JPH08317795A - Apparatus for producing cellooligosaccharide - Google Patents
Apparatus for producing cellooligosaccharideInfo
- Publication number
- JPH08317795A JPH08317795A JP7126398A JP12639895A JPH08317795A JP H08317795 A JPH08317795 A JP H08317795A JP 7126398 A JP7126398 A JP 7126398A JP 12639895 A JP12639895 A JP 12639895A JP H08317795 A JPH08317795 A JP H08317795A
- Authority
- JP
- Japan
- Prior art keywords
- cellulose
- cellooligosaccharide
- liquid
- reaction
- cellulase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Landscapes
- Apparatus Associated With Microorganisms And Enzymes (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、セロビオース等のセロ
オリゴ糖の酵素的製造装置−特にセルロース又はセルロ
ース含有物質をセルロース分解酵素セルラーゼの作用に
より加水分解し、生成したセロオリゴ糖を限外ろ過装置
でセルロース又はセルロース含有物質及びセルラーゼと
分離し製造する装置であって、その系内に叩解処理を施
す手段を備えることを特徴とするセロオリゴ糖の製造装
置に関するものである。FIELD OF THE INVENTION The present invention relates to an apparatus for enzymatically producing cellooligosaccharides such as cellobiose-particularly by hydrolyzing cellulose or a cellulose-containing substance by the action of a cellulolytic enzyme cellulase, and the produced cellooligosaccharides by an ultrafiltration apparatus. The present invention relates to an apparatus for separating cellulose or a cellulose-containing substance and cellulase for production, and a cellooligosaccharide production apparatus characterized by comprising a means for performing a beating treatment in the system.
【０００２】[0002]
【従来の技術】従来、酵素加水分解によるセロオリゴ糖
の生成は、一般にセルロースにセルラーゼを作用させる
ことによる低分子化反応によって成される。このセロオ
リゴ糖の製造装置としては、限外ろ過膜を用いた分離装
置を用いるのが一般的であり（特開平1-25639 ）、工業
的な規模では図１に示した様な装置が常識的である。こ
の一般的な膜バイオリアクターシステムは、温度調節装
置（５）を持つ反応槽（２）と加水分解反応により生成
するセロオリゴ糖を分離採取するための限外ろ過膜を用
いた分離装置（４）、及び系内に反応液を循環させる送
液装置（３）並びに送液ライン（６）、いわゆる反応液
循環ラインにより構成されている。装置では、先ずセロ
オリゴ糖の生成原料となるセルロース又はセルロース含
有物質を、反応槽内でセルラーゼの作用により加水分解
してセロオリゴ糖を生成させ、このセロオリゴ糖を含む
反応液を送液装置を介して、セロオリゴ糖を採取する分
離装置に送る。この分離装置では、装置内に設置された
分離膜により、セロオリゴ糖のみを含む透過液と、セロ
オリゴ糖とセルラーゼで分解されなかったセルロース又
はセルロース含有物質を多く含む液とに分離される。前
者は、セロオリゴ糖液として採取し、後者は再び反応さ
せるために、反応槽内に返送する。2. Description of the Related Art Conventionally, the production of cellooligosaccharides by enzymatic hydrolysis is generally carried out by a reaction for lowering the molecular weight by reacting cellulase with cellulose. As a device for producing this cellooligosaccharide, a separation device using an ultrafiltration membrane is generally used (JP-A-1-25639), and on an industrial scale, the device shown in Fig. 1 is common sense. Is. This general membrane bioreactor system comprises a reactor (2) having a temperature control device (5) and a separation device (4) using an ultrafiltration membrane for separating and collecting cellooligosaccharides produced by a hydrolysis reaction. , And a liquid sending device (3) for circulating the reaction liquid in the system, and a liquid sending line (6), a so-called reaction liquid circulating line. In the apparatus, first, cellulose or a cellulose-containing substance that is a raw material for producing cellooligosaccharides is hydrolyzed in the reaction tank by the action of cellulase to produce cellooligosaccharides, and a reaction solution containing the cellooligosaccharides is passed through a liquid feeding device. , Send to a separation device for collecting cellooligosaccharides. In this separation device, a separation membrane installed in the device separates a permeate containing only cellooligosaccharides and a liquid containing many cellooligosaccharides and cellulose or a cellulose-containing substance not decomposed by cellulase. The former is collected as a cellooligosaccharide solution, and the latter is returned to the reaction tank for reaction again.
【０００３】前記従来一般的に知られている反応装置に
おいて、セロオリゴ糖はセルロースの分解産物として製
造される。しかしながら、前記のような反応装置では、
セルロースの分解効率が徐々に低下したり、また限外ろ
過装置での目詰まりを起こしやすい欠点があった。この
解決策として、前者に関しては、酵素の反応性を良くす
るため、原料としてあらかじめ微細化したセルロースを
用いたり、燐酸などの化学処理により低分子化あるいは
膨潤化してから用いる例はあったが、これらの処理を実
施することによって原料が非常に高価になり、また充分
満足できる分解率の得られない欠点があった。後者に関
しては未反応セルロースを一時的に除いて分離装置にか
ける方法（特開平5-317074）等が提案されているが、こ
れも装置的に非常に複雑になる欠点があった。In the above-mentioned conventionally generally known reactor, cellooligosaccharide is produced as a decomposition product of cellulose. However, in the reactor as described above,
There are drawbacks that the decomposition efficiency of cellulose gradually decreases and that clogging in the ultrafiltration device is likely to occur. As a solution to this problem, in the former case, in order to improve the reactivity of the enzyme, there was an example in which a finely divided cellulose was used as a raw material in advance, or it was used after being reduced in molecular weight or swollen by a chemical treatment such as phosphoric acid. By carrying out these treatments, the raw materials became very expensive, and there was a drawback that a satisfactory decomposition rate could not be obtained. Regarding the latter, a method of temporarily removing unreacted cellulose and applying it to a separation device (Japanese Patent Laid-Open No. 5-317074) and the like have been proposed, but this also has a drawback that the device becomes very complicated.
【０００４】[0004]
【発明が解決しようとする課題】そこで、本発明者ら
は、前記問題点を解決すべく鋭意検討した結果、セルロ
ース又はセルロース含有物質とセルラーゼとを反応させ
た後の液、あるいは分離膜等によってセロビオースを分
離除去した後の反応液に対して、叩解処理を施すことに
よって、上記問題点を解決できることを見出し本発明に
到達した。The inventors of the present invention have made extensive studies to solve the above-mentioned problems, and as a result, the liquid after the reaction of cellulose or a cellulose-containing substance with cellulase, or a separation membrane or the like is used. The present inventors have found that the above-mentioned problems can be solved by subjecting the reaction liquid after the cellobiose has been separated and removed to a beating treatment to reach the present invention.
【０００５】従って、本発明の目的は、セルロース又は
セルロース含有物質をセルラーゼの作用により加水分解
してセロオリゴ糖を生成するための反応槽、得られた反
応液を分離するための限外ろ過装置から成るセロオリゴ
糖の製造装置において、叩解処理手段を介在させること
により、セロオリゴ糖の製造を効率よく連続して行うこ
とが可能であるセロオリゴ糖の製造装置を提供すること
を目的とする。Therefore, an object of the present invention is to provide a reaction tank for hydrolyzing cellulose or a cellulose-containing substance by the action of cellulase to produce cellooligosaccharides, and an ultrafiltration device for separating the obtained reaction solution. It is an object of the present invention to provide a cellooligosaccharide production apparatus capable of efficiently and continuously producing cellooligosaccharide by interposing a beating treatment means.
【０００６】[0006]
【課題を解決するための手段】本発明の具体的な装置の
一例を図２に示した。バイオリアクターシステムは、温
度調節装置（５）を持つ反応槽（２）と、加水分解反応
により生成するセロオリゴ糖を分離採取するための限外
ろ過膜を用いた分離装置（４）、及び系内に反応液を循
環させる送液装置（３）並びに送液ライン（６）、いわ
ゆる反応液循環ラインにより構成されている。（８）が
叩解装置である。この叩解機は形式には特にこだわら
ず、また叩解効果のある湿式の粉砕機でもさしつかえな
い。叩解機の例としては、ディスク型のもの、コニカル
型のもの、ビーター型のもの、また粉砕機の例として
は、ボールミル型のもの、湿式ミル型のもの等がある。An example of a concrete apparatus of the present invention is shown in FIG. The bioreactor system comprises a reaction tank (2) having a temperature control device (5), a separation device (4) using an ultrafiltration membrane for separating and collecting cellooligosaccharides produced by a hydrolysis reaction, and an internal system. It is composed of a liquid feeding device (3) for circulating the reaction liquid and a liquid feeding line (6), a so-called reaction liquid circulation line. (8) is a beating apparatus. This beating machine is not particularly limited to the type, and a wet type crusher having a beating effect can be used. Examples of the beater include disc type, conical type, beater type, and examples of the crusher include ball mill type and wet mill type.
【０００７】一般的な叩解の処理条件としては、パルプ
濃度０．１〜２５wt％、温度５〜１８０℃、圧力０．１
〜１５kg/cm 2 （ケ゛ーシ゛ 圧）、そしてｐＨは酸性からア
ルカリ性までの全領域の設定が可能であるが、本発明に
おいては、系内に組み込まれている酵素反応や膜分離装
置の条件によって制約される。従って、通常パルプ濃度
０．５〜５wt％、温度３０〜６０℃、圧力０．５〜１５
kg/cm 2 （ケ゛ーシ゛ 圧）、ｐＨ４〜６の条件に設定する。The general beating treatment conditions are pulp concentration of 0.1 to 25 wt%, temperature of 5 to 180 ° C. and pressure of 0.1.
-15 kg / cm 2 (gauge pressure), and the pH can be set in the whole range from acidic to alkaline, but in the present invention, it is restricted by the enzymatic reaction incorporated in the system and the conditions of the membrane separation device. To be done. Therefore, the pulp concentration is usually 0.5 to 5 wt%, the temperature is 30 to 60 ° C., and the pressure is 0.5 to 15
Set to the conditions of kg / cm 2 (gauge pressure) and pH 4-6.
【０００８】また、叩解の効果すなわちフィブリル化の
最大効果を得るためのこの他の条件として、回転刃の形
状、回転刃の間隔、刃の回転速度等が重要である。先
ず、刃の形状に関しては、刃の幅やピッチの細かいも
の、できれば１〜５ｍｍ程度が好ましい。次に、回転刃
の間隔に関しては、通常では５〜４００μｍ、好ましく
は水で膨潤した繊維１本分以下に相当する５〜５０μｍ
程度に設定するのが好ましい。また、刃の回転速度に関
しては、装置の処理能力と実際の供給量によって決まる
が、周速として通常５〜５０ｍ／秒に設定する。なお、
以上の条件は、セロオリゴ糖の生成原料であるセルロー
ス又はセルロース含有物質の種類や性状によって好適条
件が多少変化する。Further, as other conditions for obtaining the effect of beating, that is, the maximum effect of fibrillation, the shape of the rotary blade, the interval between the rotary blades, the rotational speed of the blade, etc. are important. First, regarding the shape of the blade, it is preferable that the width and pitch of the blade are small, preferably about 1 to 5 mm. Next, with respect to the distance between the rotary blades, it is usually 5 to 400 μm, preferably 5 to 50 μm corresponding to one fiber swollen with water or less.
It is preferable to set it to a degree. The blade rotation speed is usually set to 5 to 50 m / sec as the peripheral speed, although it depends on the processing capacity of the device and the actual supply amount. In addition,
Regarding the above conditions, suitable conditions are somewhat changed depending on the type and properties of cellulose or a cellulose-containing substance, which is a raw material for producing cellooligosaccharides.
【０００９】また、図に示したように反応前の原料も叩
解機に通す（図２に示す点線部分）ことにより、より一
層の効果が得られる。さらに叩解機を設置する場所は、
図３、図４に示したように、送液ライン（６）のどこで
もかまわない。また、送液装置（３）と叩解機（８）を
兼ね合わせることも可能である。なお、本装置で用いる
限外ろ過膜を用いた分離装置はチューブラー型のものが
一般的であるが、デッドエンドタイプを含めた平膜型の
ものでも構わない。また、分離装置として、限外ろ過等
の半透膜を用いるろ過のほか、無機及び有機ろ材を用い
る一般的なろ過、さらには遠心力や重力沈降を含む固液
分離装置を組み合わせたセロオリゴ糖の製造装置での応
用も可能である。Further, as shown in the figure, the raw material before the reaction is also passed through the beater (dotted line portion shown in FIG. 2) to obtain a further effect. Furthermore, the place to install the beater is
As shown in FIGS. 3 and 4, it may be anywhere in the liquid delivery line (6). It is also possible to combine the liquid delivery device (3) and the beater (8). The separation device using the ultrafiltration membrane used in this device is generally a tubular type, but may be a flat membrane type including a dead end type. Further, as a separation device, in addition to filtration using a semipermeable membrane such as ultrafiltration, general filtration using inorganic and organic filter media, and further a cellooligosaccharide combining a solid-liquid separation device including centrifugal force and gravity settling It can also be applied to manufacturing equipment.
【００１０】本発明におけるセロオリゴ糖の製造原料と
するセルロース又はセルロース含有物質としては、木材
パルプやリンターパルプ及びそれらの粉末、木材チッ
プ、木粉、廃木の木質原料及びそれらを利用した再生セ
ルロース、更に農業副産物である稲ワラ、モミやサトウ
キビ、トウモロコシ等の廃棄物、更に果実の絞り粕等、
を広く選択することができる。The cellulose or cellulose-containing substance used as a raw material for producing cellooligosaccharides in the present invention includes wood pulp, linter pulp and powders thereof, wood chips, wood flour, wood raw materials of waste wood, and regenerated cellulose using them. In addition, agricultural by-products such as rice straw, fir and sugar cane, corn, and other waste products, as well as fruit cakes, etc.
Can be widely selected.
【００１１】本発明におけるセルロース分解酵素セルラ
ーゼの種類については特定されず、通常の培養によって
得られたセルラーゼを用いることもできるし、市販のセ
ルラーゼを用いることもできる。また、このセルラーゼ
は、液体状のもの、粉末状のもの等の、その形状には特
に限定されない。The type of cellulolytic enzyme cellulase in the present invention is not specified, and cellulase obtained by ordinary culture may be used, or commercially available cellulase may be used. The shape of this cellulase is not particularly limited, and it may be liquid or powder.
【００１２】[0012]
【作用】本装置では、反応槽内でセルラーゼと反応しき
れなかったセルロース成分のみが集中的に叩解されるた
め、効果的にフィブリル化及び微細化まで行われる。ま
た、これら反応液中に残存するセルロース成分は、一度
セルラーゼによる加水分解反応を受けているために、消
費エネルギーも少なくかつ叩解によって容易にフィブリ
ル化及び微細化することができる。その結果、再びセル
ラーゼとの反応性が良くなり、効率良くセロビオースに
変換し、微細セルロース等は消失するため、限外ろ過装
置内での詰まりはなくなる。In this apparatus, only the cellulose component that has not completely reacted with the cellulase in the reaction vessel is beaten intensively, so that fibrillation and micronization are effectively performed. Further, since the cellulose component remaining in these reaction solutions has once undergone the hydrolysis reaction by cellulase, it consumes less energy and can be easily fibrillated and refined by beating. As a result, the reactivity with cellulase becomes good again, the cells are efficiently converted into cellobiose, and the fine cellulose and the like disappear, so that the clogging in the ultrafiltration device is eliminated.
【００１３】[0013]
【実施例】 （実施例１）図２の本発明のセロオリゴ糖製造装置を用
いて、セロオリゴ糖の製造を以下のように行った。セル
ロース原料（１）としては、亜硫酸パルプ製造工程で得
られた漂白した溶解パルプを用いた。２wt％の溶解パル
プを反応槽（２）に送り込み、この槽内の液温を温度調
節装置（５）により５０℃に調節し、ｐＨを５．０に調
製した後、溶解パルプに対して１wt％のセルラーゼを添
加し、加水分解反応を開始した。生成したセロオリゴ糖
を含む反応液送液装置（３）を介して分離装置（４）
（日東電工社製、チューブラー型限外ろ過装置（NTU-35
20）、ポリスルホン系膜、分画分子量20,000）に送っ
た。この時の平均操作圧力は、入口圧５〜６kg/cm 2 、
出口圧３．５〜４．５kg/cm 2 、チューブ内の平均流量
は、１５リットル／分とした。この分離装置（４）にて、目
的物であるセロオリゴ糖を透過液（７）と共に採取す
る。透過液が採取された後のセルロース性繊維を含む反
応液を、叩解装置（８）（熊谷理機工業社製シングルデ
ィスクリファイナー、リファイナープレート18034-N ）
に送り込み、叩解処理による繊維の改質を施した後、再
び反応槽に返送した。この時の回転刃の間隔は、０．４
mm、回転刃の回転数は、３０００rpm （周速として、約
４５m/秒）であった。EXAMPLES Example 1 Using the cellooligosaccharide production apparatus of the present invention shown in FIG. 2, cellooligosaccharides were produced as follows. As the cellulose raw material (1), the bleached dissolving pulp obtained in the sulfite pulp manufacturing process was used. 2 wt% of dissolving pulp was sent to the reaction tank (2), the liquid temperature in this tank was adjusted to 50 ° C. by the temperature controller (5), and the pH was adjusted to 5.0, and then 1 wt. % Cellulase was added to initiate the hydrolysis reaction. Separation device (4) via reaction liquid delivery device (3) containing the produced cellooligosaccharide
(Nitto Denko Co., Ltd., tubular type ultrafiltration device (NTU-35
20), polysulfone-based membrane, molecular weight cut off 20,000). The average operating pressure at this time is 5-6 kg / cm 2 at the inlet pressure,
The outlet pressure was 3.5 to 4.5 kg / cm 2 , and the average flow rate in the tube was 15 liters / minute. In the separation device (4), the target cellooligosaccharide is collected together with the permeate (7). The reaction liquid containing cellulosic fibers after the permeated liquid was collected was beaten (8) (Kumagaya Riki Kogyo Co., Ltd. single disc refiner, refiner plate 18034-N)
Then, the fibers were modified by beating and then returned to the reaction tank. The interval between the rotary blades at this time is 0.4
mm, the rotation speed of the rotary blade was 3000 rpm (peripheral speed was about 45 m / sec).
【００１４】前記セルラーゼを添加して３０分後から、
分離装置（４）を透過した透過液（７）を連続的に採取
すると共に、この透過液量と同量の１wt％溶解パルプス
ラリー液を叩解装置（８）を介して追加することによ
り、反応系内の液量及びパルプ濃度をほぼ一定に保つよ
うにした。After 30 minutes from the addition of the cellulase,
The permeated liquid (7) that has permeated the separator (4) is continuously collected, and the same amount of 1 wt% dissolved pulp slurry liquid as this permeated liquid is added via the beating device (8) to react. The liquid amount and pulp concentration in the system were kept almost constant.
【００１５】このようにして、セロオリゴ糖の製造装置
（図２）を連続的に運転することにより分離装置（４）
からセロオリゴ糖を含む液を多量に採取した。In this way, by continuously operating the cellooligosaccharide production apparatus (FIG. 2), the separation apparatus (4)
A large amount of a liquid containing cellooligosaccharide was collected from.
【００１６】また、経時的に透過液中の糖濃度及び透過
流束を測定した。結果を表１に示した。本発明による叩
解装置を使った装置では、セロビオース濃度及び透過流
束がほぼ一定に保たれた。Further, the sugar concentration in the permeate and the permeation flux were measured over time. The results are shown in Table 1. In the apparatus using the beating apparatus according to the present invention, the cellobiose concentration and the permeation flux were kept substantially constant.
【００１７】表１の比較例では、実施例と同じセルロー
ス原料を用い、また酵素反応条件及び膜による分離につ
いても実施例と同一の条件で行ったが、図１に示したよ
うな装置で、その後の叩解処理を行わなかったところセ
ロビオース濃度及び透過流束が徐々に低下した。In the comparative example shown in Table 1, the same cellulose raw material as that used in the example was used, and the enzymatic reaction conditions and the separation by the membrane were performed under the same conditions as the example, but the apparatus shown in FIG. When the subsequent beating process was not performed, the cellobiose concentration and the permeation flux gradually decreased.
【００１８】このようにして、セロオリゴ糖の製造装置
（図１）を連続的に運転することにより分離装置（４）
からセロオリゴ糖を含む透過液を多量に採取した。In this way, by continuously operating the cellooligosaccharide production apparatus (FIG. 1), the separation apparatus (4)
A large amount of permeated liquid containing cellooligosaccharide was collected from.
【００１９】また、経時的に透過液中の糖濃度及び透過
流束を測定した。結果を表１に示した。本発明による叩
解装置を使った装置では、セロビオース濃度及び透過流
束がほぼ一定に保たれた。Further, the sugar concentration in the permeate and the permeation flux were measured over time. The results are shown in Table 1. In the apparatus using the beating apparatus according to the present invention, the cellobiose concentration and the permeation flux were kept substantially constant.
【００２０】（実施例２）上記実施例１と同様に、図３
の本発明のセロオリゴ糖製造装置を用いて、セロオリゴ
糖の製造を行った。セルロース原料（１）及び反応槽
（２）での酵素反応条件は、実施例１と同一条件で行っ
た。透過液が採取された後のセルロース性繊維を含む反
応液を、叩解装置（８）（熊谷理機工業社製加圧リファ
イナー、リファイナープレート18034-N ）に送り込み、
叩解処理による繊維の改質を施した後、再び反応槽に返
送した。この時の回転刃の間隔は、０．４mm、回転刃の
回転数は、３０００rpm （周速は約４５m ／秒）であっ
た。(Embodiment 2) As in Embodiment 1 above, FIG.
The cellooligosaccharides were produced using the cellooligosaccharide production apparatus of the present invention. The enzyme reaction conditions in the cellulose raw material (1) and the reaction tank (2) were the same as in Example 1. The reaction liquid containing the cellulosic fibers after the permeated liquid was collected was sent to a beating device (8) (a pressure refiner made by Kumagai Riki Kogyo Co., Ltd., a refiner plate 18034-N),
After the fibers were modified by beating, they were returned to the reaction tank. At this time, the interval between the rotary blades was 0.4 mm, and the rotation speed of the rotary blade was 3000 rpm (peripheral speed was about 45 m 2 / sec).
【００２１】前記セルラーゼを添加して３０分後から、
分離装置（４）を透過した透過液（７）を連続的に採取
すると共に、この透過液量と同量の１wt％溶解パルプス
ラリー液を叩解装置（８）を介して追加することによ
り、反応系内の液量及びパルプ濃度をほぼ一定に保つよ
うにした。After 30 minutes from the addition of the cellulase,
The permeated liquid (7) that has permeated the separator (4) is continuously collected, and the same amount of 1 wt% dissolved pulp slurry liquid as this permeated liquid is added via the beating device (8) to react. The liquid amount and pulp concentration in the system were kept almost constant.
【００２２】このようにして、セロオリゴ糖の製造装置
（図３）を連続的に運転することにより分離装置（４）
からセロオリゴ糖を含む透過液を多量に採取した。In this way, by continuously operating the cellooligosaccharide production apparatus (FIG. 3), the separation apparatus (4)
A large amount of permeated liquid containing cellooligosaccharide was collected from.
【００２３】また、経時的に透過液中の糖濃度及び透過
流束を測定した。結果を表２に示した。本発明による叩
解装置を使った装置では、セロビオース濃度及び透過流
束がほぼ一定に保たれた。Further, the sugar concentration in the permeate and the permeation flux were measured over time. The results are shown in Table 2. In the apparatus using the beating apparatus according to the present invention, the cellobiose concentration and the permeation flux were kept substantially constant.
【００２４】[0024]
【表１】 [Table 1]
【表２】 [Table 2]
【００２５】[0025]
【発明の効果】以上述べたように、本発明の酵素反応液
に叩解処理を施す手段を具備した装置を使用することに
よって、限外ろ過装置内での詰まりもなく、ほぼ一定の
透過液流束及びセロビオース濃度が得られ、セロオリゴ
糖の製造装置を連続的に、かつ安定して運転することが
できる。このことによって、セルロース又はセルロース
含有物質からセロオリゴ糖を効率よく連続的に製造する
ことができる。As described above, by using the apparatus equipped with the means for subjecting the enzyme reaction solution of the present invention to beating treatment, there is no clogging in the ultrafiltration apparatus and a substantially constant permeate flow rate. The bundle and cellobiose concentrations are obtained, and the cellooligosaccharide production apparatus can be operated continuously and stably. As a result, cellooligosaccharides can be efficiently and continuously produced from cellulose or a substance containing cellulose.
【図１】従来のセロオリゴ糖の製造装置の概略図であ
る。FIG. 1 is a schematic view of a conventional cellooligosaccharide production apparatus.
【図２】本発明の実施例１のセロオリゴ糖の製造装置の
概略図である。FIG. 2 is a schematic view of a cellooligosaccharide production apparatus of Example 1 of the present invention.
【図３】本発明の実施例２のセロオリゴ糖の製造装置の
概略図である。FIG. 3 is a schematic view of a cellooligosaccharide production apparatus of Example 2 of the present invention.
【図４】本発明の実施例以外のその他のセロオリゴ糖の
製造装置の概略図である。FIG. 4 is a schematic view of another cellooligosaccharide production apparatus other than the example of the present invention.
【符号の説明】 （１）原料 （２）反応槽 （３）送液装置 （４）分離装置 （５）温度調節装置 （６）送液ライン （７）透過液 （８）叩解装置[Explanation of Codes] (1) Raw material (2) Reaction tank (3) Liquid feeder (4) Separator (5) Temperature controller (6) Liquid feed line (7) Permeate (8) Beating device
Claims (2)
ルラーゼの作用により加水分解してセロオリゴ糖を生成
するための反応槽、得られた反応液を分離するための限
外ろ過装置に送液するための送液手段を有する送液装置
を介して設けられた限外ろ過装置、及びセルロース又は
セルロース含有物質を含む反応液を再度反応槽に送液す
るための送液手段からなるセロオリゴ糖の製造装置にお
いて、その送液手段に叩解処理手段を介在させることを
特徴とするセロオリゴ糖の製造装置。1. A reaction tank for hydrolyzing cellulose or a cellulose-containing substance by the action of cellulase to produce cellooligosaccharides, and a feed for feeding the obtained reaction solution to an ultrafiltration device for separation. In an apparatus for producing cellooligosaccharides, which comprises an ultrafiltration device provided via a liquid feeding device having a liquid means, and a liquid feeding means for feeding a reaction liquid containing cellulose or a cellulose-containing substance to a reaction tank again, An apparatus for producing cellooligosaccharides, characterized in that a beating treatment means is interposed in the liquid feeding means.
置に至る送液手段及び／又は限外ろ過装置から反応槽に
至る送液手段に設けられている請求項１記載のセロオリ
ゴ糖製造装置。2. The cellooligosaccharide production according to claim 1, wherein the beating treatment means is provided in the liquid feeding means from the reaction tank to the ultrafiltration device and / or the liquid feeding means from the ultrafiltration device to the reaction tank. apparatus.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7126398A JPH08317795A (en) | 1995-05-25 | 1995-05-25 | Apparatus for producing cellooligosaccharide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7126398A JPH08317795A (en) | 1995-05-25 | 1995-05-25 | Apparatus for producing cellooligosaccharide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH08317795A true JPH08317795A (en) | 1996-12-03 |
Family
ID=14934171
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7126398A Pending JPH08317795A (en) | 1995-05-25 | 1995-05-25 | Apparatus for producing cellooligosaccharide |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH08317795A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006087319A (en) * | 2004-09-22 | 2006-04-06 | Research Institute Of Innovative Technology For The Earth | Method for continuously saccharifying lignocellulose |
| JP2013517134A (en) * | 2010-01-20 | 2013-05-16 | ザイレコ，インコーポレイテッド | Raw material dispersion and material processing method |
| JP2015231388A (en) * | 2009-03-31 | 2015-12-24 | ベータ リニューアブルス エス・ピー・エーＢＥＴＡ ＲＥＮＥＷＡＢＬＥＳ Ｓ．ｐ．Ａ． | An improved process for the rapid hydrolysis of high solids biomass |
| US10781466B2 (en) | 2014-09-05 | 2020-09-22 | Toray Industries, Inc. | Method of producing sugar liquid |
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1995
- 1995-05-25 JP JP7126398A patent/JPH08317795A/en active Pending
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2006087319A (en) * | 2004-09-22 | 2006-04-06 | Research Institute Of Innovative Technology For The Earth | Method for continuously saccharifying lignocellulose |
| JP4554314B2 (en) * | 2004-09-22 | 2010-09-29 | 財団法人地球環境産業技術研究機構 | Continuous saccharification method of lignocellulose |
| JP2015231388A (en) * | 2009-03-31 | 2015-12-24 | ベータ リニューアブルス エス・ピー・エーＢＥＴＡ ＲＥＮＥＷＡＢＬＥＳ Ｓ．ｐ．Ａ． | An improved process for the rapid hydrolysis of high solids biomass |
| JP2013517134A (en) * | 2010-01-20 | 2013-05-16 | ザイレコ，インコーポレイテッド | Raw material dispersion and material processing method |
| US9260735B2 (en) | 2010-01-20 | 2016-02-16 | Xyleco, Inc. | Dispersing feedstocks and processing materials |
| US9428722B2 (en) | 2010-01-20 | 2016-08-30 | Xyleco, Inc. | Dispersing feedstocks and processing materials |
| JP2016154547A (en) * | 2010-01-20 | 2016-09-01 | ザイレコ，インコーポレイテッド | Method for dispersing feedstocks and method for processing materials |
| JP2017212997A (en) * | 2010-01-20 | 2017-12-07 | ザイレコ，インコーポレイテッド | Method for processing raw material dispersion and material |
| US10053662B2 (en) | 2010-01-20 | 2018-08-21 | Xyleco, Inc. | Dispersing feedstocks and processing materials |
| US10781466B2 (en) | 2014-09-05 | 2020-09-22 | Toray Industries, Inc. | Method of producing sugar liquid |
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