WO2011087131A1 - 固体酸触媒糖化装置及び方法 - Google Patents
固体酸触媒糖化装置及び方法 Download PDFInfo
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- WO2011087131A1 WO2011087131A1 PCT/JP2011/050755 JP2011050755W WO2011087131A1 WO 2011087131 A1 WO2011087131 A1 WO 2011087131A1 JP 2011050755 W JP2011050755 W JP 2011050755W WO 2011087131 A1 WO2011087131 A1 WO 2011087131A1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
- B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
- B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms
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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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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F33/00—Other mixers; Mixing plants; Combinations of mixers
- B01F33/40—Mixers using gas or liquid agitation, e.g. with air supply tubes
- B01F33/406—Mixers using gas or liquid agitation, e.g. with air supply tubes in receptacles with gas supply only at the bottom
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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
- C13K13/00—Sugars not otherwise provided for in this class
- C13K13/002—Xylose
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
- B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
- B01J27/053—Sulfates
Definitions
- the present invention relates to a solid acid catalyzed saccharification apparatus and method.
- This application claims priority based on Japanese Patent Application No. 2010-8552 for which it applied to Japan on January 18, 2010, and uses the content here.
- Non-Patent Document 1 discloses a technique for saccharifying biomass by using a solid acid catalyst as an elemental technique in such a bioethanol production process.
- saccharification of biomass using a solid acid catalyst is a reaction in which a solid acid catalyst that is also solid acts on solid biomass to decompose the biomass into monosaccharides. That is, there is a problem that since the solid (solid acid catalyst) acts on the solid (biomass), the reaction rate is slow, and thus it is difficult to accurately grasp the reaction state in the reaction tank. In particular, when the solid acid catalyst is used alone, it is extremely difficult to accurately grasp the reaction state because the reaction rate is extremely slow. Therefore, when the biomass saccharification technology using a solid acid catalyst is adopted in the bioethanol production process, the reaction state of the biomass saccharification process cannot be accurately grasped, and thus the operation of the entire system cannot be accurately controlled.
- the present invention has been made in view of the above-described circumstances, and an object thereof is to accurately grasp the reaction state of a raw material saccharification process using a solid acid catalyst.
- the solid acid catalyzed saccharification apparatus accommodates the raw material polysaccharide together with water and the solid acid catalyst as a mixed solution, and monosaccharides the polysaccharide using the solid acid catalyst.
- Catalyst reaction tank, stirring device for stirring the liquid mixture in the catalyst reaction tank, redox potential meter for measuring the redox potential of the liquid mixture in the catalyst reaction tank, and pH meter for measuring the pH of the liquid mixture in the catalyst reaction tank It comprises.
- a catalyst separation tank for separating the solid acid catalyst from the treated liquid received from the catalyst reaction tank, and a catalyst return for supplying the solid acid catalyst discharged from the catalyst separation tank to the catalyst reaction tank
- a second oxidation-reduction potentiometer for measuring the oxidation-reduction potential of the liquid obtained by separating the solid acid catalyst from the treated liquid in the catalyst separation tank, and the liquid obtained by separating the solid acid catalyst from the treated liquid in the catalyst separation tank It is desirable to include a second pH meter that measures pH.
- the stirring apparatus may stir the treatment target liquid by rotating a paddle immersed in the mixed liquid.
- the stirring apparatus may stir the treatment target liquid by blowing a gas into the mixed liquid.
- the solid acid catalyst saccharification method according to the present invention includes a liquid to be treated and a solid acid catalyst when the polysaccharide is mono-saccharified by causing a solid acid catalyst to act on the liquid to be treated consisting of water and a raw material polysaccharide.
- the redox potential and pH of the mixed solution are measured, and the monosaccharification state is evaluated based on the redox potential and pH.
- the oxidation-reduction potential and pH of the liquid obtained by separating the solid acid catalyst from the treated liquid are measured, and the state of the solid acid catalyst is evaluated based on the oxidation-reduction potential and pH. Good.
- the oxidation-reduction potential and pH of the liquid to be treated are measured. Therefore, the state of monosaccharification treatment is determined by the measured values of the oxidation-reduction potential and pH. Can be evaluated. That is, according to the knowledge of the present inventors, there is a difference in oxidation-reduction potential between a reaction in which the polysaccharide is monosaccharided and a state in which the reaction is favorable. Moreover, pH has shown the active state of the solid acid catalyst. Therefore, by measuring the pH of the treatment target liquid in addition to the oxidation-reduction potential of the treatment target liquid, it is possible to accurately grasp the state of the monosaccharide saccharification reaction of the polysaccharide when using the solid acid catalyst.
- the solid acid catalyst saccharification apparatus A includes a raw water supply pump 1, a flow meter 2, a catalytic reaction tank 3, a stirring device 4, a redox potentiometer 5, a pH meter 6, and catalyst separation.
- the gas blower 16 and the on-off valves 17 to 19 are used.
- the present solid acid-catalyzed saccharification apparatus A is an apparatus that saccharifies a raw material (polysaccharide) supplied from the outside.
- a solid acid-catalyzed saccharification apparatus A is, for example, a plant that produces bioethanol from biomass (biological resources excluding fossil resources), and that is a latter stage that incorporates polysaccharides obtained from biomass by a first-stage saccharification apparatus.
- the pre-stage saccharification apparatus for example, a hot water flow saccharification apparatus that saccharifies biomass by allowing hot water of a predetermined temperature to flow through the granular biomass charged in the tubular reactor for a predetermined time can be considered.
- the present applicant adjusts the hot water temperature in the pressurized hot water reactor (pre-stage saccharification device) in Japanese Patent Application No. 2009-219362 (filed on Sep. 24, 2009, title of invention: biomass processing apparatus and method).
- xylooligosaccharide and cellooligosaccharide are individually obtained from the polysaccharide (carbohydrate) contained in biomass (woody biomass), and xylose (C 5 H 10 O 5 : pentose sugar) and by treating cellooligosaccharide with a second catalytic reactor (second stage saccharification equipment) and glucose (C 6 H 12 O 6 : hexose sugar) saccharified, with further fermentation xylose in the first fermenter, bioethanol by fermentation of glucose in the second fermentor (C 2 H O) proposes a biomass processing apparatus and method for manufacturing the.
- woody biomass is mainly composed of cellulose (polysaccharide), hemicellulose (polysaccharide) and lignin.
- Decomposing cellulose and hemicellulose into polysaccharides xylooligosaccharides, cellooligosaccharides, and various oligosaccharides with a slightly higher degree of polymerization) by applying hot water to the woody biomass of such components Can do.
- the present solid acid catalyzed saccharification apparatus A has the same basic functions as the first and second catalytic reaction apparatuses described above, and converts the granular polysaccharide mixed with water from the previous saccharification apparatus (hot water flow saccharification apparatus) into raw water. It is taken in as X1 (treatment target liquid), and the raw material is monosaccharided into, for example, xylose or glucose.
- the raw water supply pump 1 in the present solid acid catalytic saccharification apparatus A continuously supplies the raw water X1 to the catalytic reaction tank 3 sequentially at a predetermined flow rate.
- the flow meter 2 is provided in the middle of the pipe connecting the raw water supply pump 1 and the catalyst reaction tank 3, and measures the supply flow rate of the raw water X1.
- the raw acid X1 is allowed to act on the solid acid catalyst X2 to monosaccharideize the polysaccharide.
- the catalyst reaction tank 3 is a cylindrical container that accommodates a predetermined volume of raw water X1, and is provided in a posture in which the central axis is in the vertical direction.
- the bottom of the catalyst reaction tank 3 is provided with a catalyst take-in part 3a for taking up the granular solid acid catalyst X2, and the exhaust periphery 3b for discharging the treated liquid X4 is provided at the upper periphery of the catalyst reaction tank 3. ing. That is, the liquid stored in the catalytic reaction tank 3 is a mixed liquid X3 in which the raw water X1 is mixed with the granular solid acid catalyst X2.
- the stirring device 4 is fixed to a rotating shaft in a vertical posture and is rotated at a predetermined speed by a motor by rotating a paddle (stirring blade) immersed in the mixed solution X3 of the catalytic reaction tank 3 to thereby form a catalyst.
- the mixed solution X3 in the reaction vessel 3 is stirred.
- the paddle in the stirrer 4 is provided in two upper and lower stages with respect to the rotating shaft as shown in the figure in order to uniformly mix the mixed solution X3 in the cylindrical catalyst reaction tank 3 without being biased in the vertical position. If the upper and lower heights increase, three or more stages are preferable.
- the oxidation-reduction potential meter 5 measures the oxidation-reduction potential of the mixed solution X3 in the catalytic reaction tank 3.
- the pH meter 6 measures the pH of the mixed solution X3 in the catalyst reaction tank 3.
- the oxidation-reduction potential shows different values depending on the type of chemical reaction and the equilibrium state (progression state) of the chemical reaction.
- the active state of the solid acid catalyst X2 as a catalyst appears as the pH (hydrogen ion index) of the mixed solution X3.
- the present inventors have found that the reaction in which the polysaccharide in the mixed solution X3 in the catalytic reaction tank 3 is monosaccharided causes a difference between the oxidation-reduction potential and the pH depending on whether the reaction is good or not. . That is, the oxidation-reduction potentiometer 5 and the pH meter 6 decompose the polysaccharide into the monosaccharide in the catalytic reaction tank 3, that is, the decomposition reaction that monosaccharides the polysaccharide in the mixed solution X3 using the solid acid catalyst X2. This is a characteristic component in the present solid acid catalyst saccharification apparatus A for grasping the state.
- the measured value of the pH meter 6 can be effectively used to accurately evaluate the measured value of the redox potential meter 5. Is done.
- the state of the decomposition reaction based on the measured value of the oxidation-reduction potentiometer 5 and the measured value of the pH meter 6 uses an information processing device (computer) equipped with a dedicated evaluation program. This can be done automatically and objectively.
- the catalyst separation tank 7 is a precipitation tank for separating the solid acid catalyst X2 from the treated liquid X4 received from the catalyst reaction tank 3.
- the catalyst separation tank 7 is a cylindrical container that stores a predetermined volume of the treated liquid X4, and is provided with a posture in which the central axis is in the vertical direction.
- a cylindrical member 7a for receiving the treated liquid X4 is provided in the vertical center in the upper center of the catalyst separation tank 7, and a precipitated granular solid acid catalyst X2 is provided at the bottom of the catalyst separation tank 7. Is provided with a catalyst outlet 7b.
- a treated water discharge port 7c for discharging the liquid obtained by separating the solid acid catalyst X2 from the treated liquid X4 to the outside as treated water X5 is provided at the upper peripheral edge of the catalyst separation tank 7.
- the catalyst return device 8 is a screw conveyor as shown in the figure, and supplies the solid acid catalyst X2 discharged from the catalyst discharge port 7b to the catalyst take-in portion 3a.
- the second oxidation-reduction potentiometer 9 measures the oxidation-reduction potential of the supernatant in the catalyst separation tank 7, that is, the treated water X5.
- the second pH meter 10 measures the pH of the supernatant liquid in the catalyst separation tank 7, that is, the treated water X5.
- the second oxidation-reduction potentiometer 9 and the second pH meter 10 are for evaluating the properties of the treated water X5 and the active state of the solid acid catalyst X2.
- the properties of the treated water X5 and the active state of the solid acid catalyst X2 based on the measured value of the second oxidation-reduction potentiometer 9 and the measured value of the second pH meter 10 are not shown, but are not shown. It is conceivable to perform this automatically and objectively by using an information processing apparatus (computer) equipped with the evaluation program.
- the catalyst recovery pump 11 dispenses a part of the mixed solution X 3 from the catalyst reaction tank 3 and supplies it to the catalyst recovery tank 12.
- the catalyst recovery tank 12 is a container for temporarily storing the mixed solution X3 supplied from the catalyst recovery pump 11, and separates the solid acid catalyst X2 from the mixed solution X3 and discharges it from the bottom.
- the liquid return pump 13 returns the liquid obtained by separating the solid acid catalyst X2 from the mixed liquid X3 (raw water X1 is treated to some extent by the solid acid catalyst X2) from the catalyst recovery tank 12 to the catalyst reaction tank 3.
- the float switch 14 is a mechanical switch that operates according to the draft of the catalyst recovery tank 12, and turns on / off the operation of the catalyst recovery pump 11. That is, the float switch 14 is turned on to operate the catalyst recovery pump 11 when the draft of the catalyst recovery tank 12 becomes a predetermined value or less.
- the catalyst discharge valve 15 is an on-off valve provided in a pipe communicating with the bottom of the catalyst recovery tank 12, and turns ON / OFF the discharge of the solid acid catalyst X2 from the catalyst recovery tank 12 to the outside.
- the blockage prevention gas blower 16 is supplied with compressed air for preventing blockage by the solid acid catalyst X2 in the pipes communicating with the bottoms of the catalyst take-in portion 3a, the catalyst return device 8 and the catalyst recovery tank 12. It is a pump to supply.
- the on-off valve 17 is provided between the blockage-preventing gas blower 16 and the catalyst intake 3a, the on-off valve 18 is provided between the blockage-preventing gas blower 16 and the catalyst return device 8, and the on-off valve 19 is Further, it is provided between a pipe communicating with the bottom of the catalyst recovery tank 12 and a gas blower 16 for blocking prevention.
- raw water X1 is sequentially and continuously supplied to the catalytic reaction tank 3 by the raw water supply pump 1 at a predetermined flow rate.
- the raw water X1 stays in the catalyst reaction tank 3 for a certain period of time as a mixed state with the solid acid catalyst X2, that is, as a mixed solution X3.
- the granular polysaccharide contained in the raw water X1 is saccharified by the catalytic action of the solid acid catalyst X2 during the residence in the catalytic reaction tank 3.
- the treated liquid X4 after saccharification is discharged as a supernatant from a discharge port 3b provided at the upper peripheral edge of the catalyst reaction tank 3, and is supplied into the cylindrical member 7a of the catalyst separation tank 7.
- the progress state of the decomposition reaction of polysaccharides into monosaccharides in the catalytic reaction tank 3 is monitored by the oxidation-reduction potentiometer 5 and the pH meter 6. That is, the oxidation-reduction potential value that is the measurement result of the oxidation-reduction potentiometer 5 indicates the progress state of the decomposition reaction, and the pH value that is the measurement result of the pH meter 6 is the hydrogen ion concentration corresponding to the decomposition reaction. Show.
- the cellooligosaccharide contained in the raw water X1 is mainly composed of cellooligosaccharide
- the cellooligosaccharide is decomposed into glucose by the catalytic action of the solid acid catalyst X2 in the catalytic reaction tank 3, but this decomposition reaction proceeds normally.
- the redox potential value is smaller than ⁇ 1100 (mV (vs.sSHE).
- the mixed solution X3 in the catalyst reaction tank 3 has a pH value smaller than 4.0, the solid acid catalyst X2 exhibits a sufficient catalytic action as an acid.
- the measured value output from the oxidation-reduction potentiometer 5 is smaller than ⁇ 1100 (mV vs. SHE) and the measured value output from the pH meter 6 shows a value smaller than 4.0, It can be evaluated that the decomposition reaction is proceeding smoothly in the catalytic reaction tank 3.
- the measured value output from the oxidation-reduction potentiometer 5 is ⁇ 1100 (mV vs. SHE) or more and the measured value output from the pH meter 6 is 4.0 or more, It can be determined that the decomposition reaction is unsatisfactory for some reason.
- the treated liquid X4 is sequentially and continuously supplied from the catalyst reaction tank 3 into the cylindrical member 7a of the catalyst separation tank 7 as described above.
- the liquid from which the solid acid catalyst X2 has been separated from the treated liquid X4 that is, the supernatant liquid containing only monosaccharides, is discharged to the outside as the treated water X5 (product).
- the solid acid catalyst X2 recovered in the catalyst separation tank 7 is sequentially returned to the catalyst reaction tank 3 from the catalyst discharge port 7b by the catalyst return device 8.
- the activity of the solid acid catalyst X2 gradually decreases. Also in this case, since the oxidation / reduction potential of the supernatant liquid, that is, the treated water X5 in the catalyst separation tank 7 is measured by the second oxidation-reduction potentiometer 9, and the pH of the treated water X5 is measured by the second pH meter 10. The properties of the treated water X5 and the active state of the solid acid catalyst X2 can be accurately evaluated.
- the treated water X5 contains mainly glucose, but it can be said that such treated water X5 has good properties.
- the value is in a range smaller than ⁇ 900 (mV vs. SHE).
- the treated water X5 has a pH value lower than 5.0, it can be said that the solid acid catalyst X2 is in an active state sufficient as an acid.
- the catalyst recovery pump 11 When it is confirmed that the activity of the solid acid catalyst X2 has decreased to some extent based on the measurement value output from the second pH meter 10, the catalyst recovery pump 11 is activated and the solid acid catalyst X2 in the catalyst reaction tank 3 is activated. Recovery to the catalyst recovery tank 12 is started. When the catalyst recovery pump 11 is started in this manner, the mixed solution X3 is recovered from the catalyst reaction tank 3 based on the control by the float switch 14.
- the concentration of the solid acid catalyst X2 in the catalyst reaction tank 3 is reduced by the recovery of the solid acid catalyst X2 to the catalyst recovery tank 12, a new solid acid catalyst X2 is separately added to the catalyst reaction tank 3 to compensate for this. Additional supply.
- the solid acid catalyst X2 is separated, and the solid acid catalyst X2 is recovered to the outside through the catalyst discharge valve 15.
- the liquid from which the solid acid catalyst X 2 has been separated is returned to the catalytic reaction tank 3 by the liquid return pump 13.
- the pipe communicating with the bottom of the catalyst take-in part 3a, the catalyst return device 8 and the catalyst recovery tank 12 may be blocked because the granular solid acid catalyst X2 passes through, but is compressed from the gas blower 16 for blocking prevention. Since air is supplied, the blockage can be effectively prevented.
- the oxidation-reduction potential of the mixed solution X3 in the catalytic reaction tank 3 is measured by the oxidation-reduction potentiometer 5, and the pH of the mixed solution X3 is measured by the pH meter 6. It is possible to accurately evaluate the progress state of the decomposition reaction from the polysaccharide that proceeds in the catalytic reaction tank 3 to the monosaccharide.
- the liquid mixture X3 is fixed by rotating the paddle (stirring blade) fixed to the rotary shaft in the vertical posture and immersed in the liquid mixture X3 of the catalytic reaction tank 3 at a predetermined speed by a motor.
- the stirring device 4 for stirring is adopted, the configuration of the stirring device 4 is not limited to this.
- the stirring device 4 is not limited to this.
- an air diffuser 4a provided near the bottom in the catalytic reaction tank 3, a gas blower 4b that compresses and supplies gas to the air diffuser 4a
- the gas include air or carbon dioxide obtained by a fermentation reaction in the above-described fermentation apparatus.
- the effect of accelerating the decomposition reaction can be expected because oxygen in the air functions as an oxidizing agent that contributes to the decomposition reaction.
- the catalytic reaction tank 3 is provided with the oxidation-reduction potentiometer 5 and the pH meter 6, and the catalyst separation tank 7 is provided with the second oxidation-reduction potentiometer 9 and the second pH meter 10.
- the second oxidation-reduction potentiometer 9 and the second pH meter 10 may be omitted as necessary.
- the decomposition reaction and results in the catalytic reaction tank 3 based on the measured values of the oxidation-reduction potentiometer 5, the pH meter 6, the second oxidation-reduction potentiometer 9, and the second pH meter 10.
- the properties of the product and the activity of the solid acid catalyst X2 are evaluated, but some control is not performed using the results of the evaluation.
- the operation state of the solid acid catalyst saccharification apparatuses A and B may be changed by controlling controlled devices such as the raw water supply pump 1 based on the evaluation result as necessary.
- the feed rate of the raw water X1 to the catalytic reaction tank 3 is limited by reducing the number of revolutions of the raw water supply pump 1. It is conceivable to maintain the properties of the product in a desired state by increasing the residence time of the polysaccharide in the tank 3.
- A, B Solid acid catalytic saccharification device, 1 ... Raw water supply pump, 2 ... Flow meter, 3 ... Catalytic reaction tank, 4, 4A ... Stirrer, 5 ... Redox potential meter, 6 ... pH meter, 7 ... Catalyst separation Tank, 8 ... catalyst return device, 9 ... second oxidation-reduction potentiometer, 10 ... second pH meter, 11 ... catalyst recovery pump, 12 ... catalyst recovery tank, 13 ... liquid return pump, 14 ... float switch, 15 ... Catalyst discharge valve, 16 ... Gas blower for blocking prevention, 17 to 19 ... Open / close valve
Abstract
Description
本願は、2010年1月18日に日本に出願された特願2010-8552号に基づき優先権を主張し、その内容をここに援用する。
なお、非特許文献1の技術では、固体酸触媒と水熱反応とを組み合わせているが、固体酸触媒を単独で用いてバイオマスを糖化する技術が研究されている。
すなわち、本発明者らの知見によれば、多糖類が単糖化する反応について、反応が良好な状態と不調な状態とで酸化還元電位に差異が生じる。また、pHは固体酸触媒の活性状態を示している。
したがって、処理対象液の酸化還元電位に加えて、処理対象液のpHを計測することにより、固体酸触媒を用いる場合における多糖類の単糖化反応の状態を的確に把握することが可能である。
本実施形態に係る固体酸触媒糖化装置Aは、図1に示すように、原水供給ポンプ1、流量計2、触媒反応槽3、攪拌装置4、酸化還元電位計5、pH計6、触媒分離槽7、触媒返送装置8、第2の酸化還元電位計9、第2のpH計10、触媒回収ポンプ11、触媒回収槽12、液返送ポンプ13、フロートスイッチ14、触媒排出弁15、閉塞防止用ガスブロワ16、開閉弁17~19によって構成されている。
(1)上記実施形態では、鉛直姿勢の回転軸に固定されると共に触媒反応槽3の混合液X3に浸漬されたパドル(攪拌翼)を、モータによって所定速度で回転させることにより混合液X3を攪拌する攪拌装置4を採用したが、攪拌装置4の構成はこれに限定されない。
例えば、図2に示す固体酸触媒糖化装置Bのように、触媒反応槽3内の底部近傍に設けられた散気部材4aと、散気部材4aに気体を圧縮して供給するガスブロワ4bと、散気部材4aに供給される気体の流量を計測する流量計4cとから攪拌装置4Aを構成してもよい。上記気体としては、空気あるいは上述した発酵装置における発酵反応によって得られる二酸化炭素等が考えられる。なお、空気を用いた場合には、空気中の酸素が上記分解反応に寄与する酸化剤として機能することによって分解反応を促進させる効果が期待できる。
Claims (6)
- 原料である多糖類を水及び固体酸触媒と共に混合液として収容し、固体酸触媒を用いて多糖類を単糖化処理する触媒反応槽と、
触媒反応槽における混合液を攪拌する攪拌装置と、
触媒反応槽における混合液の酸化還元電位を計測する酸化還元電位計と、
触媒反応槽における混合液のpHを計測するpH計と
を具備する固体酸触媒糖化装置。 - 触媒反応槽から受け入れた処理済み液から固体酸触媒を分離する触媒分離槽と、
触媒分離槽から排出された固体酸触媒を触媒反応槽に供給する触媒返送装置と、
触媒分離槽において処理済み液から固体酸触媒を分離した液の酸化還元電位を計測する第2の酸化還元電位計と、
触媒分離槽において処理済み液から固体酸触媒を分離した液のpHを計測する第2のpH計と
を備える請求項1に記載の固体酸触媒糖化装置。 - 攪拌装置は、混合液内に浸漬されたパドルを回転させることにより処理対象液を攪拌する請求項1または2に記載の固体酸触媒糖化装置。
- 攪拌装置は、混合液内に気体を吹き込むことにより処理対象液を攪拌する請求項1または2に記載の固体酸触媒糖化装置。
- 水と原料である多糖類とからなる処理対象液に固体酸触媒を作用させて多糖類を単糖化処理する際に処理対象液と固体酸触媒との混合液の酸化還元電位とpHとを計測し、酸化還元電位及びpHに基づいて単糖化状態を評価する固体酸触媒糖化方法。
- 処理済み液から固体酸触媒を分離した液の酸化還元電位とpHとを計測し、酸化還元電位及びpHに基づいて固体酸触媒の状態を評価する請求項5に記載の固体酸触媒糖化方法。
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BRBR112012017587-4A BR112012017587A2 (pt) | 2010-01-18 | 2011-01-18 | Dispositivo e método de sacarificação catalisada por sólido-ácido |
US13/521,630 US20120279495A1 (en) | 2010-01-18 | 2011-01-18 | Solid-acid-catalyzed saccharification device and method |
CN2011800062017A CN102892905A (zh) | 2010-01-18 | 2011-01-18 | 固体酸催化剂糖化装置及方法 |
AU2011206011A AU2011206011A1 (en) | 2010-01-18 | 2011-01-18 | Solid-acid-catalyzed saccharification device and method |
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JP2010008552A JP2011142892A (ja) | 2010-01-18 | 2010-01-18 | 固体酸触媒糖化装置及び方法 |
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US (1) | US20120279495A1 (ja) |
JP (1) | JP2011142892A (ja) |
CN (1) | CN102892905A (ja) |
AU (1) | AU2011206011A1 (ja) |
BR (1) | BR112012017587A2 (ja) |
WO (1) | WO2011087131A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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WO2014007295A1 (ja) * | 2012-07-03 | 2014-01-09 | 昭和電工株式会社 | 植物性バイオマスの分解方法及びグルコースの製造方法 |
WO2015041178A1 (ja) * | 2013-09-18 | 2015-03-26 | フタムラ化学株式会社 | 合成樹脂バインダー成形固体酸及びその製造方法 |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
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CA2900759C (en) * | 2013-02-28 | 2017-08-29 | Mitsubishi Heavy Industries Mechatronics Systems, Ltd. | Biomass treatment system, saccharide solution producing process using biomass as raw material, and organic raw material producing process |
CN108839282B (zh) * | 2018-05-29 | 2020-10-27 | 安徽航睿电子科技有限公司 | 一种光催化塑料生物降解系统 |
CN112023852B (zh) * | 2019-06-03 | 2023-05-09 | 中国石油化工股份有限公司 | 一种苯部分加氢制备环己烯的生产装置 |
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JPS63164886A (ja) * | 1986-12-27 | 1988-07-08 | Hitachi Ltd | 耐熱性グルコアミラ−ゼの製造方法及び装置 |
JPH09297A (ja) * | 1995-06-22 | 1997-01-07 | Daicel Chem Ind Ltd | セルロース加水分解酵素の活性を測定する方法 |
WO2009004951A1 (ja) * | 2007-06-29 | 2009-01-08 | Nippon Oil Corporation | セルロースを含む材料の加水分解および酵素糖化による単糖類の製造方法 |
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ES2566672T3 (es) * | 2006-10-26 | 2016-04-14 | Kawasaki Jukogyo Kabushiki Kaisha | Método y sistema para sacarificación hidrolítica de una biomasa celulósica |
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2011
- 2011-01-18 US US13/521,630 patent/US20120279495A1/en not_active Abandoned
- 2011-01-18 WO PCT/JP2011/050755 patent/WO2011087131A1/ja active Application Filing
- 2011-01-18 CN CN2011800062017A patent/CN102892905A/zh active Pending
- 2011-01-18 BR BRBR112012017587-4A patent/BR112012017587A2/pt not_active IP Right Cessation
- 2011-01-18 AU AU2011206011A patent/AU2011206011A1/en not_active Abandoned
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Cited By (3)
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---|---|---|---|---|
WO2014007295A1 (ja) * | 2012-07-03 | 2014-01-09 | 昭和電工株式会社 | 植物性バイオマスの分解方法及びグルコースの製造方法 |
WO2015041178A1 (ja) * | 2013-09-18 | 2015-03-26 | フタムラ化学株式会社 | 合成樹脂バインダー成形固体酸及びその製造方法 |
JP2015083298A (ja) * | 2013-09-18 | 2015-04-30 | フタムラ化学株式会社 | 合成樹脂バインダー成形固体酸及びその製造方法 |
Also Published As
Publication number | Publication date |
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AU2011206011A1 (en) | 2012-08-09 |
CN102892905A (zh) | 2013-01-23 |
BR112012017587A2 (pt) | 2015-09-01 |
US20120279495A1 (en) | 2012-11-08 |
JP2011142892A (ja) | 2011-07-28 |
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