WO2012042841A1 - Method for saccharifying/breaking down cellulosic biomass and saccharification/breakdown apparatus - Google Patents
Method for saccharifying/breaking down cellulosic biomass and saccharification/breakdown apparatus Download PDFInfo
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- 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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- 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
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- 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
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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
- 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
Description
セルロース系バイオマスのスラリーを過熱水蒸気と共に油圧シリンダ型加圧式反応器内で超臨界状態又は亜臨界状態となるまで加圧することにより、セルロース系バイオマスの糖化分解を行うセルロース系バイオマスの糖化分解方法であって、
前記油圧シリンダ型加圧式反応器への過熱水蒸気供給を、油圧シリンダ型蒸気圧縮機によって行い、
前記油圧シリンダ型加圧式反応器の油圧返送経路と前記油圧シリンダ型蒸気圧縮機の油圧室とを油圧回収経路で接続することにより、セルロース系バイオマスの糖化分解後、前記油圧シリンダ型加圧式反応器内を超臨界状態又は亜臨界状態以下に減圧する際に、前記油圧シリンダ型加圧式反応器の油圧室の油圧を前記油圧シリンダ型蒸気圧縮機の油圧室へと回収し、
糖化分解後のスラリーをフラッシュタンク内へと供給した後にフラッシュ蒸発させ、フラッシュ蒸気を前記油圧シリンダ型蒸気圧縮機へと回収する、
ことを特徴とする方法に関する。 Specifically, the present invention
This 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. And
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.
セルロース系バイオマスのスラリーを過熱水蒸気と共に超臨界状態又は亜臨界状態となるまで加圧する油圧シリンダ型加圧式反応器と、
前記油圧シリンダ型加圧式反応器に過熱水蒸気を供給する油圧シリンダ型蒸気圧縮機と、
前記複数の油圧シリンダ型加圧式反応器から取り出した高温高圧のスラリーを供給してフラッシュ蒸発させるフラッシュタンクとを有し、
前記油圧シリンダ型加圧式反応器の油圧返送経路と前記油圧シリンダ型蒸気圧縮機の油圧室とは、油圧回収経路によって接続されており、前記油圧シリンダ型加圧式反応器の油圧室の油圧は、前記油圧回収経路によって前記油圧シリンダ型蒸気圧縮機の油圧室へと回収され、
前記フラッシュタンクは、前記油圧シリンダ型蒸気圧縮機と接続されており、高温高圧のスラリーから発生したフラッシュ蒸気を前記油圧シリンダ型蒸気圧縮機へと回収することを特徴とする装置に関する。 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.
1台の前記油圧シリンダ型加圧式反応器の油圧返送経路と1台の前記油圧シリンダ型蒸気圧縮機の油圧室とを油圧回収経路で接続することにより、セルロース系バイオマスの糖化分解後、前記油圧シリンダ型加圧式反応器内を超臨界状態又は亜臨界状態以下に減圧する際に、1台の前記油圧シリンダ型加圧式反応器の油圧室の油圧を1台の前記油圧シリンダ型蒸気圧縮機の油圧室へと周期的に回収することが好ましい。 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.
それぞれの副経路には、蓄圧設定値が異なるエアチャンバーが1つずつ設けられており、
前記油圧シリンダ型加圧式反応器の油圧室の油圧を、高い蓄圧設定値のエアチャンバーから順に蓄圧した後、低い蓄圧設定値のエアチャンバーから順に油圧を開放し、前記油圧シリンダ型蒸気圧縮機の油圧室へと供給することが好ましい。 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.
図1は、本発明のセルロース系バイオマスの糖化分解方法を行うための処理装置の一例を示す概略構成図である。図1では、油圧シリンダ型加圧式反応器及び油圧シリンダ型蒸気圧縮機は、4台ずつ設置されているが、設置台数は4台ずつには限定されない。 (Embodiment 1)
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. In 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.
油圧シリンダ型蒸気圧縮機5a~5dはすべて同様に動作し、油圧シリンダ型加圧式反応器1a~1dもすべて同様に動作する。そこで、本発明のセルロース系バイオマスの分解方法における油圧シリンダ型蒸気圧縮機5a及び油圧シリンダ型加圧式反応器1aの組み合わせにおける油圧回収について、図2に基づいて説明する。 <1. Recovery of hydraulic pressure>
The hydraulic cylinder
水蒸気は、蒸気供給経路14aを経て、油圧シリンダ型蒸気圧縮機5aの蒸気圧縮室8aに供給される。油圧室6aの容積は最も小さくなり、油圧室6a内の油圧は、油圧返送経路19a及び19を経て、油タンク26へと返送される。このとき、油圧シリンダ型加圧式反応器1aは、セルロース系バイオマスのスラリー及び過熱水蒸気が供給された反応室4aを圧縮し、超臨界状態又は亜臨界状態としてセルロース系バイオマスを分解している。水蒸気は、油圧シリンダ型蒸気圧縮機5aによって圧縮された後、さらに反応室4aで圧縮されるので、最も温度及び圧力が高い状態となっている。セルロース系バイオマスを分解する際には、反応室4a内を350~400℃、18~30MPaとすることが好ましい。分解時間は、0.1~30秒間とすることが好ましく、0.1~3秒間とすることがより好ましい。 (Explanation of Fig. 2 (a))
The steam is supplied to the
油圧シリンダ型加圧式反応器1aは、セルロース系バイオマスの分解反応終了後、反応室内4a内を減圧することによって急冷し、さらなる化学反応を停止させる。このとき、油圧シリンダ型加圧式反応器1aの油圧室2aの油圧が上昇するため、油圧回収経路9aを経て、油圧室2aの油圧を油圧シリンダ型蒸気圧縮機5aの油圧室6aへと回収し、蒸気圧縮室8a内の水蒸気を圧縮する。回収された油圧によって、図2(a)のときに蒸気圧縮室8aに供給された水蒸気を圧縮するための動力を削減することができる。 (Explanation of Fig. 2 (b))
The hydraulic cylinder type
蒸気圧縮室8a内の水蒸気は、さらに高温高圧(250~300℃、3.9~8.5MPa)の過熱水蒸気となるまで圧縮される。このとき、亜臨界状態以下の温度及び圧力に減圧された糖生成後のスラリーは、油圧シリンダ型加圧式反応器1aから反応後スラリー移送経路20aへと排出される。排出直前の反応後スラリーは、150~300℃、0.5~8.6MPaとすることが好ましい。一方、セルロース系バイオマスのスラリーは、スラリー供給経路11aからスラリー投入室27へと充填される。 (Explanation of Fig. 2 (c))
The steam in the
蒸気圧縮室8aから排出された高温高圧の過熱水蒸気は、高圧蒸気供給経路10aを経て、油圧シリンダ型加圧式反応器1aの反応室4aへと供給される。このとき、スラリー投入室27内のセルロース系バイオマスのスラリーも、油圧シリンダ型加圧式反応器1aの反応室4aへと同時に供給される。一方、油圧シリンダ型加圧式反応器1aの油圧室2a内の油圧は、油圧返送経路17a及び17を経て、油タンク26へと返送される。 (Explanation of Fig. 2 (d))
The high-temperature and high-pressure superheated steam discharged from the
次に、反応後スラリーからのフラッシュ蒸気の回収について説明する。図2(c)のときに反応後スラリー移送経路20aへと排出された反応後スラリーは、反応後スラリー移送経路20を経て、フラッシュタンク13へと移送される。フラッシュタンク13内でフラッシュ蒸発させることにより、反応後スラリーは0.1~1.6MPa程度の圧力となる。その後、反応後スラリーは、フラッシュタンク13の底部からポンプ22によって、装置外の貯液設備又は発酵装置へと移送される。 <2. Flash steam recovery>
Next, the collection | recovery of the flash vapor | steam from the slurry after reaction is demonstrated. The post-reaction slurry discharged to the post-reaction
図3は、本発明のセルロース系バイオマスの糖化分解方法を行うための処理装置の別の一例のうち、油圧シリンダ型蒸気圧縮機5a及び油圧シリンダ型加圧式反応器1aの接続状態を示す概略構成図である。この処理装置は、油圧シリンダ型蒸気圧縮機5a及び油圧シリンダ型加圧式反応器1a間の油圧回収用の経路が異なること以外は、すべて図1に示される処理装置と同じである。この処理装置では、油圧返送経路17aに油圧回収経路32が接続しており、油圧回収経路32は32a~32dの4つの副経路に分岐している。副経路32a~32dには、それぞれ油圧用バルブセット33a~33dが設けられている。 (Embodiment 2)
FIG. 3 is a schematic configuration showing a connection state of a hydraulic cylinder
図4は、セルロース系バイオマスの糖化分解方法を行うための従来の処理装置の一例を示す概略構成図である。この処理装置は、セルロース系バイオマスのスラリーと過熱水蒸気とを油圧シリンダ型加圧式反応器によって圧縮することにより、超臨界状態又は亜臨界状態としてセルロース系バイオマスを分解する点において、本発明のセルロース系バイオマスの糖化分解方法と共通する。しかし、この処理装置は、ボイラのような蒸気発生装置(図示せず)から供給された過熱水蒸気を、蒸気圧縮機によって再圧縮した後、油圧シリンダ型加圧式反応器に供給する構成とはなっていない。反応後スラリーからのフラッシュ蒸気の回収する構成ともなっていない。 (Conventional technology)
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. Common to biomass saccharification and decomposition methods. However, this processing apparatus has a configuration in which superheated steam supplied from a steam generator (not shown) such as a boiler is recompressed by a steam compressor and then supplied to a hydraulic cylinder type pressurized reactor. Not. It is not configured to collect flash vapor from the slurry after the reaction.
2a~2d:油圧室
3a~3d:油圧シリンダ
4a~4d:反応室
5a~5d:油圧シリンダ型蒸気圧縮機
6a~6d:油圧室
7a~7d:油圧シリンダ
8a~8d:蒸気圧縮室
9a~9d:油圧回収経路
10a~10d:高圧蒸気供給経路
11,11a~11d:スラリー供給経路
12:蒸気供給経路
13:フラッシュタンク
14,14a~14d:蒸気供給経路
15,15a~15d:油圧経路
16,16a~16d:油圧経路
17,17a~17d:油圧返送経路
18,18a~18d:油圧経路
19,19a~19d:油圧返送経路
20,20a~20d:反応後スラリー移送経路
21:糖化液経路
22:ポンプ
23,24,25:油圧ポンプ
26:油タンク
27:スラリー投入室
28,28a,28b:配管
31,34,38:弁
32:油圧回収経路
32a~32d:油圧回収経路(副経路)
33a~33d:油圧用バルブセット
35a~35d:エアチャンバー経路
36:油圧回収経路
36a~36d:油圧供給経路(副経路)
37a~37d:油圧用バルブセット
41:スラリー供給経路
42:高圧蒸気供給経路
43:油圧シリンダ型加圧式反応器
44:油圧室
45:油圧シリンダ
46:反応室
47:油圧経路
48:油圧返送経路
49:油圧ポンプ
50:反応後スラリー移送経路
51:フラッシュタンク
52:フラッシュ蒸気排気経路
53:熱交換器
54:糖化液経路
55:ポンプ
P1~P4:エアチャンバー DESCRIPTION OF
33a to 33d: Hydraulic valve set 35a to 35d: Air chamber path 36: Hydraulic
37a to 37d: Hydraulic valve set 41: Slurry supply path 42: High pressure steam supply path 43: Hydraulic cylinder type pressurized reactor 44: Hydraulic chamber 45: Hydraulic cylinder 46: Reaction chamber 47: Hydraulic path 48: Hydraulic return path 49 : Hydraulic pump 50: Slurry transfer path after reaction 51: Flash tank 52: Flash steam exhaust path 53: Heat exchanger 54: Saccharification liquid path 55: Pumps P 1 to P 4 : Air chamber
Claims (10)
- セルロース系バイオマスのスラリーを過熱水蒸気と共に油圧シリンダ型加圧式反応器内で超臨界状態又は亜臨界状態となるまで加圧することにより、セルロース系バイオマスの糖化分解を行うセルロース系バイオマスの糖化分解方法であって、
前記油圧シリンダ型加圧式反応器への過熱水蒸気供給を、油圧シリンダ型蒸気圧縮機によって行い、
前記油圧シリンダ型加圧式反応器の油圧返送経路と前記油圧シリンダ型蒸気圧縮機の油圧室とを油圧回収経路で接続することにより、セルロース系バイオマスの糖化分解後、前記油圧シリンダ型加圧式反応器内を超臨界状態又は亜臨界状態以下に減圧する際に、前記油圧シリンダ型加圧式反応器の油圧室の油圧を前記油圧シリンダ型蒸気圧縮機の油圧室へと回収し、
糖化分解後のスラリーをフラッシュタンク内へと供給した後にフラッシュ蒸発させ、フラッシュ蒸気を前記油圧シリンダ型蒸気圧縮機へと回収する、
ことを特徴とする方法。 This 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. And
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.
A method characterized by that. - 前記油圧シリンダ型加圧式反応器及び前記油圧シリンダ型蒸気圧縮機が複数であり、 前記油圧シリンダ型加圧式反応器への過熱水蒸気供給を、同数の油圧シリンダ型蒸気圧縮機によって行い、
1台の前記油圧シリンダ型加圧式反応器の油圧返送経路と1台の前記油圧シリンダ型蒸気圧縮機の油圧室とを油圧回収経路で接続することにより、セルロース系バイオマスの糖化分解後、前記油圧シリンダ型加圧式反応器内を超臨界状態又は亜臨界状態以下に減圧する際に、1台の前記油圧シリンダ型加圧式反応器の油圧室の油圧を1台の前記油圧シリンダ型蒸気圧縮機の油圧室へと周期的に回収する、請求項1に記載のセルロース系バイオマスの糖化分解方法。 There are a plurality of the hydraulic cylinder type pressurized reactor and the hydraulic cylinder type steam compressor, and the 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. The saccharification / decomposition method for cellulosic biomass according to claim 1, wherein the saccharification / decomposition method is periodically collected into a hydraulic chamber. - 前記油圧回収経路は、前記油圧返送経路及び前記油圧シリンダ型蒸気圧縮機の油圧室との接続部分では1本の経路であり、それ以外の部分では複数の副経路に分岐しており、
それぞれの副経路には、蓄圧設定値が異なるエアチャンバーが1つずつ設けられており、
前記油圧シリンダ型加圧式反応器の油圧室の油圧を、高い蓄圧設定値のエアチャンバーから順に蓄圧した後、低い蓄圧設定値のエアチャンバーから順に油圧を開放し、前記油圧シリンダ型蒸気圧縮機の油圧室へと供給する、請求項1に記載のセルロース系バイオマスの糖化分解方法。 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 The method for saccharifying and decomposing cellulosic biomass according to claim 1, wherein the method is supplied to a hydraulic chamber. - 前記フラッシュタンクに水蒸気発生装置を接続し、前記水蒸気発生装置から供給された水蒸気とフラッシュ蒸気とを混合して前記油圧シリンダ型蒸気圧縮機へと水蒸気を供給する、請求項1に記載のセルロース系バイオマスの糖化分解方法。 The cellulosic system according to claim 1, wherein a steam generator is connected to the flash tank, the steam supplied from the steam generator and flash steam are mixed, and steam is supplied to the hydraulic cylinder type steam compressor. Biomass saccharification and decomposition method.
- 前記フラッシュタンク又は前記フラッシュタンクと前記油圧シリンダ型蒸気圧縮機とを接続する蒸気配管の少なくともいずれか一方に空気及び/又は窒素の供給装置を接続し、前記油圧シリンダ型蒸気圧縮機の蒸気圧縮室に供給する水蒸気に、蒸気量の1/7以上1/3以下の空気及び/又は窒素を混入させる、請求項1に記載のセルロース系バイオマスの糖化分解方法。 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. The method for saccharifying and decomposing cellulosic biomass according to claim 1, wherein air and / or nitrogen having a vapor amount of 1/7 or more and 1/3 or less of the amount of vapor is mixed into the water vapor supplied to.
- セルロース系バイオマスのスラリーを過熱水蒸気と共に超臨界状態又は亜臨界状態となるまで加圧する油圧シリンダ型加圧式反応器と、
前記油圧シリンダ型加圧式反応器に過熱水蒸気を供給する油圧シリンダ型蒸気圧縮機と、
前記複数の油圧シリンダ型加圧式反応器から取り出した高温高圧のスラリーを供給してフラッシュ蒸発させるフラッシュタンクとを有し、
前記油圧シリンダ型加圧式反応器の油圧返送経路と前記油圧シリンダ型蒸気圧縮機の油圧室とは、油圧回収経路によって接続されており、前記油圧シリンダ型加圧式反応器の油圧室の油圧は、前記油圧回収経路によって前記油圧シリンダ型蒸気圧縮機の油圧室へと回収され、
前記フラッシュタンクは、前記油圧シリンダ型蒸気圧縮機と接続されており、高温高圧のスラリーから発生したフラッシュ蒸気を前記油圧シリンダ型蒸気圧縮機へと回収することを特徴とする装置。 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 collects the flash steam generated from the high temperature and high pressure slurry to the hydraulic cylinder type steam compressor. - 前記油圧シリンダ型加圧式反応器及び前記油圧シリンダ型蒸気圧縮機が複数であり、
前記油圧シリンダ型加圧式反応器への過熱水蒸気供給を、同数の油圧シリンダ型蒸気圧縮機によって行い、
1台の前記油圧シリンダ型加圧式反応器の油圧返送経路と1台の前記油圧シリンダ型蒸気圧縮機の油圧室とは、油圧回収経路によって接続されており、1台の前記油圧シリンダ型加圧式反応器の油圧室の油圧は、前記油圧回収経路によって1台の前記油圧シリンダ型蒸気圧縮機の油圧室へと回収され、
前記フラッシュタンクは、複数の前記油圧シリンダ型蒸気圧縮機と接続されており、高温高圧のスラリーから発生したフラッシュ蒸気を複数の前記油圧シリンダ型蒸気圧縮機へと周期的に回収する、請求項6に記載のセルロース系バイオマスの糖化分解装置。 The hydraulic cylinder type pressurized reactor and the hydraulic cylinder type steam compressor are plural,
The superheated steam supply to the hydraulic cylinder type pressurized reactor is performed by the same number of hydraulic cylinder type steam compressors,
The hydraulic pressure return path of one hydraulic cylinder type pressurization reactor and the hydraulic chamber of one hydraulic cylinder type steam compressor are connected by a hydraulic pressure recovery path, and one hydraulic cylinder type pressurization type The hydraulic pressure of the hydraulic chamber of the reactor is recovered to the hydraulic chamber of one hydraulic cylinder type steam compressor by the hydraulic pressure recovery path,
The flash tank is connected to a plurality of the hydraulic cylinder type steam compressors, and periodically collects the flash steam generated from the high temperature and high pressure slurry into the plurality of hydraulic cylinder type steam compressors. A saccharification / decomposition device for cellulosic biomass as described in 1. - 前記油圧回収経路は、前記油圧返送経路及び前記油圧シリンダ型蒸気圧縮機の油圧室との接続部分では1本の経路であり、それ以外の部分では複数の副経路に分岐しており、
それぞれの副経路には、蓄圧設定値が異なるエアチャンバーが1つずつ設けられており、
前記油圧シリンダ型加圧式反応器の油圧室の油圧を、高い蓄圧設定値のエアチャンバーから順に蓄圧した後、低い蓄圧設定値のエアチャンバーから順に油圧を開放し、前記油圧シリンダ型蒸気圧縮機の油圧室へと供給する、請求項6に記載のセルロース系バイオマスの糖化分解装置。 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 The saccharification / decomposition apparatus for cellulosic biomass according to claim 6, which is supplied to a hydraulic chamber. - 前記フラッシュタンクに水蒸気発生装置を接続し、前記水蒸気発生装置から供給された水蒸気とフラッシュ蒸気とを混合して複数の前記油圧シリンダ型蒸気圧縮機へと水蒸気を供給する、請求項6に記載のセルロース系バイオマスの糖化分解装置。 The steam generator is connected to the flash tank, the steam supplied from the steam generator and flash steam are mixed, and steam is supplied to the plurality of hydraulic cylinder steam compressors. Cellulose biomass saccharification and decomposition equipment.
- 前記フラッシュタンク又は前記フラッシュタンクと複数の前記油圧シリンダ型蒸気圧縮機とを接続する蒸気配管の少なくともいずれか一方に空気及び/又は窒素の供給装置を接続し、前記油圧シリンダ型蒸気圧縮機の蒸気圧縮室に供給する水蒸気に、蒸気量の1/7以上1/3以下の空気及び/又は窒素を混入させる、請求項6に記載のセルロース系バイオマスの糖化分解装置。 An air and / or nitrogen supply device is connected to at least one of the flash tank or a steam pipe connecting the flash tank and the plurality of hydraulic cylinder steam compressors, and the steam of the hydraulic cylinder steam compressor is connected. The saccharification / decomposition apparatus for cellulosic biomass according to claim 6, wherein the steam supplied to the compression chamber is mixed with 1/7 or more and 1/3 or less of the amount of steam of air and / or nitrogen.
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JP2012504967A JPWO2012042841A1 (en) | 2010-09-30 | 2011-09-27 | Method and apparatus for saccharification and decomposition of cellulosic biomass |
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JP5696310B1 (en) * | 2014-07-15 | 2015-04-08 | 国立大学法人東北大学 | Sludge nutrient recovery method, algae culture method, and algae culture system |
US9328963B2 (en) | 2013-07-10 | 2016-05-03 | Renmatix, Inc. | Energy recovery when processing materials with reactive fluids |
WO2021210216A1 (en) * | 2020-04-17 | 2021-10-21 | 日本有機物リサイクルプラント株式会社 | Subcritical water treatment device |
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JP2000233127A (en) * | 1998-12-14 | 2000-08-29 | Hitachi Ltd | Organic matter treating system |
JP2002059118A (en) * | 2000-08-23 | 2002-02-26 | Nobuyuki Hayashi | Method of pressure hydrothermally decomposing plant based biomass and system therefor |
JP2002263465A (en) * | 2001-03-07 | 2002-09-17 | Saka Shiro | Reaction apparatus for organic material by supercritical water or subcritical water |
JP2003212888A (en) * | 2002-01-18 | 2003-07-30 | Asahi Kasei Corp | Method for producing glucose and/or water-soluble cellooligosaccharide |
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JPS5834116B2 (en) * | 1975-02-06 | 1983-07-25 | カブシキガイシヤ エバラセイサクシヨ | starch |
JPS6110009A (en) * | 1984-06-26 | 1986-01-17 | Kimura Kakoki Kk | Improvement of evaporation method of mechanical compression type |
JPS6211501A (en) * | 1985-07-06 | 1987-01-20 | Kimura Kakoki Kk | Heat recovering device for evaporator or the like |
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JP2000233127A (en) * | 1998-12-14 | 2000-08-29 | Hitachi Ltd | Organic matter treating system |
JP2002059118A (en) * | 2000-08-23 | 2002-02-26 | Nobuyuki Hayashi | Method of pressure hydrothermally decomposing plant based biomass and system therefor |
JP2002263465A (en) * | 2001-03-07 | 2002-09-17 | Saka Shiro | Reaction apparatus for organic material by supercritical water or subcritical water |
JP2003212888A (en) * | 2002-01-18 | 2003-07-30 | Asahi Kasei Corp | Method for producing glucose and/or water-soluble cellooligosaccharide |
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US9328963B2 (en) | 2013-07-10 | 2016-05-03 | Renmatix, Inc. | Energy recovery when processing materials with reactive fluids |
JP5696310B1 (en) * | 2014-07-15 | 2015-04-08 | 国立大学法人東北大学 | Sludge nutrient recovery method, algae culture method, and algae culture system |
WO2021210216A1 (en) * | 2020-04-17 | 2021-10-21 | 日本有機物リサイクルプラント株式会社 | Subcritical water treatment device |
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