.
- the temperature difference measuring means is provided, it is possible to easily grasp the deterioration of the heat transfer performance of the heat transfer tube 24.
- the rotation speed change means is provided, when the heat transfer performance of the heat transfer tube 24 is lowered, the rotation speed of the stirrer 23 is increased to increase the speed of the flow of the stored matter. The heat transfer performance from the heat transfer tube 24 to the stored material can be recovered.
- the suit blower which injects the separated water isolate
- the biomass fuel production plant according to the present modification is different from the first embodiment in that the biomass fuel production plant includes a supply unit that supplies additional water or steam into the processing vessel 21 at the start of operation of the hydrothermal treatment apparatus 3.
- the same components as those in the first embodiment are denoted by the same reference numerals, and detailed description thereof is omitted.
- the sludge before hydrolysis reaction is apparently high in water content of about 80% to 85%, but is solid (sponge-like water) and has low fluidity. That is, before the hydrolysis reaction, the moisture of the sludge is constrained inside the cell wall, so the fluidity is low for a high moisture content. Therefore, at the start of operation of the hydrothermal treatment apparatus 3 before the hydrolysis reaction, there is a possibility that the agitation of the stored material cannot be suitably performed.
- the fluidity of the stored material can be improved even before the hydrolysis reaction. it can.
- moisture content restrained is discharged
- liquidity can be maintained with the water
- the additional water or steam to be supplied may be provided with a dedicated flow path, and the liquid remaining in the processing container 21 at the previous stop is stored, and the stored liquid is supplied. May be.
- the biomass fuel production plant 91 according to the present embodiment is mainly different from the first embodiment in that it includes a digester 92, a desulfurizer 93, a desiloxaner 94, and a gas engine (internal combustion engine) 95.
- the same components as those in the first embodiment are denoted by the same reference numerals, and detailed description thereof is omitted.
- the digestion tank 92 is provided on the upstream side of the sludge dehydrator 9 and is supplied with sludge from the sewage treatment facility 8.
- the digestion tank 92 performs a digestion process on the supplied sludge, and volatile gas such as methane is generated.
- the separation water separated from the dehydrator 4 is supplied to the digestion tank 92 via a separation water pipe (second separation water flow path) 97, and the heat of the separation water is used as a heat source for the digestion process. .
- the volatile gas generated in the digestion tank 92 is supplied to the desulfurization apparatus 93 and desulfurized.
- the volatile gas (fuel gas) desulfurized by the desulfurizer 93 is then supplied to the desiloxaner 94 to remove siloxane.
- Volatile gas from which siloxane has been removed is supplied to a gas engine 95.
- the fuel gas for the internal combustion engine is supplied to the gas engine 95.
- the gas engine 95 is driven by combustion using a volatile gas for part or all of the fuel gas for the internal combustion engine.
- Internal combustion engine exhaust gas is discharged.
- the internal combustion engine exhaust gas discharged from the gas engine 95 is, for example, about 150 ° C. to 400 ° C.
- the gas engine exhaust gas pipe 96 merges with the boiler exhaust gas pipe 13. That is, the internal combustion engine exhaust gas is joined to the boiler exhaust gas piping 13 through the gas engine exhaust gas piping 96, and then processed by the second heat exchanger 6a provided in the second dryer 6 (third heat exchange section). It is used as a heat source for drying objects.
- the exhaust gas from the internal combustion engine used as the heat source for drying the processed product in the second dryer 6 is discharged from the second dryer 6.
- the exhaust gas from the internal combustion engine discharged from the second dryer 6 is deodorized by the deodorizer 14, then impurities such as dust are removed by the dust remover 15, and then released from the chimney 16 to the atmosphere.
- the gas engine exhaust gas pipe 96 may be connected to the second dryer 6 independently without joining the boiler exhaust gas pipe 13. Further, the boiler exhaust gas pipe 13 is connected to the second dryer (first heat exchange unit) 6, and the gas engine exhaust gas pipe 96 is connected to a third dryer (second heat exchange unit) different from the second dryer 6. The heat treatment may be exchanged with the treated product by the third dryer, and the treated product may be dried. Note that the third dryer is not shown.
- the gas engine 95 is driven by taking out the volatile gas from the sludge before being supplied to the processing vessel 21 in the digestion tank 92 and using the taken out volatile gas as part or all of the fuel gas for the internal combustion engine. are doing. Further, the exhaust gas from the internal combustion engine of the gas engine 95 and the hydrothermally treated product are subjected to heat exchange, whereby the treated product is heated with the exhaust gas and dried. As described above, since the heat treated heat-treated product can be dried using the heat of the exhaust gas from the internal combustion engine of the gas engine 95, the biomass fuel is compared with the configuration in which the heat of the exhaust gas from the gas engine 95 is not used. The energy efficiency of the entire manufacturing plant 91 can be improved.
- the separated water separated from the dehydrator 4 is guided to the digestion tank 92, so that necessary heat is applied in the digestion tank 92.
- the energy efficiency of the biomass fuel production plant 91 as a whole can be improved as compared with a configuration that does not use the heat of the separated water. .
- the biomass fuel production plant 101 does not supply the steam discharged from the heat transfer tube 24 of the processing vessel 21 and the partially drained warm water to the first dryer 5,
- the point leading to 6 is mainly different from the second embodiment.
- the same components as those in the second embodiment are denoted by the same reference numerals, and detailed description thereof is omitted.
- the steam discharged from the heat transfer pipe 24 and the partially drained warm water are guided to the separated water tank heat exchanger 73a provided in the separated water tank 73 through the third steam discharge pipe 102.
- the separated water tank heat exchanger (fifth heat exchanging unit) 73a the steam and the partially drained warm water exchange heat with the separated water separated by the dehydrator 4, thereby heating the separated water, Steam and partially drained hot water are cooled.
- the steam that has been heat-exchanged with the separated water in the separated water tank heat exchanger 73 a and the partially drained warm water are guided to the sludge storage tank 17 through the fourth steam discharge pipe 103.
- FIG. 1 In the sludge storage tank heat exchanger 17a, heat is exchanged between the steam and the partially drained warm water and the sludge. Through this heat exchange, the sludge can be heated with the heat of steam and partially drained warm water, and the steam and partially drained warm water can be cooled.
- the steam that has been heat-exchanged with the separated water in the sludge storage tank heat exchanger 17a (sixth heat exchange section) and the partially drained warm water are guided to the tank 105 via the fifth steam discharge pipe 104.
- the steam guided to the tank 105 and the drained warm water are supplied to the boiler 2 via the pipe 57.
- the boiler exhaust gas discharged from the boiler 2 is guided to the first heat exchanger 5a provided in the first dryer 5 through the boiler exhaust gas pipe 107.
- the boiler exhaust gas guided to the first heat exchanger 5a exchanges heat with the processed material. By this heat exchange, the processed material is heated and the boiler exhaust gas is cooled.
- the boiler exhaust gas discharged from the first dryer 5 is released from the chimney 16 to the atmosphere via the deodorizer 14 and the dust remover 15.
- the internal combustion engine exhaust gas discharged from the gas engine 95 is guided to the second heat exchanger 6a provided in the second dryer 6 through the internal combustion engine pipe 108.
- the internal combustion engine exhaust gas guided to the second heat exchanger 6a exchanges heat with the processed material. By this heat exchange, the processed material is heated and the exhaust gas of the internal combustion engine is cooled.
- the boiler exhaust gas discharged from the first dryer 5 is discharged from the chimney 109 to the atmosphere.
- the heat of steam discharged from the heat transfer tube 24 can be used to preheat the separated water supplied to the processing vessel 21 and to preheat the sludge supplied to the processing vessel 21. . Therefore, the energy efficiency of the biomass fuel production plant 81 as a whole can be improved as compared with a configuration that does not use the heat of steam.
- the steam and the partially drained warm water exchanged with the separated water in the separated water tank heat exchanger 73a are led to the supply chamber 31 instead of the sludge storage tank 17, and the steam and the partially drained warm water You may heat-exchange with the sludge in a supply chamber.
- the present invention is not limited to the invention according to each of the above embodiments, and can be modified as appropriate without departing from the scope of the invention.
- the example in which the water content of the stored matter in the processing container 21 is maintained by introducing the separated water separated by the dehydrator 4 into the processing container 21 has been described. It is not limited to.
- steam generated in the boiler 2 may be supplied to the processing container 21 to maintain the moisture content of the stored matter.
- both the steam from the boiler 2 and the separated water separated by the dehydrator 4 may be supplied to maintain the moisture content of the stored matter.
- the gas engine is used for the internal combustion engine, a power generation system using a small boiler and a small steam turbine may be used.
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Abstract
Description
バイオマス燃料の製造手段の1つとして、下水汚泥等の高含水率バイオマスからバイオマス燃料を製造する方法がある。しかしながら、含水率の高いバイオマスは、自燃不能であり、前処理として乾燥処理を行わなければ燃焼用の燃料として活用することが難しいという問題がある。また、高含水率バイオマスを燃料化する場合、乾燥のために脱水させる水分が多いため乾燥に必要なエネルギーが大きく、脱水させた水分に含まれる不純物の処理が必要になりコストアップとなる。また、高含水率バイオマスは、水分が生物由来の細胞壁内に拘束されており、乾燥効率が低いという課題がある。
なお、特許文献1及び特許文献2に記載の装置では、水熱処理をバッチ処理するために水熱処理後には温度と圧力を低下して処理物を搬出して、再度に高含水率バイオマスを搬入充填して温度と圧力の上昇を行う必要があり、分離・除去に要するエネルギーが増大するとともに、水熱処理時間以外に必要な前後の処置時間を要するため生産性を向上できないというさらなる課題もある。
本発明の一態様に係る水熱処理装置は、高含水率バイオマスを加熱することで水熱処理する水熱処理装置であって、前記高含水率バイオマスを貯留する処理容器と、前記処理容器の鉛直方向上部に空間が形成されるように、前記処理容器の内部に前記高含水率バイオマスを供給する第1供給部と、前記処理容器の内部に設けられ、所定方向の流れが発生するように該高含水率バイオマスを撹拌する撹拌部と、前記処理容器の内部に前記所定方向と交差するように配置され、内部を流通する蒸気の熱によって前記高含水率バイオマスを加熱する少なくとも1つの伝熱管と、を備える。
また、撹拌部により、該高含水率バイオマスに所定方向の流れが発生するように撹拌されて、伝熱管が高含水率バイオマスの所定方向の流れに交差するように配置されているので、より多くの高含水率バイオマスを伝熱管と効率よく接触させて、加熱することができる。これにより、加水分解反応を促進させ、好適に水熱処理を行うことができる。したがって、水熱処理時間を短縮化することができる。
上記構成では、伝熱管を水平方向に延在するように配置している。したがって、鉛直上下方向に循環する高含水率バイオマスの対向流に対して、確実に、交差するように伝熱管を配置することができる。したがって、確実に、多くの高含水率バイオマスを伝熱管と接触させ、加熱することができる。したがって、処理容器内の高含水率バイオマスを均一に加水分解反応させることができるので、好適に水熱処理を行うことができる。
また、羽根部は、径方向の先端が、処理容器の内周面に近接するように配置されることで、処理容器の内周面に汚泥が付着して固化することを抑制することができる。
脱水部で分離された分離水にも、高含水率バイオマスに含有していた揮発成分や不純物が含まれているので、揮発成分や不純物を分離する処理を行う必要がある。上記構成では、脱水部で分離された分離水を処理容器へ導いている。このため、分離水は処理容器内で蒸発し、蒸気となって蒸気排出部から排出され、分離処理部で処理される。このように、分離水及び処理容器内で発生した蒸気を、一つの分離処理部で処理しているので、夫々に分離処理部を設ける構成と比較して、バイオマス燃料製造プラントの構造を簡素化することができる。したがって、省スペース化を図れるとともに、設置コストを低減することができる。
したがって、例えば、処理容器内に貯留されている貯留物の上面付近に、分岐配管を接続した場合には、上面付近に配置されている伝熱管に対して分離水を噴出させて高含水率バイオマスをパージすることができるので、上面付近に配置されている伝熱管に高含水率バイオマスの固着を抑制することができる。
また、例えば、処理容器の取出し口近傍に、分岐配管を接続した場合には、貯留物が詰まる可能性がある取出し口に対して分離水を噴射させて、貯留物をパージすることで、取出し口の閉塞を抑制することができる。
また、分離水を消化槽へ導くことで、消化槽で必要な熱を付与している。このように、脱水部から分離された分離水の保有熱を有効に利用しているので、分離水の熱を利用しない構成と比較して、バイオマス燃料製造プラント全体のエネルギー効率向上させることができる。
なお、以下の説明で、上方や上方向などの上および同様に下は、鉛直方向での上や下を示すものとする。
以下、本発明の第1実施形態について、図1から図5を用いて説明する。
本実施形態に係るバイオマス燃料製造プラント1は、図1に示すように、蒸気を生成するボイラ2と、ボイラ2からの蒸気の熱を用いて、例えば、汚泥(高含水率バイオマス)を水熱処理する水熱処理装置3と、水熱処理装置3で水熱処理された汚泥(以下、「処理物」という。)を脱水する脱水機(脱水部)4と、脱水機4で脱水された処理物を乾燥させる第1乾燥機(第4熱交換部)5及び第2乾燥機(第1熱交換部)6と、第1乾燥機5及び第2乾燥機6で乾燥された処理物をバイオマス燃料に成型する成型機7と、を備えている。また、バイオマス燃料製造プラント1は、下水処理設備8からの汚泥を、水熱処理装置3に導入する前に、脱水する汚泥脱水機9と、汚泥脱水機9で脱水した汚泥を一時的に貯留する汚泥貯留タンク(高含水率バイオマスタンク)17と、を備えている。汚泥脱水機9で分離された分離水は、処理場において、分離水に含まれた不純物や揮発成分(CH4、ベンゼン、HmSn化合物等)が、分離・除去される。
なお、以下の説明では、バイオマス燃料の原料の一例として、下水処理設備8から供給された下水汚泥を用いる例について説明するが、バイオマス燃料製造プラント1で処理される原料は下水汚泥に限定されない。高含水率バイオマス(湿潤燃料)であればよい。
ボイラ2には、蒸気供給配管11が接続されている。ボイラ2で生成された蒸気は、蒸気供給配管11を介して、水熱処理装置3の伝熱管24へ供給される。蒸気供給配管11のボイラ2の出口側もしくは伝熱管24の入口側などには、内部を流れる蒸気の温度を計測する温度計12が設けられている(図2参照)。温度計12が計測する蒸気の温度が所定の値より低い場合には、バーナに供給する燃料を増加させて、蒸気の温度を上昇させる。
また、ボイラ2には、ボイラ排ガス配管13が接続されている。ボイラ2から排出されたボイラ排ガスは、ボイラ排ガス配管13を介して、第2乾燥機6へ供給される。ボイラ2から排出されるボイラ排ガスは、例えば、300℃~400℃程度となっている。
第1蒸気排出配管26には、流量調整弁26aよりも下流側に復水器28が設けられていて、復水器28において、処理容器21から排出された蒸気を凝縮している。凝縮された凝縮水は、処理場(分離処理部)29において、凝縮水に含まれた不純物や揮発成分(CH4、ベンゼン、HmSn化合物等)が、分離・除去される。なお、凝縮水が導入される処理場29は、汚泥脱水機9から分離された分離水が導入される処理場と同じ施設であってもよく、また、別の施設であってもよい。
なお、第1供給側バルブ22a、リーク弁31b、第2供給側バルブ22b、第3供給側バルブ22c、及びフィーダ32の動作は、制御部18により制御される。
なお、処理容器21内に発生させる貯留物の流れは、別の流れであってもよい。例えば、回転軸41に沿って下方へ移動するとともに、処理容器21の内周面に沿って上方に移動する対向流を発生させてもよい。このような対向流を発生させるには、羽根部43を、回転の進行方向における前部が、後部よりも下方に位置するように傾斜させる、もしくは回転軸41の回転方向を逆にすればよい。
また、固定箇所に固定する棒部42の数も上記説明の数に限定されない。上記説明では、180度間隔で2本の棒部42を設ける例について説明したが、設ける棒部42の数は、例えば単数の棒部42を設けてもよいし、3本以上の複数の棒部42をもうけてもよい。なお、複数設ける場合には、撹拌能力を向上させるために、回転軸41の外周面の周方向に沿って等間隔に設けることが望ましい。すなわち、例えば、1つの固定箇所に4本の棒部42を設ける場合には、上面視で棒部42が十字状になるように配置することが望ましい。
本実施形態では、伝熱管24は、図2に示すように、水平方向に延在する複数(本実施形態では、一例として、4つ)の水平伝熱管51と、複数の水平伝熱管51同士を直列に連結する鉛直方向に延在する鉛直伝熱管52とを備えており、1本の連続した配管として蒸気供給ができるよう構成されている。
また、複数の水平伝熱管51は、複数の水平伝熱管51同士を並列に連結して蒸気の供給と回収が可能な伝熱管ヘッダとを備えることで、複数の水平伝熱管51と伝熱管ヘッダ(図示省略)との間には調整弁(図示省略)を設けて、複数の水平伝熱管51の間の蒸気供給バランスを調整可能になるよう構成されてもよい。
上述したように、処理容器21内では、上下方向に循環する貯留物の対向流が発生しているので、水平伝熱管51は、この流れに交差するように配置されている。
複数の水平伝熱管51は、図5に示すように、各々、管台21cから回転軸41を挟んで反対側に延びるとともに、複数回折り返した形状に形成されている。換言すれば、水平伝熱管51は、上面視でW字状に形成されている。また、水平伝熱管51は、撹拌機23と干渉しない位置に配置され、撹拌機23が回転軸41を中心として回転した場合でも水平伝熱管51と撹拌機23が物理的に接触しない位置に配置されている。
なお、複数の水平伝熱管51のうち、最下段に配置される水平伝熱管51は、処理容器21の底面付近のために、羽根部43に挟まれていないので、撹拌機23と干渉し難いことから、渦巻きコイル状に形成してもよい。このようにすることで、伝熱面積が増大するので、伝熱管24の伝熱効率を向上させることができる。
第3処理物配管65は処理物タンク62と脱水機4とを接続している。
なお、第1排出側バルブ25a、第2排出側バルブ25b、リーク弁61b、第3排出側バルブ25c、及び脱水機4の動作は、制御部18により行われる。
なお、最上段の水平伝熱管51及び取出し口以外に、清掃等の目的から分離水を供給したい部分がある場合には、図2の破線で示しているように、分離水配管71を2本以上に分岐させてもよい。
また、ブロー配管72には、内部を流通する分離水の流量を調整する流量調整弁72aが設けられている。流量調整弁72aは、分離水中に含まれる不純物成分として、例えば、汚泥の加水分解反応により、植物繊維(植物の細胞壁及び細胞膜)が破壊されて植物細胞中のナトリウム(Na)、カリウム(K)、リン(P)等の濃度に応じて、開度を調整し、ブロー配管72内を流通する分離水の流量を調整する。従い、処理容器21に供給される分離水に含まれる不純物成分が、処理容器21内に蓄積されて不純物成分の濃度が高くなり結晶化することを抑制できる。これにより、処理容器21内で不純物成分の結晶化による貯留物の粘性上昇を抑制し、処理容器21内の撹拌による加水分解反応促進や、処理容器21底部からの処理物の排出をスムーズにすることができる。
T5で第1排出側バルブ25a及び第2排出側バルブ25bを開状態とすると、排出チャンバー61と処理容器21が連通した状態となり、処理容器21内の底部にある処理物が排出チャンバー61に移動するので、T5からT6にかけて、処理容器21の貯留物量が低減する((e)参照)。処理容器21から所定量の処理物が排出されるタイミングであるT6で、第1排出側バルブ25a及び第2排出側バルブ25bを閉状態とする((f)参照)。排出チャンバー61と処理容器21が切り離した状態となる。次に、T7で第3排出側バルブ25cを開状態として、排出チャンバー61から処理物を排出する((g)参照)。処理物の排出が終了するタイミングであるT8で、第3排出側バルブ25cを閉状態とする。
このようにして、水熱処理装置3では、供給チャンバー31と排出チャンバー61とをそれぞれ処理容器21と連通した状態と切り離した状態とにできることで、処理容器21内の温度及び圧力を所定の温度及び圧力に保った状態で、汚泥の供給及び処理物の排出を連続的に行っているといえる。
本実施形態では、1度に導入される汚泥量は、処理容器21内の貯留物量の例えば20%と設定した場合を説明している。すなわち、処理容器21内の貯留物量をVとすると、1度に導入される汚泥量は、0.2Vとなる。また、処理容器21に汚泥が導入されてから、次の汚泥の導入までの時間(図6のT3からT9までの時間)であるサイクルタイムTを例えば5分と設定している。したがって、処理容器21内の貯留物がすべて入れ替わるのに要する時間は、下記式(1)から導かれ、25分となる。換言すれば、処理容器21内に導入された汚泥が、水熱処理を行われ、処理物として処理容器21から外部に排出されるまでの時間が25分となり、一般的な加水分解反応時間として適当な時間を確保することができる。
(V/0.2V)×T・・・(1)
撹拌機23の回転駆動機器の回転数と回転負荷(電流値など)の計測と動作は、制御部18内に設けた回転数制御部により行われてもよい。
まず、バイオマス製造プラントを用いた汚泥からバイオマス燃料を製造する方法について説明する。
下水処理設備8から水熱処理装置3の処理容器21に供給された汚泥は(供給工程)、処理容器21内において、所定の圧力下で、ボイラ2からの蒸気の熱で伝熱管24を介して間接的に加熱される(加熱工程)ことで、水熱処理を施され加水分解反応により細胞壁が破壊される。このとき、処理容器21内の貯留物は、撹拌機23によって、撹拌及び細分化がされる(撹拌工程)。
ボイラ2で生成された蒸気は、蒸気供給配管11を介して伝熱管24に供給される。ボイラ2から伝熱管24への蒸気の供給は、例えば0.8MPa~10MPa程度の飽和蒸気または過熱蒸気とし、加水分解温度(処理容器21内の維持温度)に、供給エネルギー相当温度(20度~50度、蒸気の潜熱分まで利用とし処理容器21に導入する汚泥量に合せて設定する)として蒸気供給配管11(例えばボイラ出口)に設けられた温度計12の計測温度で制御する。また、処理容器21内の温度が所定の温度(好適に加水分解反応を起こせる温度、例えば150度から230度)を維持できるよう、伝熱管24から戻る給水流量を給水ポンプ等で調整してもよい。
伝熱管24に供給された蒸気は、伝熱管24内を流通するとともに、伝熱管24を介して、処理容器21内の貯留物を間接的に加熱する。伝熱管24から排出された蒸気と一部ドレン化した温水は、第2蒸気排出配管53を介して、第1乾燥機5内に配置された第1熱交換器5aへ導入される。第1熱交換器5aへ導入された蒸気と温水は、第1熱交換器5aで、処理物と熱交換を行うことで処理物を間接的に加熱するとともに、蒸気は冷却され凝縮し、温水は温度が低下し凝縮水に混合される。凝縮した凝縮水は、第1乾燥機5から排出される。処理容器21においても第1乾燥機5においても間接熱交換が行われることで、給水には不純物や揮発成分(CH4、ベンゼン、HmSn化合物等)が混入されない。第1乾燥機5から排出された凝縮水は、給水供給配管54を介して、給水として、再度ボイラ2に供給される。
本実施形態に係るバイオマス燃料製造プラント1における蒸気等の流れは、以上のようになる。
本実施形態では、処理容器21内の貯留物が所定の含水率を維持するように、分離水を処理容器21に供給している。これにより、貯留物の流動性の低減を抑制することができる。したがって、常に、流動性を維持し、好適な撹拌を行うことができるので、均一な加水分解反応を起こすことができる。また、流動性を維持しているので、貯留物を容易に処理容器21から排出することができる。
脱水機4で分離された分離水にも、汚泥に含有していた揮発成分や不純物が含まれているので、揮発成分や不純物を分離する処理を行う必要がある。本実施形態では、脱水部で分離された分離水を処理容器21へ導いている。このため、分離水は処理容器21内で蒸発し、蒸気となって蒸気排出部から排出され、分離処理部で処理される。このように、分離水及び処理容器21内で発生した蒸気を、一つの分離処理部で処理しているので、夫々に分離処理部を設ける構成と比較して、バイオマス燃料製造プラント1の構造を簡素化することができる。したがって、省スペース化を図れるとともに、設置コストを低減することができる。
本実施形態では、水熱処理装置3で行う水熱処理を、いわゆる連続処理としている。すなわち、処理容器21内を降温させずに処理物(水熱処理で細胞壁が破壊された汚泥)を搬出可能としている。これにより、水熱処理装置3の処理容器21および処理物の降温による投入エネルギーのロスを抑制できる。また、バッチ処理を行う場合と比較して、昇温・昇圧する工程及び減圧する工程等を削減することができるので、効率的に水熱処理を行うことができる。
本実施形態では、ブロー配管72を設け、脱水機4から排出される分離水のうち、1%~10%(より好ましくは1%~5%)の分離水が常時排出されるようになっている。これにより、処理容器21内での不純物の蓄積濃縮を抑制して貯留物の粘性上昇を抑制することができる。
以下、第1実施形態の第1変形例について、図7を用いて説明する。
本変形例に係るバイオマス燃料製造プラント81は、図7に示すように、処理容器21から排出される蒸気が流通する蒸気排出配管の構造が、第1実施形態と異なる。第1実施形態と同様の構成については、同一の符号を付し、その詳細な説明は省略する。
分離水を加熱した蒸気は、復水器28に導入される。蒸気は冷却が進んでいるため、復水器28での冷却能力を軽減化できる。
以下、第1実施形態の第2変形例について、説明する。
本変形例に係るバイオマス燃料製造プラントは、伝熱管24の入口における蒸気温度と伝熱管24の出口における蒸気温度との温度差を計測する温度差計測手段、及び、温度差計測手段が計測した温度差に基づいて撹拌機23の回転軸41の回転速度を変化させる回転速度変化手段を備えている点で、第1実施形態と異なる。第1実施形態と同様の構成については、同一の符号を付し、その詳細な説明は省略する。
また、回転速度変化手段は、例えば、算出部が算出した温度差が所定の値以下である場合には、伝熱管24における熱交換が好適に行われておらず、伝熱管24に汚れが付着していると判断する判断部と、判断部からの情報に基づいて回転軸41を駆動するモータなどの回転駆動機器の回転数を上昇させる回転数制御部と、によって構成される。判断部と回転数制御部は、制御部18内に設けてもよい。
以下、第1実施形態の第3変形例について、説明する。
本変形例に係るバイオマス燃料製造プラントは、水熱処理装置3の運転開始時に、処理容器21内に追加の水または蒸気を供給する供給手段を備えている点で、第1実施形態と異なる。第1実施形態と同様の構成については、同一の符号を付し、その詳細な説明は省略する。
供給する追加の水または蒸気は、専用の流路を設けてもよく、また、前回の停止時に処理容器21内に残っていた液体分を保管しておき、この保管していた液体分を供給してもよい。
以下、本発明の第2実施形態について、図8を用いて説明する。
本実施形態に係るバイオマス燃料製造プラント91は、消化槽92、脱硫装置93、脱シロキサン装置94及びガスエンジン(内燃機関)95を備えている点で、主に第1実施形態と異なる。第1実施形態と同様の構成については、同一の符号を付し、その詳細な説明は省略する。
本実施形態では、消化槽92で処理容器21に供給する前の汚泥から揮発性ガスを取り出し、取り出した揮発性ガスを内燃機関用燃料ガスの一部または全てに用いることでガスエンジン95を駆動している。また、ガスエンジン95の内燃機関排ガスと、水熱処理された処理物とを熱交換させることで、処理物を排ガスで加熱し、乾燥させている。このように、ガスエンジン95の内燃機関排ガスの熱を利用して、水熱処理された処理物の乾燥させることができるので、ガスエンジン95の排ガスの熱を利用しない構成と比較して、バイオマス燃料製造プラント91全体のエネルギー効率を向上させることができる。
また、脱水機4から分離された分離水を消化槽92へ導くことで、消化槽92で必要な熱を付与している。このように、脱水機4から分離された分離水の熱を利用しているので、分離水の熱を利用しない構成と比較して、バイオマス燃料製造プラント91全体のエネルギー効率を向上させることができる。
以下、第2実施形態の変形例について、図9を用いて説明する。
本変形例に係るバイオマス燃料製造プラント101は、図9に示すように、処理容器21の伝熱管24から排出された蒸気及び一部ドレン化した温水を、第1乾燥機5に供給せず、分離水タンク73へ導く点、ボイラ2から排出されたボイラ排ガスを第2乾燥機6ではなく第1乾燥機5へ導く点、及び、ガスエンジン95から排出された内燃機関排ガスを第2乾燥機6へ導く点が、主に第2実施形態と異なる。第2実施形態と同様の構成については、同一の符号を付し、その詳細な説明は省略する。
例えば、上記各実施形態では、脱水機4で分離された分離水を処理容器21に導入することで、処理容器21内の貯留物の含水率を維持する例について説明したが、本発明はこれに限定されない。例えば、処理容器21に、ボイラ2で生成した蒸気を供給して貯留物の含水率を維持してもよい。また、ボイラ2からの蒸気及び脱水機4で分離された分離水の両方を供給して貯留物の含水率を維持してもよい。
また、内燃機関にガスエンジンを用いているが、小型ボイラと小型蒸気タービンによる発電システムであってもよい。
2 :ボイラ
3 :水熱処理装置
4 :脱水機(脱水部)
5 :第1乾燥機(第4熱交換部)
5a :第1熱交換器
6 :第2乾燥機(第1熱交換部、第3熱交換部)
6a :第2熱交換器
7 :成型機
8 :下水処理設備
9 :汚泥脱水機
10 :燃料供給配管
11 :蒸気供給配管
12 :温度計
13 :ボイラ排ガス配管
14 :脱臭機
15 :脱塵機
16 :煙突
17 :汚泥貯留タンク(高含水率バイオマスタンク)
17a :汚泥貯留タンク熱交換器(第6熱交換部)
18 :制御部
21 :処理容器
21a :天井部
21b :本体部
21c :管台(固定部)
22 :汚泥供給部(第1供給部)
22a :第1供給側バルブ
22b :第2供給側バルブ(第1切替え手段)
22c :第3供給側バルブ(第1切替え手段)
23 :撹拌機(撹拌部)
24 :伝熱管
25 :処理物排出部
25a :第1排出側バルブ(第2切替え手段)
25b :第2排出側バルブ(第2切替え手段)
25c :第3排出側バルブ
26 :第1蒸気排出配管(蒸気排出部)
26a :流量調整弁
27 :圧力計
28 :復水器
29 :処理場(分理処理部)
31 :供給チャンバー
31a :リーク流路
31b :リーク弁
32 :フィーダ
33 :第1汚泥配管
34 :第2汚泥配管
35 :第3汚泥配管
41 :回転軸
42 :棒部
43 :羽根部
44 :シール構造
45 :弾力性緩衝体
51 :水平伝熱管
52 :鉛直伝熱管
53 :第2蒸気排出配管
54 :給水供給配管
55 :流量計
56 :給水タンク
57 :配管
61 :排出チャンバー
61a :リーク流路
61b :リーク弁
62 :処理物タンク
63 :第1処理物配管
64 :第2処理物配管
65 :第3処理物配管
71 :分離水配管(第2供給部、第1分離水流路)
71a :第1分岐配管
71b :第2分岐配管
71c :第1流量調整弁
71d :第2流量調整弁
72 :ブロー配管
72a :流量調整弁
73 :分離水タンク
73a :分離水タンク熱交換器(第5熱交換部)
76 :第4処理物配管
77 :第5処理物配管
78 :第6処理物配管
81 :バイオマス燃料製造プラント
82 :蒸気排出配管
91 :バイオマス燃料製造プラント
92 :消化槽
93 :脱硫装置
94 :脱シロキサン装置
95 :ガスエンジン(内燃機関)
96 :ガスエンジン排ガス配管
97 :分離水流路(第2分離水流路)
101 :バイオマス燃料製造プラント
102 :第3蒸気排出配管
103 :第4蒸気排出配管
104 :第5蒸気排出配管
105 :タンク
S :空間
Claims (18)
- 高含水率バイオマスを加熱することで水熱処理する水熱処理装置であって、
前記高含水率バイオマスを貯留する処理容器と、
前記処理容器の鉛直方向上部に空間が形成されるように、前記処理容器の内部に前記高含水率バイオマスを供給する第1供給部と、
前記処理容器の内部に設けられ、所定方向の流れが発生するように該高含水率バイオマスを撹拌する撹拌部と、
前記処理容器の内部に前記所定方向と交差するように配置され、内部を流通する蒸気の熱によって前記高含水率バイオマスを加熱する少なくとも1つの伝熱管と、を備える水熱処理装置。 - 前記撹拌部は、水平面に対して傾斜するように配置される羽根部を備え、
前記羽根部は、鉛直上下方向に延在する軸方向を中心として回転し、
前記羽根部の径方向の先端は、前記処理容器の内周面に近接するように配置され、
前記伝熱管は、水平方向に延在している請求項1に記載の水熱処理装置。 - 前記撹拌部は、鉛直上下方向に延在する軸方向を中心として回転する複数の羽根部を備え、
複数の前記羽根部は、回転の中心となる前記軸方向から、径方向に所定距離離間した位置に、前記軸方向の周方向に沿って等間隔に配置されるとともに、各々、水平面に対して回転方向に向かって所定の角度で傾斜するように配置されていて、
前記伝熱管は、水平方向に延在していて、
前記所定方向の流れは、鉛直上方向および鉛直下方向を含む対向流である請求項1に記載の水熱処理装置。 - 前記処理容器内の貯留物の少なくとも一部が所定の含水率を維持するように水または蒸気を前記処理容器に供給する第2供給部を備えた請求項1から請求項3のいずれかに記載の水熱処理装置。
- 前記処理容器は、側面と底面をなす本体部及び鉛直上面をなす天井部を有する外殻と、前記伝熱管の少なくとも1つを前記本体部に対して固定する固定部と、を備え、
前記天井部は、前記本体部に取外し可能に固定され、
前記固定部は、前記本体部に取外し可能に固定されている請求項1から請求項4のいずれかに記載の水熱処理装置。 - 前記処理容器に前記高含水率バイオマスを供給する供給チャンバーと、
前記処理容器内に貯留された貯留物が排出される排出チャンバーと、
前記供給チャンバーと前記処理容器とが連通した状態と、前記供給チャンバーと前記処理容器とが隔絶された状態と、を切替える第1切替え手段と、
前記排出チャンバーと前記処理容器とが連通した状態と、前記排出チャンバーと前記処理容器とが隔絶された状態と、を切替える第2切替え手段と、を備え、
前記処理容器内の温度及び圧力を所定の温度及び圧力に保った状態で、前記供給チャンバーから前記処理容器への前記高含水率バイオマスの供給を行うとともに、前記処理容器から前記排出チャンバーへの前記貯留物の排出を行う請求項1から請求項5のいずれかに記載の水熱処理装置。 - 前記処理容器内で水熱処理時に、前記処理容器内の前記高含水率バイオマスの位置による温度差が、所定の温度差の範囲内となるように、前記撹拌部の回転速度を調整する制御部を備えた請求項1から請求項6のいずれかに記載の水熱処理装置。
- 請求項1から請求項7のいずれかに記載の水熱処理装置を備えたバイオマス燃料製造プラントであって、
前記水熱処理装置で水熱処理された前記高含水率バイオマスを脱水する脱水部と、
前記脱水部において前記高含水率バイオマスから分離された分離水を前記処理容器へ導く第1分離水流路と、
前記処理容器内で発生した蒸気を、該処理容器の外部に排出する蒸気排出部と、
前記蒸気排出部から排出された蒸気から不純物を分離する分離処理部と、を備えたバイオマス燃料製造プラント。 - 前記第1分離水流路が分岐した複数の分岐配管を備え、
複数の前記分岐配管は、前記処理容器の鉛直上下方向の異なる位置へ連通している請求項8に記載のバイオマス燃料製造プラント。 - 前記脱水部で分離された分離水のうち、所定の割合の分離水を外部へ排出するブロー配管を備えた請求項8または請求項9に記載のバイオマス燃料製造プラント。
- 投入した燃料の燃焼熱で蒸気を生成し、生成した蒸気を前記伝熱管に供給するボイラと、
前記水熱処理装置で水熱処理された前記高含水率バイオマスと前記ボイラから排出されるボイラ排ガスとを熱交換させる第1熱交換部と、を備えた請求項8から請求項10のいずれかに記載のバイオマス燃料製造プラント。 - 前記処理容器に供給する前の前記高含水率バイオマスが導入される消化槽と、
前記脱水部において前記高含水率バイオマスから分離された分離水を前記消化槽へ導く第2分離水流路と、
前記消化槽から排出される燃料ガスを含む内燃機関用燃料ガスを燃焼することで駆動する内燃機関と、
前記水熱処理装置で水熱処理された前記高含水率バイオマスと前記内燃機関から排出される内燃機関排ガスとを熱交換させる第2熱交換部と、を備える請求項8から請求項11のいずれかに記載のバイオマス燃料製造プラント。 - 投入した燃料の燃焼熱で蒸気を生成し、生成した蒸気を前記伝熱管に供給するボイラと、
前記処理容器に供給する前の前記高含水率バイオマスが導入される消化槽と、
前記脱水部において前記高含水率バイオマスから分離された分離水を前記消化槽へ導く第2分離水流路と、
前記消化槽から排出される燃料ガスを含む内燃機関用燃料ガスを燃焼することで駆動する内燃機関と、
前記水熱処理装置で水熱処理された前記高含水率バイオマスと前記ボイラから排出されるボイラ排ガス及び前記内燃機関から排出される内燃機関排ガスとを熱交換させる第3熱交換部と、を備える請求項8から請求項10のいずれかに記載のバイオマス燃料製造プラント。 - 前記水熱処理装置で水熱処理された前記高含水率バイオマスと前記伝熱管から排出された蒸気とを熱交換させる第4熱交換部を備える請求項8から請求項13のいずれかに記載のバイオマス燃料製造プラント。
- 前記伝熱管から排出された蒸気と前記脱水部から排出された前記分離水とを熱交換させる第5熱交換部を備えた請求項8から請求項14のいずれかに記載のバイオマス燃料製造プラント。
- 前記処理容器に供給する前記高含水率バイオマスを貯留する高含水率バイオマスタンクと、
前記伝熱管から排出された蒸気と前記高含水率バイオマスタンク内の前記高含水率バイオマスとを熱交換させる第6熱交換部と、を備えた請求項8から請求項15のいずれかに記載のバイオマス燃料製造プラント。 - 高含水率バイオマスを加熱することで水熱処理する水熱処理方法であって、
処理容器の鉛直方向上部に空間が形成されるように、前記処理容器の内部に前記高含水率バイオマスを供給する供給工程と、
前記処理容器の内部に設けられ撹拌部によって、所定方向の流れが発生するように該高含水率バイオマスを撹拌する撹拌工程と、
前記処理容器の内部に前記所定方向と交差するように配置された少なくとも1つの伝熱管の内部を流通する蒸気によって、前記高含水率バイオマスを加熱する加熱工程と、を備える水熱処理方法。 - 請求項17に記載された水熱処理方法を用いたバイオマス燃料製造方法。
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BR112020025133A8 (pt) | 2022-12-20 |
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US20210230494A1 (en) | 2021-07-29 |
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