WO2012042841A1 - Procédé de saccharification/décomposition de la biomasse cellulosique et appareil de saccharification/décomposition - Google Patents

Procédé de saccharification/décomposition de la biomasse cellulosique et appareil de saccharification/décomposition Download PDF

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Publication number
WO2012042841A1
WO2012042841A1 PCT/JP2011/005420 JP2011005420W WO2012042841A1 WO 2012042841 A1 WO2012042841 A1 WO 2012042841A1 JP 2011005420 W JP2011005420 W JP 2011005420W WO 2012042841 A1 WO2012042841 A1 WO 2012042841A1
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Prior art keywords
hydraulic
hydraulic cylinder
cylinder type
steam
pressure
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Ceased
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PCT/JP2011/005420
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English (en)
Japanese (ja)
Inventor
浩雅 楠田
憲明 和泉
浩範 田尻
章次 ▲辻▼田
西野　毅
田中　邦彦
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Kawasaki Heavy Industries Ltd
Kawasaki Motors Ltd
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Kawasaki Heavy Industries Ltd
Kawasaki Jukogyo KK
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Priority to US13/813,583 priority Critical patent/US20130125877A1/en
Priority to JP2012504967A priority patent/JPWO2012042841A1/ja
Publication of WO2012042841A1 publication Critical patent/WO2012042841A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
    • C—CHEMISTRY; METALLURGY
    • C13—SUGAR INDUSTRY
    • C13K—SACCHARIDES OBTAINED FROM NATURAL SOURCES OR BY HYDROLYSIS OF NATURALLY OCCURRING DISACCHARIDES, OLIGOSACCHARIDES OR POLYSACCHARIDES
    • C13K1/00—Glucose; Glucose-containing syrups
    • C13K1/02—Glucose; Glucose-containing syrups obtained by saccharification of cellulosic materials
    • 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 OR C10K; LIQUIFIED PETROLEUM GAS; USE OF ADDITIVES TO FUELS OR FIRES; FIRE-LIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only

Definitions

  • the present invention relates to a method and an apparatus for producing saccharides by hydrolyzing cellulosic biomass in a supercritical state or a subcritical state.
  • the main components of the plant are cellulose (polymer of glucose, a C6 monosaccharide composed of 6 carbons), hemicellulose (polymer of C5 and C6 monosaccharides composed of 5 carbons), lignin
  • cellulose polymer of glucose, a C6 monosaccharide composed of 6 carbons
  • hemicellulose polymer of C5 and C6 monosaccharides composed of 5 carbons
  • lignin lignin
  • ethanol is produced by fermentation of microorganisms such as yeast using saccharides such as C5 monosaccharides, C6 monosaccharides, and oligosaccharides, which are complexes thereof, as raw materials.
  • Cellulosic biomass such as cellulose or hemicellulose is decomposed into saccharides by 1) hydrolysis using strong acid such as sulfuric acid, 2) enzymatic decomposition, 3) supercritical water or subcritical water oxidation.
  • strong acid such as sulfuric acid
  • enzymatic decomposition 3) supercritical water or subcritical water oxidation.
  • Three types of methods using power are going to be used industrially.
  • the acid decomposition method of 1) since the added acid becomes an inhibitor for yeast fermentation, after the cellulose or hemicellulose is decomposed into saccharides, the saccharides are added before ethanol fermentation. Sum processing is indispensable, and its processing cost is difficult to put into practical use economically.
  • the enzymatic decomposition method 2) can be processed at room temperature and constant pressure, an effective enzyme has not been found, and even if it is discovered, the production cost of the enzyme is expected to increase. There is still no prospect of realization on an industrial scale.
  • Patent Document 3 A method for hydrolyzing cellulose biomass by supercritical water or subcritical water to form sugars by contacting cellulose powder with pressurized hot water at 240 to 340 ° C.
  • a method for producing a water-soluble polysaccharide is disclosed in Patent Document 1.
  • Patent Document 2 discloses a method in which a fragmented biomass is hydrolyzed with hot water pressurized at 140 to 230 ° C. to a saturated water vapor pressure or higher for a predetermined time to decompose and extract hemicellulose, and then heated to a temperature higher than the decomposition temperature of cellulose.
  • a method for decomposing and extracting cellulose by hydrolyzing with hot water is disclosed.
  • cellulose having an average degree of polymerization of 100 or more is contact-reacted with supercritical water or subcritical water having a temperature of 250 ° C. or more and 450 ° C. or less and a pressure of 15 MPa or more and 450 MPa or less and 0.01 seconds or more and 5 seconds or less, and then cooled.
  • a method for producing glucose and / or water-soluble cellooligosaccharide which comprises hydrolyzing by contacting with subcritical water at a temperature of 250 ° C. to 350 ° C. and a pressure of 15 MPa to 450 MPa for 1 second to 10 minutes. Yes.
  • Patent Document 4 discloses a reactor in which water vapor supplied from a boiler is pressurized with a piston to form supercritical water or subcritical water. .
  • Patent Document 4 discloses that a cylinder of a reactor is driven by a crank mechanism or a cam mechanism, steam is collected from a product taken out from the reactor, and steam pressure is used to drive the crank mechanism or the cam mechanism. ing.
  • Patent Document 5 discloses an organic matter system for supplying a fluid containing organic matter at a high temperature and high pressure at a stable flow rate.
  • the system disclosed in Patent Document 5 includes a first driving unit that receives a high-pressure fluid and pressure after processing by a piston of a cylinder as a force for pressurizing the fluid before processing, and a first driving unit. And a second driving means for adding a driving force to the cylinder, and the energy of the high-pressure fluid after processing is reduced by using a back pressure valve and then introduced into the cylinder of the first driving means.
  • the present invention relates to a method and apparatus for decomposing cellulosic biomass in a supercritical state or a subcritical state, and recovering excess pressure when reducing the pressure of the reactor to reduce the compression power, and operating the reactor and the compression mechanism.
  • the purpose is to ensure timing freedom.
  • Another object of the present invention is to improve the thermal efficiency by recovering latent heat by circulating and using flash steam.
  • a hydraulic cylinder type pressurized reactor is used as a reactor for bringing cellulosic biomass into a supercritical state or a subcritical state, and a hydraulic cylinder type steam compressor is used as a supply source of superheated steam. I tried to make it work together.
  • the excess hydraulic pressure at the end of the decomposition of the cellulosic biomass is recovered as the compression power of the hydraulic cylinder type steam compressor, and the flash steam generated from the slurry containing the decomposition product is further transferred to the hydraulic cylinder type steam compressor.
  • the present invention is a method for saccharifying and decomposing cellulosic biomass by saccharifying and decomposing cellulosic biomass by pressurizing a cellulosic biomass slurry with superheated steam in a hydraulic cylinder type pressure reactor until it reaches a supercritical state or a subcritical state.
  • Superheated steam supply to the hydraulic cylinder type pressurized reactor is performed by a hydraulic cylinder type steam compressor, By connecting the hydraulic pressure return path of the hydraulic cylinder type pressurized reactor and the hydraulic chamber of the hydraulic cylinder type steam compressor by a hydraulic pressure recovery path, after the saccharification and decomposition of cellulosic biomass, the hydraulic cylinder type pressurized reactor When depressurizing the inside to a supercritical state or a subcritical state or less, the hydraulic pressure of the hydraulic cylinder type pressurized reactor is recovered into the hydraulic chamber of the hydraulic cylinder type steam compressor, The slurry after saccharification and decomposition is supplied into the flash tank and then flash evaporated, and the flash steam is recovered into the hydraulic cylinder type steam compressor. It is related with the method characterized by this.
  • the present invention also provides A hydraulic cylinder type pressure reactor for pressurizing a slurry of cellulosic biomass with superheated steam until it becomes a supercritical state or a subcritical state;
  • a hydraulic cylinder type steam compressor for supplying superheated steam to the hydraulic cylinder type pressurized reactor;
  • a flash tank for supplying a high-temperature and high-pressure slurry taken out from the plurality of hydraulic cylinder type pressure reactors and flash-evaporating;
  • the hydraulic pressure return path of the hydraulic cylinder type pressurized reactor and the hydraulic chamber of the hydraulic cylinder type steam compressor are connected by a hydraulic pressure recovery path, and the hydraulic pressure of the hydraulic chamber of the hydraulic cylinder type pressurized reactor is: Recovered into the hydraulic chamber of the hydraulic cylinder type steam compressor by the hydraulic recovery path,
  • the flash tank is connected to the hydraulic cylinder type steam compressor, and relates to an apparatus that collects flash steam generated from a high-temperature and high-pressure slurry into the hydraulic cylinder type steam compressor.
  • the hydraulic cylinder type pressurized reactor and the hydraulic cylinder type steam compressor are plural, superheated steam supply to the hydraulic cylinder type pressurized reactor is performed by the same number of hydraulic cylinder type steam compressors, After the saccharification and decomposition of cellulosic biomass, the oil pressure return path of one hydraulic cylinder type pressurized reactor and the hydraulic chamber of one hydraulic cylinder type steam compressor are connected by a hydraulic pressure recovery path, and then the oil pressure When depressurizing the inside of a cylinder type pressurization reactor to a supercritical state or a subcritical state or less, the hydraulic pressure of the hydraulic chamber of one hydraulic cylinder type pressurization type reactor is reduced to one hydraulic cylinder type steam compressor. It is preferable to periodically recover to the hydraulic chamber.
  • the hydraulic pressure recovery path is a single path at the connection portion between the hydraulic pressure return path and the hydraulic chamber of the hydraulic cylinder type steam compressor, and branches at other portions into a plurality of sub paths, Each sub-path has one air chamber with a different pressure accumulation setting value, After accumulating the hydraulic pressure in the hydraulic chamber of the hydraulic cylinder type pressurization reactor in order from the air chamber having the higher pressure accumulation setting value, the hydraulic pressure is released in order from the air chamber having the lower pressure accumulation setting value, and the hydraulic cylinder type steam compressor It is preferable to supply the hydraulic chamber.
  • a steam generator is connected to the flash tank, the steam supplied from the steam generator is mixed with the flash steam, and the steam is supplied to the hydraulic cylinder type steam compressor.
  • An air and / or nitrogen supply device is connected to at least one of the flash tank or the steam pipe connecting the flash tank and the hydraulic cylinder type steam compressor, and the steam compression chamber of the hydraulic cylinder type steam compressor is connected. It is preferable to mix 1/7 or more and 1/3 or less of air and / or nitrogen into the water vapor supplied to.
  • the present invention it is possible to reduce the compression power by collecting the surplus pressure (surplus oil pressure) of the reactor in the steam compressor via the hydraulic path. According to the present invention, since the latent heat of flash vapor can be recovered, the thermal efficiency is also high. Furthermore, according to the present invention, it is easy to link the reactor and the vapor compressor. Furthermore, by mixing air and / or nitrogen with flash steam, condensation of water vapor in the steam compressor can be prevented.
  • FIG. 1 shows the schematic block diagram explaining an example of the processing apparatus for performing the saccharification decomposition
  • FIG. 2 is a conceptual diagram for explaining the operation of the hydraulic cylinder type steam compressor 5a and the hydraulic cylinder type pressurized reactor 1a.
  • FIG. 3 is a schematic configuration diagram in the vicinity of the hydraulic cylinder type steam compressor 5a and the hydraulic cylinder type pressurized reactor 1a in another example of the processing apparatus for performing the saccharification / decomposition method of cellulosic biomass of the present invention.
  • FIG. 4 shows the schematic block diagram which shows an example of the conventional processing apparatus for performing the saccharification decomposition method of a cellulose biomass.
  • FIG. 1 is a schematic configuration diagram showing an example of a processing apparatus for performing the saccharification / decomposition method for cellulosic biomass of the present invention.
  • FIG. 1 four hydraulic cylinder type pressurized reactors and four hydraulic cylinder type steam compressors are installed, but the number of installed units is not limited to four.
  • the cellulosic biomass slurry is preheated as necessary, and then supplied to the high-pressure steam supply paths 10a to 10d via the slurry supply paths 11 and 11a to 11d.
  • a slurry of cellulosic biomass for example, (1) vegetation biomass such as bagasse, sugar beet lees, or straw is crushed to a particle size of several mm or less, and the solid concentration is about 20 to 50% by weight using water.
  • Residue (dehydrated cake) obtained by saccharifying and decomposing hemicellulose in straw-cellulosic biomass and then dehydrating it again with water to a solids concentration of about 20 to 50% by weight It may be a slurry.
  • water vapor supplied from a steam generator (not shown) such as a boiler is supplied from the path 12 to the flash tank 13 and further passes through the recovery steam supply paths 14 and 14a to 14d to be hydraulic cylinder type steam compression. Is supplied to the vapor compression chambers 8a to 8d of the machines 5a to 5d.
  • the steam supplied from the steam generator is preferably 150 to 200 ° C. and 0.5 to 1.6 MPa.
  • the temperature of the water vapor supplied from the recovered steam supply path 14 decreases. Cheap.
  • water vapor is condensed in the vapor compression chambers 8a to 8d, and the latent heat of the water vapor may be lost.
  • it is considered effective to insulate the steam pipe, but on the other hand, it is difficult to heat the steam pipe at the start of operation.
  • the processing apparatus shown in FIG. 1 is provided with pipes 28, 28a and 28b as an arbitrary configuration.
  • the pipe 28 is connected to an air and / or nitrogen supply device (not shown). Examples of supply devices are air compressors, gas cylinders or nitrogen generators.
  • the pipe 28 is branched into a pipe 28 a and a pipe 28 b, the pipe 28 a is connected to the flash tank 13, and the pipe 28 b is connected to the steam supply path. Either the pipe 28a or the pipe 28b may be omitted.
  • air and / or nitrogen When air and / or nitrogen is supplied from the pipe 28a and the pipe 28b, air and / or nitrogen is mixed with the steam in the flash tank 13 and the recovered steam supply path 14, and the steam of the hydraulic cylinder type steam compressor. Air and / or nitrogen can be mixed into the water vapor supplied to the compression chambers 8a to 8d. As a result, the steam is no longer saturated, so that it is difficult for the steam to condense when it is introduced into the steam compression chambers 8a to 8d.
  • the pressure of air and / or nitrogen supplied to the flash tank 13 and / or the recovered steam supply path 14 is adjusted so as to be the same pressure as the water vapor, and the air and / or nitrogen pressure is adjusted to a predetermined ratio.
  • Such a mixing ratio can be adjusted by adjusting the flow rate.
  • the pressure in the reaction chambers 4a to 4d should be set to be 10% to 30% higher than when no air and / or nitrogen is supplied. Is preferred. This is because the water vapor partial pressure is set to the same pressure as when air and / or nitrogen is not supplied.
  • the steam is supplied to the steam compression chamber 8a of the hydraulic cylinder type steam compressor 5a through the steam supply path 14a.
  • the volume of the hydraulic chamber 6a becomes the smallest, and the hydraulic pressure in the hydraulic chamber 6a is returned to the oil tank 26 via the hydraulic pressure return paths 19a and 19.
  • the hydraulic cylinder type pressurized reactor 1a compresses the reaction chamber 4a to which the slurry of the cellulosic biomass and the superheated steam are supplied, and decomposes the cellulosic biomass in a supercritical state or a subcritical state.
  • the water vapor is compressed by the hydraulic cylinder type vapor compressor 5a and then further compressed in the reaction chamber 4a, so that the temperature and pressure are the highest.
  • the inside of the reaction chamber 4a is preferably set to 350 to 400 ° C. and 18 to 30 MPa.
  • the decomposition time is preferably 0.1 to 30 seconds, and more preferably 0.1 to 3 seconds.
  • the hydraulic path 15a is a high-pressure hydraulic path of about 22 MPa, and in the state of FIG. 2 (a), the reaction chamber 4a to which the slurry of cellulosic biomass and superheated steam is supplied is compressed, and is in a supercritical state or a subcritical state. Therefore, the hydraulic cylinder 3a is pushed with a hydraulic pressure of about 22 MPa.
  • the hydraulic path 16a is a low pressure hydraulic path of about 2 MPa.
  • the hydraulic cylinder 3a is moved to the leftmost position in the drawing at about 2 MPa.
  • the volume of the reaction chamber 4a is made zero.
  • FIG. 2 (d) is followed by the state shown in FIG. 2 (a). Thereafter, the operations shown in FIG. 2 (a) ⁇ FIG. 2 (b) ⁇ FIG. 2 (c) ⁇ FIG. 2 (d) are repeated continuously. Since such oil pressure recovery is continuously performed, the compression power can be reduced.
  • the surplus pressure at the time of depressurizing the reactor is recovered as a hydraulic pressure to the steam compressor, it is easy to adjust the reaction time in the reactor according to the processing object or the processing amount.
  • the degree of freedom in changing the operating conditions is very large, for example, by adjusting the time by a partial cycle of the reactor.
  • the invention is greatly different from the invention disclosed in Patent Document 4 or 5.
  • Flash steam recovery> Next, the collection
  • the post-reaction slurry becomes a pressure of about 0.1 to 1.6 MPa.
  • the post-reaction slurry is transferred from the bottom of the flash tank 13 to a liquid storage facility or fermentation apparatus outside the apparatus by a pump 22.
  • the flash steam generated in the flash tank 13 is supplied to the hydraulic cylinder type steam compressors 5a to 5d through the steam supply paths 14, 14a to 14d, and the above-described processing steps are repeated.
  • the inside of the flash tank 13 does not reach the predetermined temperature and pressure, water vapor is supplied from the steam generator to the flash tank 13.
  • the inside of the flash tank 13 exceeds a predetermined temperature and pressure, excess steam is exhausted outside the system.
  • the post-reaction slurry can be rapidly cooled by flash evaporation, and the flash steam generated from the post-reaction slurry is recovered as water vapor for decomposition of the cellulosic biomass, so that the latent heat of the flash steam is also recovered. obtain. Since such steam recovery is continuously performed, the thermal efficiency can be improved.
  • FIG. 3 is a schematic configuration showing a connection state of a hydraulic cylinder type steam compressor 5a and a hydraulic cylinder type pressurized reactor 1a in another example of a processing apparatus for performing the saccharification / decomposition method of cellulosic biomass of the present invention.
  • FIG. This processing apparatus is the same as the processing apparatus shown in FIG. 1 except that the hydraulic pressure recovery path between the hydraulic cylinder type steam compressor 5a and the hydraulic cylinder type pressurized reactor 1a is different.
  • a hydraulic pressure recovery path 32 is connected to the hydraulic pressure return path 17a, and the hydraulic pressure recovery path 32 is branched into four sub-paths 32a to 32d.
  • the sub-paths 32a to 32d are provided with hydraulic valve sets 33a to 33d, respectively.
  • the sub paths 32a to 32d are connected to the air chamber paths 35a to 35d, respectively.
  • Air chambers P 1 to P 4 are provided at the ends of the air chamber paths 35a to 35d, respectively.
  • the pressures accumulated in the air chambers P 1 to P 4 are set to 3 MPa, 8 MPa, 13 MPa, and 18 MPa, respectively.
  • Sub-paths 36a to 36d are connected to the air chamber paths 35a to 35d, respectively.
  • the sub-paths 36a to 36d are provided with hydraulic valve sets 37a to 37d, respectively.
  • the sub-paths 36a to 36d are connected to the hydraulic chamber 6a of the hydraulic cylinder type steam compressor 5a via the hydraulic pressure supply path 36.
  • FIG. 3 shows the connection state of the hydraulic cylinder type steam compressor 5a and the hydraulic cylinder type pressurized reactor 1a.
  • the hydraulic cylinder type steam compressors 5b to 5d and the hydraulic cylinder type pressurized reactor 1b are shown.
  • the air chambers P 1 to P 4 are shared by four sets of hydraulic cylinder type steam compressors and hydraulic cylinder type pressurized reactors.
  • the valve 38 is opened. Then open the hydraulic valve 37a, the hydraulic pressure of 3MPa which has been accumulated in the hydraulic chamber P 1 is, through the air chamber passage 35a and the sub route 36a, and is supplied to the hydraulic chamber 6a. After supplying the hydraulic pressure, the hydraulic valve 37a is closed.
  • opening hydraulic valve 37d the 18MPa which has been accumulated in the hydraulic chamber P 4 hydraulic pressure, through the air chamber passage 35d and the sub route 36d, is supplied to the hydraulic chamber 6a.
  • the hydraulic valve 37d is closed.
  • the valve 38 is also closed, and one hydraulic pressure recovery cycle is completed.
  • the hydraulic valve sets 33a to 33d and 37a to 37d are composed of, for example, hydraulic counter balance valves and sequence valves, and automatically open their paths within a predetermined pressure range. A function is provided to close the path when the pressure is out of the preset pressure range.
  • the configurations of the hydraulic valve sets 33a to 33d and 37a to 37d and the air chambers P 1 to P 4 shown in FIG. 3 are examples of the hydraulic valve set and the air chamber that can be used in the embodiment of the present invention.
  • the configuration of the hydraulic path, the hydraulic valve set, or the air chamber is not limited to this.
  • the hydraulic pressure in the hydraulic chamber 2a of the hydraulic cylinder type pressurized reactor 1a is about 22 MPa
  • the hydraulic pressure in the hydraulic chamber 6a of the hydraulic cylinder type steam compressor 5a is about 0.1 to 0.6 MPa.
  • the hydraulic pressure difference is too large and the oil moving speed becomes excessive, and pressure loss and vibration are generated due to the frictional resistance of the hydraulic piping.
  • the pressure reducing valve becomes a large resistance, and pressure loss is inevitable.
  • the air chambers P 1 to P 4 is characterized in that after the pressure is accumulated in order from the highest oil pressure, the oil pressure is supplied in order from the lowest oil pressure.
  • the air chambers P 1 to P 4 is characterized in that after the pressure is accumulated in order from the highest oil pressure, the oil pressure is supplied in order from the lowest oil pressure.
  • FIG. 4 is a schematic configuration diagram illustrating an example of a conventional processing apparatus for performing a saccharification / decomposition method for cellulosic biomass.
  • This processing apparatus is composed of the cellulose-based biomass of the present invention in that the cellulosic biomass is decomposed into a supercritical state or a subcritical state by compressing the slurry of cellulose-based biomass and superheated steam with a hydraulic cylinder type pressure reactor.
  • a steam generator not shown
  • a steam compressor not shown
  • a hydraulic cylinder type pressurized reactor not configured to collect flash vapor from the slurry after the reaction.
  • the slurry of cellulosic biomass is supplied to the reaction chamber 46 of the hydraulic cylinder type pressure reactor 43 through the slurry supply path 41.
  • the superheated steam supplied from the steam generator is supplied to the reaction chamber 46 of the hydraulic cylinder type pressurized reactor 43 through the high-pressure steam supply path 42.
  • the hydraulic cylinder type pressurized reactor 43 moves the hydraulic cylinder 45 by the hydraulic pressure supplied from the hydraulic path 47.
  • the oil in the hydraulic tank 56 is supplied to the hydraulic path 47 by the hydraulic pump 49.
  • the hydraulic cylinder type pressurized reactor 43 compresses the reaction chamber 46 to which the slurry of cellulosic biomass and high-pressure steam (superheated steam) are supplied, and decomposes the cellulosic biomass into a supercritical state or a subcritical state. After the decomposition reaction of the cellulosic biomass, the inside of the reaction chamber 46 is rapidly cooled by reducing the pressure, and further chemical reaction is stopped. At this time, the oil in the hydraulic chamber 44 is returned to the oil tank 56 that is open to the atmosphere via the hydraulic pressure return path 48, and therefore, the surplus of the hydraulic cylinder type pressurized reactor 43 is used as the compression power of the superheated steam. Pressure (excess hydraulic pressure) cannot be recovered.
  • the post-reaction slurry is supplied to the flash tank 51 via the post-reaction slurry transfer path 50.
  • the flash steam generated in the flash tank 51 is exhausted from the flash steam exhaust path 52 and drained as condensed water by the heat exchanger 53.
  • the drained condensed water can be reused as a soft water source for the steam generator, but in this case, the latent heat of the flash steam cannot be recovered.
  • the cooled post-reaction slurry is taken out from the saccharified solution path 54 to the outside of the flash tank 51 by the pump 55.
  • the method for decomposing cellulosic biomass of the present invention improves the thermal efficiency by recovering latent heat by circulating flash steam while recovering excess pressure when reducing the pressure of the reactor and reducing compression power. Can be achieved. Furthermore, the cellulosic biomass decomposition method of the present invention uses the surplus pressure at the time of depressurizing the reactor as the compression power of the steam compressor in the form of hydraulic pressure, so that the invention disclosed in Patent Document 4 or 5 is used. Unlike the above, the degree of freedom regarding the operation timing of the reactor and the vapor compressor is large, and it is possible to link the two at the optimal timing.
  • the cellulosic biomass decomposition method and decomposition apparatus of the present invention are useful in the bioenergy field as a method and apparatus for decomposing cellulosic biomass and producing saccharides.

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Abstract

L'objectif de la présente invention est de réduire la puissance de compression en récupérant le surplus de pression lors de la réduction de la pression du réacteur, et d'améliorer le rendement thermique en récupérant la chaleur latente par l'intermédiaire d'une utilisation cyclique de la vapeur de revaporisation dans un procédé et un dispositif de décomposition de biomasse cellulosique dans un état supercritique ou sous-critique. Pour amener une biomasse cellulosique dans un état supercritique ou sous-critique, ce procédé et ce dispositif de saccharification/décomposition impliquent le fonctionnement à la fois d'un réacteur de mise sous pression de type vérin hydraulique, utilisé en tant que réacteur, et d'un compresseur de vapeur de type vérin hydraulique, utilisé en tant que source d'alimentation en vapeur surchauffée. Lorsque la décomposition de la biomasse cellulosique est terminée, le surplus de pression hydraulique est récupéré en tant que puissance de compression pour le compresseur de vapeur de type vérin hydraulique, la vapeur de revaporisation produite à partir de la bouillie contenant les substances décomposées est fournie au compresseur de vapeur de type vérin hydraulique, et cette vapeur est utilisée de façon cyclique.
PCT/JP2011/005420 2010-09-30 2011-09-27 Procédé de saccharification/décomposition de la biomasse cellulosique et appareil de saccharification/décomposition Ceased WO2012042841A1 (fr)

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US13/813,583 US20130125877A1 (en) 2010-09-30 2011-09-27 Method and apparatus of hydrolytic saccharification of cellulosic biomass
JP2012504967A JPWO2012042841A1 (ja) 2010-09-30 2011-09-27 セルロース系バイオマスの糖化分解方法及び糖化分解装置

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Cited By (3)

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JP5696310B1 (ja) * 2014-07-15 2015-04-08 国立大学法人東北大学 汚泥の栄養分回収方法、藻類の培養方法、および藻類培養システム
US9328963B2 (en) 2013-07-10 2016-05-03 Renmatix, Inc. Energy recovery when processing materials with reactive fluids
WO2021210216A1 (fr) * 2020-04-17 2021-10-21 日本有機物リサイクルプラント株式会社 Dispositif de traitement de l'eau sous-critique

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CN112501360B (zh) * 2021-01-04 2025-04-25 云南师范大学 一种用于纤维素原料水解糖化的压滤式稀酸水解反应器

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