JP3439675B2 - Method of hydrolysis of fats and oils - Google Patents
Method of hydrolysis of fats and oilsInfo
- Publication number
- JP3439675B2 JP3439675B2 JP33516498A JP33516498A JP3439675B2 JP 3439675 B2 JP3439675 B2 JP 3439675B2 JP 33516498 A JP33516498 A JP 33516498A JP 33516498 A JP33516498 A JP 33516498A JP 3439675 B2 JP3439675 B2 JP 3439675B2
- Authority
- JP
- Japan
- Prior art keywords
- substrate
- enzyme
- oil
- water
- supply tank
- 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.)
- Expired - Fee Related
Links
- 239000003921 oil Substances 0.000 title claims description 49
- 238000000034 method Methods 0.000 title claims description 19
- 239000003925 fat Substances 0.000 title claims description 13
- 230000007062 hydrolysis Effects 0.000 title claims description 4
- 238000006460 hydrolysis reaction Methods 0.000 title claims description 4
- 239000012071 phase Substances 0.000 claims description 47
- 239000000758 substrate Substances 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 108090000790 Enzymes Proteins 0.000 claims description 35
- 102000004190 Enzymes Human genes 0.000 claims description 35
- 238000006243 chemical reaction Methods 0.000 claims description 21
- 238000000926 separation method Methods 0.000 claims description 14
- 239000008346 aqueous phase Substances 0.000 claims description 10
- 108010093096 Immobilized Enzymes Proteins 0.000 claims description 7
- 230000003301 hydrolyzing effect Effects 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 2
- 235000019198 oils Nutrition 0.000 description 42
- 238000000354 decomposition reaction Methods 0.000 description 10
- 239000012295 chemical reaction liquid Substances 0.000 description 9
- 238000000605 extraction Methods 0.000 description 7
- 108090001060 Lipase Proteins 0.000 description 6
- 102000004882 Lipase Human genes 0.000 description 6
- 239000004367 Lipase Substances 0.000 description 6
- 235000019421 lipase Nutrition 0.000 description 6
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 5
- 239000007788 liquid Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 235000012424 soybean oil Nutrition 0.000 description 4
- 239000003549 soybean oil Substances 0.000 description 4
- 235000014113 dietary fatty acids Nutrition 0.000 description 3
- 229930195729 fatty acid Natural products 0.000 description 3
- 239000000194 fatty acid Substances 0.000 description 3
- 150000004665 fatty acids Chemical class 0.000 description 3
- 239000012528 membrane Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000003756 stirring Methods 0.000 description 3
- LDVVTQMJQSCDMK-UHFFFAOYSA-N 1,3-dihydroxypropan-2-yl formate Chemical compound OCC(CO)OC=O LDVVTQMJQSCDMK-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 235000011187 glycerol Nutrition 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 235000014593 oils and fats Nutrition 0.000 description 2
- 238000007127 saponification reaction Methods 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 108090000371 Esterases Proteins 0.000 description 1
- 240000007930 Oxalis acetosella Species 0.000 description 1
- 235000008098 Oxalis acetosella Nutrition 0.000 description 1
- 229920002125 Sokalan® Polymers 0.000 description 1
- 235000009508 confectionery Nutrition 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 229910003460 diamond Inorganic materials 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000001804 emulsifying effect Effects 0.000 description 1
- 238000006911 enzymatic reaction Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000003100 immobilizing effect Effects 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 229920001282 polysaccharide Polymers 0.000 description 1
- 239000005017 polysaccharide Substances 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Enzymes And Modification Thereof (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Fats And Perfumes (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、脂肪酸を製造する
ための、効率的な油脂の加水分解方法に関する。TECHNICAL FIELD The present invention relates to an efficient method for hydrolyzing fats and oils for producing fatty acids.
【０００２】[0002]
【従来の技術】酵素を用いての油脂の連続的加水分解方
法として、油脂分解酵素（リパーゼ）を樹脂や膜に固定
化し、バッチ攪拌式多段反応器や充填塔や膜反応器等の
流通式反応器として使用し、油状基質と水溶性基質を向
流あるいは並流で流通させる方法がある（特開昭６１−
８５１９５号公報、特開昭６３−５９８９６号公報、特
開平１−９８４９４号公報）。しかし何れの方法にして
も装置が複雑になったり、酵素塔の運転方法が非常に難
しい。さらにバッチ循環方式の反応例が、特開昭５８−
１４６２８４号公報に紹介されているが、多量の水分を
含む多糖類ゲルに固定化したリパーゼを用いて、油脂の
みの添加で、水相基質を添加せずに加水分解する方法で
あり、繰り返し使用の回数を増やすと、分解に必要な水
分が不足する恐れがあり、さらに固定化酵素に水相生成
物であるグリセリンが蓄積して、平衡が働き十分な分解
率を得られない恐れがある。また特開平４−３３５８８
１号公報では、均一に混合され、水分量が均一に維持さ
れた反応液を循環する反応装置が提案されているが、最
終生成物の油相と水相の分離が難しくなり、分離のため
の工程、付帯設備が必要になる。2. Description of the Related Art As a continuous hydrolysis method of fats and oils using an enzyme, a fats and fats-decomposing enzyme (lipase) is immobilized on a resin or a membrane, and a batch stirring type multistage reactor, a packed tower or a membrane reactor, etc. There is a method in which an oily substrate and a water-soluble substrate are used as a reactor, and the oily substrate and the water-soluble substrate are allowed to flow countercurrently or in parallel (Japanese Patent Laid-Open No. 61-61).
85195, JP-A-63-59896, and JP-A-1-98494). However, whichever method is used, the apparatus becomes complicated and the operation method of the enzyme tower is very difficult. Furthermore, a reaction example of a batch circulation system is disclosed in JP-A-58-58.
As disclosed in Japanese Patent No. 146284, it is a method of using a lipase immobilized on a polysaccharide gel containing a large amount of water and adding only oils and fats without adding an aqueous phase substrate, and repeatedly used. If the number of times is increased, the water required for decomposition may be insufficient, and further, glycerol, which is a water phase product, may be accumulated in the immobilized enzyme, and equilibrium may not work to obtain a sufficient decomposition rate. In addition, JP-A-4-33588
In Japanese Patent Laid-Open No. 1, a reactor is proposed which circulates a reaction solution in which the amount of water is uniformly mixed and the amount of water is uniformly maintained. Process and incidental equipment are required.
【０００３】[0003]
【発明が解決しようとする課題】酵素を用いた油脂の加
水分解法では、簡易な設備と簡単な操作で且つ十分な反
応速度を得ながら、酵素を損失することなく、更に油相
生成物と水相生成物を遠心分離や膜を一切使用せずに分
離できることが望まれている。[Problems to be Solved by the Invention] In the method for hydrolyzing fats and oils using an enzyme, an oil phase product is further obtained without loss of enzyme while obtaining a sufficient reaction rate with simple equipment and operation. It is desirable to be able to separate the aqueous phase product without centrifuging or using any membrane.
【０００４】[0004]
【課題を解決するための手段】本発明者は、酵素の回収
には固定化酵素を使用し、油相と水相の分離はこれらの
基質の供給槽で自然分離を行いながら反応を繰り返すこ
とで、従来問題であった反応速度や生成物の分離を解決
し、さらに酵素塔と基質供給槽のみからなる装置である
ため、設備が簡易で且つ運転方法が簡単で安定した運転
が可能になると同時に、設備投資も安価であるバッチ式
の油脂の加水分解方法を見出した。即ち本発明は、攪拌
を行わずに油相と水相を供給槽で分離させておき、これ
らを別々の配管で抜き出して酵素と接触させ、酵素塔か
ら流出する反応液を供給槽で油相と水相に分離し、これ
を繰り返すことで上記の課題を解決するものである。よ
り具体的には、本発明は、固定化酵素を用いた酵素塔
（反応塔）と油水分離槽を兼ねた基質供給槽とを用いた
油脂の加水分解方法であって、酵素塔からの反応液の排
出部分を基質供給槽の油相中であって水相との界面付近
に設け、酵素塔と基質供給槽との間で反応液を循環させ
ると共に、基質供給槽に油水界面を形成させ、油相基質
を基質供給槽の油相の中位部から上方の位置、水相基質
を基質供給槽の底部から夫々抜き出し、油相基質と水相
基質とを予め混合せずに酵素塔へ供給するバッチ式の油
脂の加水分解方法である。本発明では、基質供給槽に反
応液を戻す配管は分離上層中に浸漬し、油水界面を乱す
ことない様に取り付けられ、さらに反応液の循環流量を
調整する。これにより固定化酵素の充填塔を使用するこ
とで十分な反応速度を得ることができ、酵素の損失が抑
制できる。さらに供給槽で油相と水相の比重差を用いて
分離することで、油水分離のための特別な装置を一切使
用しないで済む。Means for Solving the Problems The present inventor uses an immobilized enzyme for the recovery of the enzyme, and the separation of the oil phase and the aqueous phase repeats the reaction while performing natural separation in a supply tank for these substrates. Therefore, it is possible to solve the reaction rate and the separation of products, which have been problems in the past, and further, since the apparatus is composed of only the enzyme tower and the substrate supply tank, the equipment is simple and the operation method is simple and stable operation is possible. At the same time, it is a batch system with low capital investment
The method of hydrolyzing the oils and fats was discovered. That is, according to the present invention, the oil phase and the aqueous phase are separated in a supply tank without stirring, and these are extracted through separate pipes and brought into contact with an enzyme, and the reaction liquid flowing out from the enzyme tower is oil phase in the supply tank. The above-mentioned problem is solved by separating into an aqueous phase and repeating this. Yo
More specifically, the present invention relates to an enzyme tower using an immobilized enzyme.
(Reaction tower) and a substrate supply tank that doubled as an oil / water separation tank were used.
A method for hydrolyzing fats and oils, in which the reaction liquid is discharged from the enzyme tower.
The output part is in the oil phase of the substrate supply tank and near the interface with the water phase
The reaction solution is circulated between the enzyme tower and the substrate supply tank.
In addition to forming an oil-water interface in the substrate supply tank,
The position above the middle part of the oil phase of the substrate supply tank, the water phase substrate
From the bottom of the substrate supply tank to separate the oil phase substrate and the water phase.
Batch type oil that is supplied to the enzyme column without premixing with the substrate
It is a method of hydrolyzing fat. In the present invention, the pipe for returning the reaction liquid to the substrate supply tank is immersed in the separation upper layer so as not to disturb the oil-water interface, and the circulation flow rate of the reaction liquid is adjusted. As a result, a sufficient reaction rate can be obtained by using a packed column of immobilized enzyme, and the loss of enzyme can be suppressed. Furthermore, by using the difference in specific gravity between the oil phase and the water phase in the supply tank, it is not necessary to use any special device for oil / water separation.
【０００５】[0005]
【発明の実施の形態】反応に使用する酵素は担体に吸着
固定化したものを用いうる。酵素の種類は油脂を加水分
解するものであれば良く、例えばリパーゼやエステラー
ゼ等が挙げられる。酵素の担体への吸着方法についても
限定されるものではなく、例えば特開平１−１５３０９
０号公報に記載の方法が挙げられる。使用する固定化酵
素の量は生産能力に見合った量（活性）を使用すれば良
い。酵素塔の形状に関しては、使用するポンプの押し込
み圧に耐えられるものであれば良い。さらにジャケット
により酵素反応に適した温度に加温できるものが良い。BEST MODE FOR CARRYING OUT THE INVENTION The enzyme used in the reaction may be immobilized on a carrier. Any kind of enzyme may be used as long as it hydrolyzes fats and oils, and examples thereof include lipase and esterase. The method for adsorbing the enzyme on the carrier is not limited, and is disclosed in, for example, JP-A-1-15309.
The method described in Japanese Patent No. 0 can be mentioned. The amount of immobilized enzyme to be used may be an amount (activity) suitable for the production capacity. The shape of the enzyme tower may be any as long as it can withstand the pushing pressure of the pump used. Furthermore, it is preferable that the jacket be capable of heating to a temperature suitable for the enzyme reaction.
【０００６】油水分離槽を兼ねた基質供給槽は、攪拌装
置を有しない。静置分離した油相と水相を別々に抜き出
し酵素塔へ送る配管を有する。さらに酵素塔から流出す
る反応液を戻すための配管を有する。油相の抜き出し配
管は、油相の中位部から上方の位置に抜き出し口を配置
する。一方、水相の抜き出し配管は、基質供給槽の底部
に抜き出し口を配置する。また反応液の戻り配管は、油
相と水相の界面を乱さない位置に戻し口を配置する。こ
れらの位置は生産量（反応液流量）や使用酵素量によっ
ても変わるので、適宜調整すればよい。また基質供給槽
の形状（槽高／槽径等）に関しては、油水分離が良好に
出来る様に設計したものであればよい。この基質供給槽
も酵素塔と同様に加温できるものがよい。The substrate supply tank which also serves as the oil-water separation tank does not have a stirring device. It has a pipe for separately extracting the oil phase and the water phase, which have been separated by standing, and sending them to the enzyme tower. Further, it has a pipe for returning the reaction liquid flowing out from the enzyme tower. The oil phase extraction pipe is provided with an extraction port at a position above the middle part of the oil phase. On the other hand, the water phase extraction pipe has an extraction port at the bottom of the substrate supply tank. Further, the return pipe for the reaction solution has a return port at a position where it does not disturb the interface between the oil phase and the water phase. These positions vary depending on the production amount (reaction liquid flow rate) and the amount of enzyme used, and may be adjusted accordingly. Further, the shape (tank height / tank diameter, etc.) of the substrate supply tank may be designed so that oil-water separation can be performed well. It is preferable that this substrate supply tank also be capable of heating like the enzyme tower.
【０００７】酵素塔への基質の供給は塔頂から塔底へ下
方流で行っても、塔底から塔頂へ上方流で行っても良い
が、油相基質、水相基質とも同方向へ流す。これまで向
流式の反応装置が提案されてきたが、液（油脂）−液
（水）系反応において充填塔内を向流で流通させること
はかなり難しく、装置上の工夫を伴い、煩雑になる。よ
って、本発明においては、液（油脂）−液（水）を並
流、即ち同一方向へ流通させ、油相、水相の供給ポンプ
の出口で混合されて酵素塔へ送られる。The substrate may be supplied to the enzyme tower in a downward flow from the top to the bottom of the tower or in an upward flow from the bottom to the top of the column, but both the oil phase substrate and the water phase substrate are in the same direction. Shed. Up to now, a countercurrent type reaction device has been proposed, but in a liquid (oil / fat) -liquid (water) system reaction, it is quite difficult to flow in a packed column in a countercurrent, and it is complicated and requires a device. Become. Therefore, in the present invention, the liquid (oil / fat) -liquid (water) flow in parallel, that is, in the same direction, and are mixed at the outlets of the oil phase and water phase supply pumps and sent to the enzyme tower.
【０００８】分解する基質によってはポンプの出口にイ
ンラインミキサー等の混合装置を取り付けても良い。希
望する分解率は仕込み時の油脂と水の仕込み比、酵素の
位置選択性（ランダムタイプ、又はα位選択性タイプ）
によって決定できる。高分解率を得るためにはランダム
タイプの固定化酵素を使用し、加水量を増やす必要があ
る。油相、水相の酵素塔への供給は初期の仕込み比で行
うことが望ましい。Depending on the substrate to be decomposed, a mixing device such as an in-line mixer may be attached to the outlet of the pump. Desired decomposition rate is the ratio of oil and water at the time of charging, regioselectivity of enzyme (random type or α-selective type)
Can be determined by In order to obtain a high decomposition rate, it is necessary to use a random type immobilized enzyme and increase the amount of water added. It is desirable to supply the oil phase and the water phase to the enzyme tower at the initial charge ratio.
【０００９】[0009]
【発明の効果】本発明によれば、酵素を損失することな
く、低投資で油脂の加水分解を行える。即ち、従来の脂
肪酸製造設備で使用していた高圧の分解塔や熱媒を発生
させる高圧ボイラーなどの高価な設備を必要とせず、更
にバッチ反応であるため操作が簡単であり、装置の簡略
化を実現できる。生成した脂肪酸は、通常のオレオケミ
カル用原料、食品製造用原料、化粧品原料等として使用
できる。また生成する甘水は酵素や夾雑タンパク等を含
有しないため、濃縮後簡単な精製をすることで通常のグ
リセリンとして使用できる。According to the present invention, fats and oils can be hydrolyzed with low investment without loss of enzyme. That is, it does not require expensive equipment such as a high-pressure decomposition tower or a high-pressure boiler that generates a heat medium used in conventional fatty acid production equipment, and since it is a batch reaction, the operation is simple and the equipment is simplified. Can be realized. The produced fatty acid can be used as a normal raw material for oleochemicals, a raw material for food production, a raw material for cosmetics, and the like. Moreover, since the produced sweet water does not contain an enzyme, a contaminating protein, etc., it can be used as normal glycerin by performing simple purification after concentration.
【００１０】[0010]
【実施例】実施例１
ジャケット付きのステンレス製のカラム２（内径22mm、
充填高さ150mm ）にイオン交換樹脂（Duolite A-568 ダ
イヤモンドシャムロック社製）に市販のリパーゼ（リパ
ーゼＯＦ 名糖産業（株）製）を固定化したリパーゼを
24ｇ充填した。一方、ジャケット付きのガラス容器１
（内径40mm、高さ300mm ）に大豆油160ｇを加えた。反
応温度40℃になるように基質供給槽１、及び酵素塔２の
ジャケットには40℃の温水を循環した。５ｇ／分の流速
でポンプ７を使用して酵素塔に大豆油を送液し、油が戻
しライン３から流出したところで、蒸留水96ｇを基質供
給槽１に加えた。加水量は60重量％（対油相基質）であ
る。この時、水は下層、大豆油は上層にきれいな界面を
形成して分層した。その後、油相抜き出しライン４（内
径3.5mm ）の下端を油相の上端から10mmの所に設置し
た。更に反応液戻りライン３の下端を界面から上方10mm
の位置に取り付けた。この後、基質供給ライン４及び５
を通じて油相をポンプ７、水相をポンプ６でそれぞれ５
ｇ／分、３ｇ／分になるように供給した。この流速は反
応終了時まで維持し、水相を60重量％（対油相）の重量
比となるようにした。戻りライン３から流出する反応液
は戻りラインの下端を出ると油相と水相に分離し、油水
界面を乱すことはなかった。反応の進行に従って油相は
白濁してくるが、これは分解の途中で生成してくるモノ
グリセライドの乳化作用によるものであるが、界面が消
えることはなかった。更に反応が進行すると、モノグリ
セライドも分解され清澄な油相が現れた。サンプルは基
質供給槽１の油相から経時で抜き出し、酸価（ＡＶ）と
ケン価（ＳＶ）を求め、酸価をケン価で除することで分
解率を求めた。最終的に大豆油の分解率は96％に達し
た。更に反応終了直後の油相の水分をカールフィッシャ
ー法で測定したところ0.5 ％であり、良好な油水分離が
出来ていることが確認された。図２に図１に示した循環
静置分離型反応器を用いた際の油相の分解率の経時変化
を示す。Example 1 A stainless steel column 2 with a jacket (inner diameter 22 mm,
A lipase obtained by immobilizing a commercially available lipase (Lipase OF Meitosu Sangyo Co., Ltd.) on an ion exchange resin (Duolite A-568 Diamond Shamrock) at a filling height of 150 mm)
24 g was filled. On the other hand, a glass container with a jacket 1
160 g of soybean oil was added to (inner diameter 40 mm, height 300 mm). Warm water at 40 ° C was circulated in the substrate supply tank 1 and the jacket of the enzyme tower 2 so that the reaction temperature was 40 ° C. Soybean oil was sent to the enzyme tower using the pump 7 at a flow rate of 5 g / min, and when the oil flowed out from the return line 3, 96 g of distilled water was added to the substrate supply tank 1. The amount of water added is 60% by weight (based on the oil phase substrate). At this time, water separated into lower layers and soybean oil into upper layers to form a clean interface. After that, the lower end of the oil phase extraction line 4 (inner diameter 3.5 mm) was installed at a position 10 mm from the upper end of the oil phase. Furthermore, the lower end of the reaction liquid return line 3 is 10 mm above the interface.
It was installed in the position. After this, the substrate supply lines 4 and 5
Pump the oil phase through pump 7 and the water phase through pump 6 through 5
It was supplied at a rate of 3 g / min. This flow rate was maintained until the end of the reaction so that the weight ratio of the aqueous phase was 60% by weight (to the oil phase). When the reaction liquid flowing out from the return line 3 exited the lower end of the return line, it was separated into an oil phase and an aqueous phase and did not disturb the oil-water interface. As the reaction progressed, the oil phase became cloudy. This was due to the emulsifying action of monoglyceride formed during the decomposition, but the interface did not disappear. As the reaction proceeded further, monoglyceride was also decomposed and a clear oil phase appeared. The sample was withdrawn from the oil phase of the substrate supply tank 1 over time, the acid value (AV) and the saponification number (SV) were determined, and the decomposition rate was determined by dividing the acid number by the saponification number. Finally, the decomposition rate of soybean oil reached 96%. Further, the water content of the oil phase immediately after the reaction was measured by the Karl Fischer method, and it was 0.5%, which confirmed that good oil-water separation was achieved. FIG. 2 shows the change over time in the decomposition rate of the oil phase when the circulation stationary separation type reactor shown in FIG. 1 was used.
【図１】 本発明に用いる循環静置分離型反応器を示す
図である。FIG. 1 is a view showing a circulating stationary separation type reactor used in the present invention.
【図２】 循環静置分離型反応器を用いた際の油相の分
解率の経時変化を示すグラフである。FIG. 2 is a graph showing changes over time in the decomposition rate of the oil phase when a circulating static separation type reactor is used.
１ 基質供給槽（油水離槽） ２ 酵素塔 ３ 反応液戻しライン ４ 油相基質抜き出しライン ５ 水相基質抜き出しライン 1 Substrate supply tank (oil water separation tank) 2 enzyme tower 3 Reaction liquid return line 4 Oil phase substrate extraction line 5 Water phase substrate extraction line
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平６−245756（ＪＰ，Ａ) 特開 平３−251168（ＪＰ，Ａ) 米国特許4678580（ＵＳ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C11C 1/04 - 1/06 C12P 7/64 C12N 9/20 C12M 1/40 ＥＵＲＯＰＡＴ（ＱＵＥＳＴＥＬ)─────────────────────────────────────────────────── --- Continuation of the front page (56) References JP-A-6-245756 (JP, A) JP-A-3-251168 (JP, A) US Pat. No. 4678580 (US, A) (58) Fields investigated (Int .Cl. 7 , DB name) C11C 1/04-1/06 C12P 7/64 C12N 9/20 C12M 1/40 EUROPAT (QUESTEL)
Claims (2)
油水分離槽を兼ねた基質供給槽とを用いた油脂の加水分
解方法であって、酵素塔からの反応液の排出部分を基質
供給槽の油相中であって水相との界面付近に設け、酵素
塔と基質供給槽との間で反応液を循環させると共に、基
質供給槽に油水界面を形成させ、油相基質を基質供給槽
の油相の中位部から上方の位置、水相基質を基質供給槽
の底部から夫々抜き出し、油相基質と水相基質とを予め
混合せずに酵素塔へ供給するバッチ式の油脂の加水分解
方法。1. A method for hydrolyzing fats and oils using an enzyme tower (reaction tower) using an immobilized enzyme and a substrate supply tank which also serves as an oil-water separation tank, wherein a portion of the reaction solution discharged from the enzyme tower is discharged. Substrate
A oil phase of the supply tank is provided in the vicinity of the interface between the aqueous phase, together with the circulating reaction solution between the enzyme column and the substrate feed tank, group
The oil-water interface is formed in the quality supply tank, and the oil phase substrate is added to the substrate supply tank.
Position above the middle part of the oil phase, the water phase substrate to the substrate supply tank
Withdrawal respectively from the bottom, batchwise fat method hydrolysis supplied to the enzyme column without prior mixing the oil phase substrate and the aqueous phase substrate.
せる請求項１記載の加水分解方法。 2. An oil phase substrate and an aqueous phase substrate are co-flowed in the same direction.
The method of hydrolysis according to claim 1, wherein
Priority Applications (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33516498A JP3439675B2 (en) | 1998-11-26 | 1998-11-26 | Method of hydrolysis of fats and oils |
| US09/448,140 US6258575B1 (en) | 1998-11-26 | 1999-11-24 | Hydrolyzing fats and oils using an immobilized enzyme column and substrate-feeding chamber that separates phases |
| EP99123232A EP1004662B1 (en) | 1998-11-26 | 1999-11-26 | A process for hydrolyzing fats and oils |
| DE69929740T DE69929740T2 (en) | 1998-11-26 | 1999-11-26 | Process for the hydrolysis of fats and oils |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP33516498A JP3439675B2 (en) | 1998-11-26 | 1998-11-26 | Method of hydrolysis of fats and oils |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000160188A JP2000160188A (en) | 2000-06-13 |
| JP3439675B2 true JP3439675B2 (en) | 2003-08-25 |
Family
ID=18285491
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP33516498A Expired - Fee Related JP3439675B2 (en) | 1998-11-26 | 1998-11-26 | Method of hydrolysis of fats and oils |
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| Country | Link |
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| JP (1) | JP3439675B2 (en) |
Families Citing this family (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4719476B2 (en) * | 2005-02-04 | 2011-07-06 | 花王株式会社 | Fat hydrolysis method |
| US8241875B2 (en) * | 2005-06-21 | 2012-08-14 | Kao Corporation | Method for producing fatty acids with an immobilized enzyme packed column |
| JP5080771B2 (en) * | 2005-10-05 | 2012-11-21 | 花王株式会社 | Method for producing useful substance using immobilized enzyme |
| KR101294474B1 (en) | 2005-10-05 | 2013-08-07 | 카오카부시키가이샤 | Method for producing a useful substance by use of an immobilized enzyme |
| JP4694938B2 (en) * | 2005-10-06 | 2011-06-08 | 花王株式会社 | Method for producing fatty acids |
| JP4694939B2 (en) * | 2005-10-06 | 2011-06-08 | 花王株式会社 | Method for producing fatty acids |
| JP4915732B2 (en) | 2006-12-15 | 2012-04-11 | 花王株式会社 | Method for producing useful substance using immobilized enzyme |
| JP5080797B2 (en) * | 2006-12-15 | 2012-11-21 | 花王株式会社 | Method for producing useful substance using immobilized enzyme |
| JP5080828B2 (en) * | 2007-03-07 | 2012-11-21 | 花王株式会社 | Method for producing useful substance using immobilized enzyme |
| KR20090097870A (en) | 2006-12-15 | 2009-09-16 | 카오카부시키가이샤 | Process for producing useful substance with immobilized enzyme |
| JP2011078328A (en) * | 2009-10-05 | 2011-04-21 | Kao Corp | Method for producing unsaturated fatty acids |
| CN101829528B (en) * | 2010-05-07 | 2011-12-28 | 清华大学 | Hydrolysis tower for oil and fat hydrolysis and method for oil hydrolysis by using same |
| JP6990076B2 (en) * | 2017-09-20 | 2022-02-03 | 花王株式会社 | Method for producing fatty acids |
| CN113684126B (en) * | 2021-10-26 | 2022-02-15 | 华南理工大学 | Device and method for continuously synthesizing diglyceride by holoenzyme method in multi-liquid-phase system |
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1998
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