WO2013190874A1 - バイオマスの処理装置および処理方法 - Google Patents
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Definitions
- the present invention relates to a saccharification apparatus that hydrolyzes fiber such as cellulose, which is the main component of biomass, into saccharides by saccharification enzymes, and a biomass processing apparatus including a pretreatment apparatus that performs pretreatment of a saccharification reaction using saccharification enzymes, and It is related with the processing method of the used biomass.
- Biomass containing cellulose and hemicellulose such as bagasse, wheat straw, rice straw, palm residue, paper, etc.
- cellulose saccharification technology it can be used as a raw material for ethanol and organic acids. It is being pioneered.
- the main components such as cellulose and hemicellulose are pretreated such as acid treatment and hydrothermal treatment, and the pretreated biomass is sterilized and sterilized.
- a saccharification enzyme is reacted with the treated biomass to obtain a saccharified solution containing sugars such as glucose, xylose, arabinose, galactose, and mannose, and this sugar is converted to ethanol or the like by a fermentation method using a microorganism such as yeast.
- a method of simultaneously performing enzymatic saccharification and fermentation in the same tank on the pretreated and sterilized biomass is often used (simultaneous saccharification and fermentation).
- sterilization may be performed simultaneously with the pretreatment instead of sterilizing after the pretreatment. This sterilization treatment is performed in order to prevent contamination and reduce the production amount of sugar or fermentation product (when simultaneous saccharification and fermentation is performed) or generation of impurities.
- the increase in concentration of the sugar or fermentation product can be achieved by increasing the concentration of the raw material in the saccharification apparatus and preventing the occurrence of the contamination.
- a method for increasing the concentration of sugar or fermentation product there is a method in which a high concentration of pretreated biomass is supplied to a saccharification apparatus (for example, a bioreactor), and the high concentration of pretreated biomass is saccharified in the bioreactor. Since this high-concentration pretreated biomass is in a solid state, the bioreactor is extremely low in fluidity and requires a high-power agitation mechanism such as a rotating drum or a rotating blade (Patent Document 1). . However, there is a problem that the conversion efficiency for converting pretreated biomass into sugar cannot be increased because sufficient stirring cannot be achieved even with such a high power stirring mechanism.
- a belt conveyor, a flight conveyor, a screw conveyor, a bucket conveyor, or the like is used to convey the pretreatment biomass from the pretreatment apparatus to the bioreactor.
- pretreated biomass generally tends to adhere to solid material conveying means such as a conveyor, and this adhered material has a problem that it deteriorates cleaning properties and becomes a source of contamination.
- a plurality of bioreactors are usually used, a plurality of belt conveyors or the like that connect the pretreatment device and the bioreactor are also required, resulting in a problem that the construction cost increases.
- This fed-batch method is a method in which the biomass concentration in the bioreactor is operated so that sufficient flow can be obtained, and the biomass dissolved by saccharification is newly added as needed.
- this fed-batch method has a problem that contamination is likely to occur because solid high-concentration pretreated biomass is conveyed from the pretreatment device to the bioreactor using a conveyor or the like.
- a main object of the present invention is to provide a biomass processing apparatus and a processing method capable of suppressing the occurrence of contamination and increasing the concentration of the final product.
- a pretreatment device for pretreating biomass A slurrying device for slurrying the pretreated biomass;
- a biomass processing apparatus having a saccharification apparatus that saccharifies the slurried biomass with a saccharifying enzyme Provide a return line for returning a part of the internal liquid in the saccharification device to the slurrying device,
- a biomass processing apparatus characterized in that biomass pre-treated by a pre-processing apparatus and an internal liquid returned through a return line are mixed in a slurrying apparatus to make biomass slurry.
- the saccharification device is a simultaneous saccharification and fermentation device that simultaneously performs a step of saccharifying the slurried biomass with a saccharifying enzyme and a step of fermenting the saccharified product with a fermentation microorganism,
- the pretreated biomass By cooling the internal liquid passing through the return line with a cooler, the pretreated biomass can be sufficiently cooled using the returned internal liquid in the slurrying apparatus. As a result, the inactivation of saccharification enzymes and the inactivation of fermentation microorganisms are prevented when the internal liquid is charged into the slurrying device or when the slurried biomass is charged into the saccharification device or simultaneous saccharification and fermentation device. Can do.
- the return line or saccharification apparatus is provided with an internal liquid slurry concentration measuring means for measuring the slurry concentration of the internal liquid, and when the internal liquid slurry concentration is high, the return amount of the internal liquid is increased or supplied to the slurrying apparatus.
- a biomass slurry concentration measuring means for measuring the slurry concentration of the slurried biomass is provided in the supply line that supplies the biomass slurried by the slurrying device to the saccharification device. When the biomass slurry concentration is high, the internal liquid is returned.
- Pre-treating biomass with a pre-treatment device Slurrying the pretreated biomass with a slurrying device; In the method for treating biomass, the slurryed biomass is reacted with a saccharification enzyme in a saccharification apparatus to saccharify.
- a return line for returning a part of the internal liquid in the saccharification device to the slurrying device is provided,
- a biomass processing method comprising mixing biomass pretreated by a pretreatment device and an internal liquid returned through a return line in a slurrying device to make biomass slurry.
- Pre-treating biomass with a pre-treatment device Slurrying the pretreated biomass with a slurrying device; In the simultaneous saccharification and fermentation apparatus, the slurry that has been slurried is reacted with a saccharification enzyme to saccharify, and at the same time, the saccharification product is reacted with a fermentation microorganism and fermented.
- a return line for returning a part of the internal liquid in the simultaneous saccharification and fermentation apparatus to the slurrying apparatus is provided, A biomass processing method characterized by mixing biomass pretreated by a pretreatment device and an internal liquid returned through a return line in a slurrying device to slurry biomass.
- biomass treatment process 1 and 2 show an outline of a biomass processing operation flow.
- the apparatus concerning this invention can be used suitably about biomass containing cellulose, hemicellulose, such as bagasse, straw, palm residue, corn stover, palm palm residue, cassava residue, a piece of wood, wood waste, jute, kenaf, and used paper.
- Biomass containing cellulose and hemicellulose is separated from foreign substances such as sand and pebbles using water in the washing process, and much of the water added in the washing process is removed by the dehydration process.
- the same effect can be obtained by a method of separating foreign matter without using water, such as specific gravity difference separation by an airflow cyclone.
- the biomass is mainly a complex in which three components of cellulose, hemicellulose, and lignin are tightly bound, and the cellulose molecule itself has a hard crystal structure, so that the saccharifying enzyme cellulase cannot approach the cellulose molecule as it is. . Therefore, in the pretreatment device, the dehydrated biomass is pretreated with any one of heat treatment, hydrothermal treatment, acid treatment, alkali method, fine pulverization method, wood decay fungus, etc. to loosen the binding of the three components. There is a need. Thereby, saccharification enzyme cellulase becomes easy to contact a cellulose molecule and enzyme saccharification is accelerated
- sterilization is usually performed to prevent contamination, but heat treatment, hydrothermal treatment (steaming, explosion), acid treatment (diluted acid method using sulfuric acid, nitric acid, phosphoric acid, concentrated acid method, SO2 impregnation explosion method) ) And alkali treatment (caustic soda method, sodium sulfite method, ammonia method, calcium hydroxide method), since the pretreatment has a sterilization effect, there is no need to provide a separate sterilization step. There is an advantage of being good.
- the pre-processed biomass is transported to a saccharification apparatus using a transporting means such as a conveyor, contamination may occur as described above. Therefore, in the present invention, the pre-processed biomass is slurried. Specifically, the pretreated biomass is conveyed to a slurrying apparatus and mixed with the liquid in the apparatus, and slurried so that the pretreated biomass is about 5% or less.
- the slurrying apparatus may be a stirring tank or a static mixer, and may simply be a joining area of a pipe through which pretreated biomass passes and a pipe through which the internal return liquid passes.
- the slurrying apparatus and the saccharification apparatus are connected by a transport pipe, and this is used as a supply line.
- the slurried biomass is pumped to the saccharification apparatus through this transport pipe and used for the saccharification process.
- a pressure difference may be generated between the slurrying apparatus and the saccharification apparatus, and transport may be performed using this pressure difference. In this way, by transporting the slurry by piping without using a conveyor or the like, cleaning becomes easy and the possibility of contamination is reduced.
- the slurried biomass is saccharified in a saccharification apparatus.
- a typical example of this saccharification apparatus is a bioreactor.
- the slurry biomass is decomposed mainly by the action of three types of cellulases (endoglucanase (EG), cellobiohydrolase (CBH), and ⁇ -glucosidase (BGL)).
- This cellulase is added in an amount of 3 to 30 FPU / g, preferably 5 to 20 FPU / g, based on the dry weight of the raw material (FPU / g is a unit of cellulase enzyme activity that produces 10.8 mg of glucose from filter paper in 60 minutes).
- the saccharification apparatus in this invention includes the simultaneous saccharification and fermentation apparatus mentioned later.
- the saccharified raw material is further processed into an organic fuel such as ethanol or an organic acid by yeast or bacteria.
- an organic fuel such as ethanol or an organic acid by yeast or bacteria.
- it is common to acquire ethanol as a biofuel by fermentation and distillation.
- Saccharomyces, Schizosaccharomyces, Kluyveromyces, Pichia, Candida yeast, Zymomonas spp., Clostridium spp. Use genetically modified microorganisms.
- this ethanol-fermenting bacterium is inoculated with 1 to 100 g wet-wt / L, preferably 5 to 50 g wet-wt / L per raw material volume.
- filamentous fungi such as Rhizopus oryzae can be used, and in order to convert sugar to succinic acid, for example, Coryneform bacteria (Coryneform bacteria) ), Bacillus bacteria, Rhizobium bacteria, and the like.
- the present invention is characterized in that the internal liquid in the saccharification apparatus is returned to the slurrying apparatus.
- the concentration of the sugar produced in the saccharification apparatus cannot be sufficiently increased.
- a liquid containing sugar such as an internal liquid in the saccharification apparatus, instead of the liquid not containing sugar, sugar is also contained in the liquid for slurrying. The sugar concentration inside can be increased.
- This internal liquid is returned by connecting the saccharification apparatus and the slurrying apparatus with a transport pipe, using this as a return line, and pumping a part of the internal liquid in the saccharification apparatus to the slurrying apparatus through this transport pipe.
- a pressure difference may be generated between the slurrying apparatus and the saccharification apparatus, and transport may be performed using this pressure difference.
- the composition of the returned internal liquid consists of water that has been put in the saccharification apparatus from the beginning, biomass straw such as lignin that has not been saccharified, sugar that has been produced, and a small amount of saccharifying enzyme.
- biomass straw such as lignin that has not been saccharified, sugar that has been produced, and a small amount of saccharifying enzyme.
- it is composed of generated ethanol, an organic acid, a fermentation microorganism, and the like.
- the return amount of the saccharification apparatus internal liquid to the slurrying apparatus and the amount of pretreatment biomass supplied to the slurrying apparatus are determined by the following equations.
- the amount of solids in the pretreated biomass supplied from the pretreatment device to the slurrying device is 1 kg / h
- the amount of liquid accompanying the pretreatment biomass is zkg / h
- the saccharification device returns to the slurrying device.
- the amount of solid (mainly lignin) contained in the internal liquid is x kg / h
- the amount of liquid is y kg / h
- the slurry concentration m that can be transported from the slurrying device to the saccharification device is 5%, Holds.
- a means for measuring the slurry concentration m is provided in the supply line for supplying the slurry from the slurrying device to the saccharification device, and the amount of internal liquid to be returned (x + y (kg / h)) or slurrying based on the measurement result You may make it increase / decrease the supply amount of the biomass to an apparatus.
- the slurry concentration m that can be transported from the slurrying device to the saccharification device varies depending on the shape of the solid contained in the slurry. More specifically, when the crushing treatment is performed before the pretreatment, the fibers are finely crushed, so that the fibers contained in the slurry tend to be short, so the fluidity is relatively good, and the slurry concentration m is 8 to 8%. Although it can be transported even if it is about 10%, if the crushing treatment is not performed, the fibers contained in the slurry tend to be long and the fluidity is poor, and if the slurry concentration m is higher than 5%, the transport is possible. It becomes difficult.
- the temperature of the internal liquid returned through the return line is usually 25 to 50 ° C.
- the temperature of the pretreated biomass generally has a temperature of around 80 ° C. because the pretreatment is often performed at a high temperature of 100 ° C. or higher in the presence of water vapor. Since saccharifying enzymes generally deactivate when the temperature exceeds 60 ° C., the pretreated biomass must be quickly cooled when the returned internal solution and the pretreated biomass are brought into contact with each other. Therefore, it is preferable to provide a cooler (A) in the return line.
- the temperature of the internal liquid to be returned is cooled to a temperature lower by about 2 to 12 ° C., and the pretreated biomass is rapidly cooled when the returned internal liquid and the pretreated biomass are mixed,
- the deactivation amount of the saccharifying enzyme in the returned internal liquid can be reduced.
- the temperature of the slurried biomass can be reduced to the same level as the temperature of the internal liquid of the saccharification apparatus, and the saccharification enzyme in the saccharification apparatus is deactivated. Can be prevented.
- a line for supplying biomass slurried by the slurrying apparatus to the saccharification apparatus is used as a supply line, and a cooler (B) is provided in this supply line so that the slurried biomass is cooled before being supplied to the saccharification apparatus. May be.
- the cooler (A) is provided, the temperature between the slurrying tank and the cooler (B) becomes higher and the risk of deactivation increases, but the distance between the slurrying tank and the cooler (B) is shortened. By doing so, operation within the range of practical enzyme inactivation becomes possible.
- coolers (A) and (B) Only one of the coolers (A) and (B) may be provided, but both may be provided for the sake of completeness. When only one of the coolers (A) and (B) is provided, it is desirable to provide the cooler (A) so as not to inactivate the saccharifying enzyme in the saccharified liquid to be returned. Since A) has a demerit that the construction cost is higher, a cooler (B) may be provided.
- FIG. 2 is a flowchart of a biomass processing operation according to the present invention, and shows a case where simultaneous saccharification and fermentation is performed.
- FIG. 1 shows a case where saccharification and fermentation are performed in separate apparatuses
- FIG. 2 shows a case where saccharification and fermentation are performed simultaneously in one apparatus.
- the simultaneous saccharification and fermentation apparatus and the slurrying apparatus are connected by a transport pipe, which is used as a return line, and a part of the internal liquid in the simultaneous saccharification and fermentation apparatus through this return line. Is transported to a slurrying apparatus. Since the return of the internal liquid is the same as in the case of the saccharification apparatus, detailed description is omitted here.
- the point which cools by providing a cooler (A) (B) is the same as that of the case of FIG.
- the saccharification process does not generate heat, but the fermentation process involves heat generation. Therefore, the saccharification and fermentation tank is maintained at a constant temperature by removing the exothermic component.
- the temperature of the slurry biomass supplied to the simultaneous saccharification and fermentation apparatus is lowered by about 0 to 5 ° C. from the temperature of the internal liquid in the simultaneous saccharification and fermentation apparatus, By supplying this to the simultaneous saccharification and fermentation apparatus, the temperature of the internal liquid in the simultaneous saccharification and fermentation apparatus can be kept constant.
- Cooling by the coolers (A) and (B) also contributes to preventing the fermentation microorganisms present in the returned internal liquid and the simultaneous saccharification and fermentation apparatus from being inactivated by touching the high-temperature slurryed biomass. Since others are the same as that of the case of the saccharification apparatus of FIG. 1, detailed description is abbreviate
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Abstract
Description
<請求項1記載の発明>
バイオマスを前処理する前処理装置と、
前処理したバイオマスをスラリー化するスラリー化装置と、
スラリー化したバイオマスを糖化酵素によって糖化する糖化装置と、を有するバイオマスの処理装置において、
前記糖化装置内の内部液の一部を前記スラリー化装置へ返送する返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化する構成にしたことを特徴とするバイオマスの処理装置。
本発明は、返送ラインを通じて糖化装置内の内部液の一部をスラリー化装置へ返送し、この返送した内部液と前処理装置で前処理したバイオマスをスラリー化装置内で混合してスラリー化することにより、スラリー化するための水などを新たに投入しなくても良くなり、糖化装置内の液体量を極力増やさずに、糖化装置に投入するバイオマスの積算量を増やすことができる。
前記糖化装置は、スラリー化したバイオマスを糖化酵素によって糖化する工程と、糖化物を発酵微生物によって発酵する工程を同時に行う同時糖化発酵装置であり、
前記同時発酵装置内の内部液の一部を前記スラリー化装置へ返送するようにした請求項1記載のバイオマスの処理装置。
同時糖化発酵装置を用いて、生成された糖化物を速やかに発酵生成物に変換するため、中間生成物たる糖化物が蓄積して糖化酵素の活性を阻害することを防ぐことができる。
前記返送ラインに返送する内部液を冷却する冷却器を設けた請求項1または2記載のバイオマスの処理装置。
返送ラインを通過する内部液を冷却器によって冷却することで、スラリー化装置内で返送内部液を用いて前処理バイオマスを十分に冷却することができる。その結果、内部液をスラリー化装置に投入したとき、またはスラリー化したバイオマスを糖化装置若しくは同時糖化発酵装置に投入したときに、糖化酵素の失活や発酵微生物の不活化が生じるのを防ぐことができる。
前記スラリー化装置でスラリー化したバイオマスを糖化装置へ供給する供給ラインに、スラリー化したバイオマスを冷却する冷却器を設けた請求項1~3のいずれか1項に記載のバイオマスの処理装置。
供給ラインを通過するスラリー化したバイオマスを冷却器によって冷却することで、スラリー化したバイオマスの温度を低くすることができ、スラリー化したバイオマスを糖化装置に投入したときに、糖化酵素の失活や発酵微生物の不活化が生じるのを防ぐことができる。
前記前処理装置は、熱処理、水熱処理、酸処理、アルカリ処理の少なくともいずれか1つの処理を行い、この処理によってバイオマスの滅菌を行う請求項1または2記載のバイオマスの処理装置。
前処理装置が滅菌処理を行うため、後の工程に滅菌装置を設けて滅菌処理を施さなくても良くなる。
前記スラリー化装置から糖化装置へスラリー輸送管が配置され、スラリー化装置でスラリー化したバイオマスが前記輸送管を通じて糖化装置へ輸送される請求項1または2記載のバイオマスの処理装置。
前処理バイオマスのスラリー化によって輸送管を用いた輸送できるため、コンタミネーションの発生を抑えることができるとともに、建設コストを抑えることができる。
前記返送ラインまたは糖化装置に内部液のスラリー濃度を計測する内部液スラリー濃度計測手段を設け、内部液のスラリー濃度が高い場合に、内部液の返送量を多くする、またはスラリー化装置へ供給するバイオマス量を少なくする請求項1または2記載のバイオマスの処理装置。
内部液のスラリー濃度が高いときに、内部液の返送量を多くすることで、またはスラリー化装置へ供給するバイオマス量を少なくすることで、スラリー化装置内および糖化装置への供給ラインにおいてスラリー濃度が低くなり、流動性が向上することにより閉塞が起こることを防止することができる。
前記スラリー化装置でスラリー化したバイオマスを糖化装置へ供給する供給ラインに、スラリー化したバイオマスのスラリー濃度を計測するバイオマススラリー濃度計測手段を設け、バイオマスのスラリー濃度が高い場合に、内部液の返送量を多くする、またはスラリー化装置へ供給するバイオマス量を少なくする請求項1、2、6または7記載のバイオマスの処理装置。
請求項7と同様の作用効果を有する。
バイオマスを前処理装置によって前処理するステップと、
前処理したバイオマスをスラリー化装置によってスラリー化するステップと、
スラリー化したバイオマスを糖化装置内で糖化酵素と反応させて糖化するステップと、を有するバイオマスの処理方法において、
前記糖化装置内の内部液の一部を前記スラリー化装置へ返送させる返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化することを特徴とするバイオマスの処理方法。
請求項1と同様の作用効果を有する。
バイオマスを前処理装置によって前処理するステップと、
前処理したバイオマスをスラリー化装置によってスラリー化するステップと、
同時糖化発酵装置内で、スラリー化したバイオマスを糖化酵素と反応させて糖化すると同時に、糖化物を発酵微生物と反応させて発酵するステップと、を有するバイオマスの処理方法において、
前記同時糖化発酵装置内の内部液の一部を前記スラリー化装置へ返送させる返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化することを特徴とするバイオマスの処理方法。
請求項2と同様の作用効果を有する。
図1および図2に、バイオマスの処理操作フローの概略を示す。
なお、本発明にかかる装置は、バガス、麦わら、パーム残渣、コーンストーバー、パームヤシ残渣、キャッサバ残渣、木片、木質廃材、ジュート、ケナフ、古紙等のセルロース、ヘミセルロースを含むバイオマスについて好適に使用できる。
セルロース、ヘミセルロースを含むバイオマスは、洗浄工程により、水を用いて砂、小石等の異物と分離され、脱水工程により洗浄工程で添加された水分の多くが除去される。一方、気流サイクロンによる比重差分離のように、水を用いずに異物を分離する方法でも同様の作用が得られる。
前記バイオマスは、主にセルロース、ヘミセルロース、リグニンの3成分が固く結合した複合体となっているうえ、セルロース分子自体も固い結晶構造を取っているため、そのままでは糖化酵素セルラーゼがセルロース分子に接近できない。そのため、前処理装置内で、脱水後のバイオマスを、熱処理、水熱処理、酸処理、アルカリ法、微粉砕法、木材腐朽菌などのどれかで前処理して、前記3成分の結合を緩くさせる必要がある。これにより、糖化酵素セルラーゼがセルロース分子に接触し易くなり、酵素糖化が促進される。その後、通常はコンタミネーションを防ぐために滅菌処理を行うが、熱処理、水熱処理(蒸煮、爆砕)、酸処理(硫酸、硝酸、リン酸などを用いた希酸法、濃酸法、SO2含浸爆砕法)並びにアルカリ処理(苛性ソーダ法、亜硫酸ソーダ法、アンモニア法、水酸化カルシウム法)のいずれかの前処理を行った場合は、その前処理が滅菌効果を有するため、別途滅菌工程を設けなくても良いという利点がある。
前処理を終えたバイオマスをコンベア等の輸送手段を用いて糖化装置へ輸送すると、前述のようにコンタミネーションの生じる可能性があるため、本発明においては前処理後のバイオマスをスラリー化する。具体的には、前処理バイオマスをスラリー化装置へ搬送して、この装置内の液体と混合して、前処理バイオマスが5%程度以下になるようスラリー化する。スラリー化装置は攪拌槽であってもよく、またスタティックミキサーでもよく、単に前処理バイオマスが通る配管と内部返送液が通る配管の合流域のことであっても良い。スラリー化装置と糖化装置は輸送管によって連結し、これを供給ラインとし、スラリー化したバイオマスは、この輸送管を通じて糖化装置へポンプ輸送され、糖化工程に供される。輸送ポンプを用いずに、例えば、スラリー化装置と糖化装置の間に圧力差を生じさせ、この圧力差を利用して輸送するようにしても良い。このように、コンベア等を用いずに、配管によってスラリーを輸送することで、洗浄が容易となり、コンタミネーションの生じる可能性を減らすことができる。
スラリー化したバイオマスは、糖化装置内で糖化される。この糖化装置の代表例としては、バイオリアクターを挙げることができる。この糖化装置内で、スラリー化したバイオマスが主に3種類のセルラーゼ(endoglucanase(EG)、cellobiohydrolase(CBH)、β-glucosidase(BGL))の作用によって分解される。このセルラーゼは、原料の乾燥重量あたり3~30FPU/g、好ましくは5~20FPU/g添加する(FPU/gは60分間にろ紙からグルコースを10.8mg生成するセルラーゼ酵素活性の単位)。なお、本発明における糖化装置には、後述する同時糖化発酵装置が含まれる。
糖化された原料は、さらに酵母や細菌によってエタノール等の有機燃料や有機酸等に加工される。特に、発酵、蒸留により、バイオ燃料としてのエタノールを取得するのが一般的である。糖をエタノールに変換するためには、サッカロマイセス属、シゾサッカロマイセス属、クルイベロマイセス属、ピキア属、キャンジダ属の酵母、ザイモモナス属、クロストリディウム属の細菌、あるいはそれらの特定遺伝子を組み込んだ遺伝子組換微生物を用いる 。このエタノール発酵菌は、例えばサッカロマイセス セレビジエの場合、原料容積あたり1~100g wet-wt/L、好ましくは5~50g wet-wt/L接種する。また、糖を乳酸に変換するためには、例えばリゾプス・オリザエ(Rhizopus oryzae)のような糸状菌等を用いることができ、糖をコハク酸に変換するためには、例えばコリネ型細菌(Coryneform bacterium)、バチルス属細菌、リゾビウム属細菌等を用いることができる。
本発明は、糖化装置内の内部液をスラリー化装置へ返送することに特徴を有する。前述のように、前処理バイオマスをスラリー化するためにスラリー化装置に糖を含まない液体を加えると、糖化装置内で生成される糖の濃度を十分に高くすることができない。一方、前記の糖を含まない液体の代わりに糖化装置内の内部液などの糖を含む液体を用いることで、スラリー化するための液体中にも糖が含まれることとなり、その分、糖化装置内の糖濃度を上昇させることが出来る。
例えば、前処理装置からスラリー化装置へ供給される前処理バイオマスのうち固形物の量を1kg/h、前処理バイオマスに同伴する液体の量をzkg/h、糖化装置からスラリー化装置へ返送される内部液に含まれる固体(リグニンを主とする)の量をxkg /h、液体の量をykg/h、スラリー化装置から糖化装置へ輸送可能なスラリー濃度mを5%とすると、次式が成り立つ。
糖化装置は通常25~50℃で運用されるため、前記返送ラインを通じて返送する内部液の温度は通常25~50℃となる。一方、前処理したバイオマスの温度は、前処理が水蒸気存在下100℃以上の高温で行われることが多いため、一般に80℃前後の温度を有する。糖化酵素は一般に60℃を超えると失活してしまうため、返送内部液と前処理バイオマスを接触させる際は前処理バイオマスを速やかに冷却させなくてはならない。そこで、前記返送ラインに冷却器(A)を設けるようにするのが好ましい。この冷却器(A)によって、返送させる内部液の温度を2~12℃程度低い温度にまで冷却し、返送内部液と前処理バイオマスを混合したときに前処理バイオマスを速やかに冷却することで、返送内部液内の糖化酵素の失活量を少なくすることができる。また、冷却した内部液と前処理バイオマスを混合することによって、スラリー化バイオマスの温度を糖化装置の内部液の温度と同程度にまで低下させることができ、糖化装置内の糖化酵素が失活するのを防ぐことができる。
図2は、本発明にかかるバイオマスの処理操作フロー図であって、同時糖化発酵を行うケースを示したものである。換言すると、図1は糖化と発酵を別々の装置で行うケースを示したが、図2は糖化と発酵を一つの装置内で同時に行うケースを示している。
Claims (10)
- バイオマスを前処理する前処理装置と、
前処理したバイオマスをスラリー化するスラリー化装置と、
スラリー化したバイオマスを糖化酵素によって糖化する糖化装置と、を有するバイオマスの処理装置において、
前記糖化装置内の内部液の一部を前記スラリー化装置へ返送する返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化する構成にしたことを特徴とするバイオマスの処理装置。 - 前記糖化装置は、スラリー化したバイオマスを糖化酵素によって糖化する工程と、糖化物を発酵微生物によって発酵する工程を同時に行う同時糖化発酵装置であり、
前記同時発酵装置内の内部液の一部を前記スラリー化装置へ返送するようにした請求項1記載のバイオマスの処理装置。 - 前記返送ラインに返送する内部液を冷却する冷却器を設けた請求項1または2記載のバイオマスの処理装置。
- 前記スラリー化装置でスラリー化したバイオマスを糖化装置へ供給する供給ラインに、スラリー化したバイオマスを冷却する冷却器を設けた請求項1~3のいずれか1項に記載のバイオマスの処理装置。
- 前記前処理装置は、熱処理、水熱処理、酸処理、アルカリ処理の少なくともいずれか1つの処理を行い、この処理によってバイオマスの滅菌を行う請求項1または2記載のバイオマスの処理装置。
- 前記スラリー化装置から糖化装置へスラリー輸送管が配置され、スラリー化装置でスラリー化したバイオマスが前記輸送管を通じて糖化装置へ輸送される請求項1または2記載のバイオマスの処理装置。
- 前記返送ラインまたは糖化装置に内部液のスラリー濃度を計測する内部液スラリー濃度計測手段を設け、内部液のスラリー濃度が高い場合に、内部液の返送量を多くする、またはスラリー化装置へ供給するバイオマス量を少なくする請求項1または2記載のバイオマスの処理装置。
- 前記スラリー化装置でスラリー化したバイオマスを糖化装置へ供給する供給ラインに、スラリー化したバイオマスのスラリー濃度を計測するバイオマススラリー濃度計測手段を設け、バイオマスのスラリー濃度が高い場合に、内部液の返送量を多くする、またはスラリー化装置へ供給するバイオマス量を少なくする請求項1、2、6または7記載のバイオマスの処理装置。
- バイオマスを前処理装置によって前処理するステップと、
前処理したバイオマスをスラリー化装置によってスラリー化するステップと、
スラリー化したバイオマスを糖化装置内で糖化酵素と反応させて糖化するステップと、を有するバイオマスの処理方法において、
前記糖化装置内の内部液の一部を前記スラリー化装置へ返送させる返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化することを特徴とするバイオマスの処理方法。 - バイオマスを前処理装置によって前処理するステップと、
前処理したバイオマスをスラリー化装置によってスラリー化するステップと、
同時糖化発酵装置内で、スラリー化したバイオマスを糖化酵素と反応させて糖化すると同時に、糖化物を発酵微生物と反応させて発酵するステップと、を有するバイオマスの処理方法において、
前記同時糖化発酵装置内の内部液の一部を前記スラリー化装置へ返送させる返送ラインを設け、
前処理装置で前処理したバイオマスと返送ラインを通じて返送した内部液をスラリー化装置内で混合してバイオマスをスラリー化することを特徴とするバイオマスの処理方法。
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Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62247897A (ja) * | 1986-04-21 | 1987-10-28 | Matsushita Electric Works Ltd | 濃縮機構を備えた微生物反応槽及び微生物反応方法 |
JPH05317074A (ja) * | 1992-05-21 | 1993-12-03 | Takashi Watanabe | セロオリゴ糖の製造装置 |
JP2002301450A (ja) * | 2001-04-06 | 2002-10-15 | Nikkiso Co Ltd | 生ゴミ処理装置 |
JP2006068606A (ja) * | 2004-08-31 | 2006-03-16 | Tsukishima Kikai Co Ltd | 含液固形物の処理設備 |
JP2008523788A (ja) * | 2004-12-17 | 2008-07-10 | アイオゲン エナジー コーポレイション | セルロースの酵素加水分解のための上向流沈殿反応器 |
JP2008259517A (ja) * | 2008-06-30 | 2008-10-30 | Tsukishima Kikai Co Ltd | セルロースからの乳酸製造装置および乳酸製造方法 |
JP2012000022A (ja) * | 2010-06-15 | 2012-01-05 | Tsukishima Kikai Co Ltd | バイオマスの処理装置及び処理方法 |
WO2012114610A1 (ja) * | 2011-02-24 | 2012-08-30 | 月島機械株式会社 | エタノール製造方法 |
Family Cites Families (3)
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KR20130087014A (ko) * | 2010-06-18 | 2013-08-05 | 부타맥스 어드밴스드 바이오퓨얼스 엘엘씨 | 알코올 생산성 향상을 위한 지방산의 보충 |
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-
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Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS62247897A (ja) * | 1986-04-21 | 1987-10-28 | Matsushita Electric Works Ltd | 濃縮機構を備えた微生物反応槽及び微生物反応方法 |
JPH05317074A (ja) * | 1992-05-21 | 1993-12-03 | Takashi Watanabe | セロオリゴ糖の製造装置 |
JP2002301450A (ja) * | 2001-04-06 | 2002-10-15 | Nikkiso Co Ltd | 生ゴミ処理装置 |
JP2006068606A (ja) * | 2004-08-31 | 2006-03-16 | Tsukishima Kikai Co Ltd | 含液固形物の処理設備 |
JP2008523788A (ja) * | 2004-12-17 | 2008-07-10 | アイオゲン エナジー コーポレイション | セルロースの酵素加水分解のための上向流沈殿反応器 |
JP2008259517A (ja) * | 2008-06-30 | 2008-10-30 | Tsukishima Kikai Co Ltd | セルロースからの乳酸製造装置および乳酸製造方法 |
JP2012000022A (ja) * | 2010-06-15 | 2012-01-05 | Tsukishima Kikai Co Ltd | バイオマスの処理装置及び処理方法 |
WO2012114610A1 (ja) * | 2011-02-24 | 2012-08-30 | 月島機械株式会社 | エタノール製造方法 |
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US20150322398A1 (en) | 2015-11-12 |
JP2014003912A (ja) | 2014-01-16 |
BR112014030781A2 (pt) | 2017-06-27 |
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