JPH0350571B2 - - Google Patents
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- Publication number
- JPH0350571B2 JPH0350571B2 JP58098052A JP9805283A JPH0350571B2 JP H0350571 B2 JPH0350571 B2 JP H0350571B2 JP 58098052 A JP58098052 A JP 58098052A JP 9805283 A JP9805283 A JP 9805283A JP H0350571 B2 JPH0350571 B2 JP H0350571B2
- Authority
- JP
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- Prior art keywords
- molecular
- organic substances
- inorganic salts
- reverse osmosis
- low
- 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 - Lifetime
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- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】
本発明は低脱塩率の逆浸透膜を用いる加圧透過
処理によつて、分子量1000〜5000の高分子有機物
と分子量200以下の低分子有機物と無機塩類との
混合溶液から前記高分子有機物を選択的に分離す
る方法に関するものである。
近年において発酵工業、製薬工業、製糖工業な
どで分子量1000〜5000の高分子有機物たとえば糖
類、抗生物質、ビタミン類、着色物質と、分子量
200以下の低分子有機物たとえばアミノ酸類と無
機塩類との混合溶液から、前記高分子有機物を選
択的に分離する必要性が生じているが、このよう
な場合、従来では前記高分子有機物を選択的に吸
着することのできる吸着材あるいは逆に前記高分
子有機物を吸着しないで、低分子有機物および無
機塩類を選択的に吸着できる吸着材を用いて分離
することが行なわれている。しかしながらこのよ
うな吸着材を用いる方法は、その分離に適した吸
着材を選定することがむずかしく、また吸着材を
選定し得ても吸着材の劣化が著しいことや、処理
操作が煩雑であつたり、あるいは余分な廃液等が
生じるなどの欠点を有している。
一方従来から有機物と無機塩類の分離に超濾過
膜を用いる加圧透過方法が採用されているが、超
濾過膜は前記高分子有機物よりもつと分子量の大
きいたとえば分子量が10000以上の乳タンパクや
アルブミンなどの分離には適しているが、分子量
が1000〜5000ぐらいの前記高分子有機物の分離に
は適していない。すなわちこの程度の分子量であ
ると、超濾過膜で阻止することができず、前記高
分子有機物が共存する低分子有機物および無機塩
類と共に超濾過膜を通過してしまい、前記高分子
有機物の回収率が大巾に低下してしまう。
本発明はこの点に鑑みてなされたもので、分子
量1000〜5000の高分子有機物と分子量200以下の
低分子有機物と無機塩類との混合溶液から当該高
分子有機物を膜により選択的に分離することを目
的とするもので、当該混合溶液を循環槽を介して
1000〜1500ppmのNaCl溶液中のNaClの排除率が
50％以下の特性を有する逆浸透膜を挿着した透過
装置に加圧下で供給し、無機塩類と低分子有機物
を含む透過水を系外に排出するとともに、高分子
有機物を含む非透過水を循環槽に循環し、かつ循
環系統に系外から水を加える操作を介在させて透
過処理することを特徴とする逆浸透膜による高分
子有機物の分離方法である。
以下に本発明を詳細に説明する。
本発明の第１の特徴とするところは高分子有機
物を低分子有機物と無機塩類から分離するにあた
り、従来の超濾過膜にかえて逆浸透膜を用いる点
である。
逆浸透膜は海水の淡水化や工業用水の脱塩など
の無機イオンの分離に従来から用いられており、
超濾過膜と相違し、膜面に物理的な孔が存在して
ないと云われ、当該膜による無機イオンと水の分
離機構は水の逆浸透作用によるものとされてい
る。
すなわち逆浸透膜を介して無機塩類の溶液側
に、当該無機塩類濃度における浸透圧以上の圧力
をかけて水を逆浸透させるものである。
したがつて処理対象となる溶液の塩類濃度が濃
くなる程操作圧力は必然的高くなる。
ところで従来から前記脱塩の目的で用いられる
逆浸透膜は、1000〜1500ppmのNaCl溶液中の
NaClを95〜98％排除する特性（以下脱塩率とい
う）を有するのが普通であるが、最近になつて脱
塩率が95％以下の各種の低脱塩率の逆浸透膜が出
現するようになつてきた。
このような低脱塩率の逆浸透膜はその脱塩率が
低下すればする程、無機塩類が多量に透過し、そ
れに伴ない低分子有機物も透過するようになる。
本発明者等は低脱塩率である各種の逆浸透膜か
ら分子量1000〜5000の高分子有機物を透過せずに
分子量200以下の低分子有機物および無機塩類を
透過するような逆浸透膜を各種の実験により選定
したところ、脱塩率50％以下の逆浸透膜であれば
前記目的に合致することを見い出した。
しかし当該逆浸透膜を用いるとしても、両有機
物と無機塩類の混合溶液を一過性で処理しても所
期の目的を達し得ない。というのはたとえば脱塩
率50％の逆浸透膜を用いた場合、無機塩類のみに
注目すると一過性の透過処理の場合は混合溶液中
の50％の無機塩類は排除し得るが、のこりの50％
は残留することになる。
したがつて循環槽に混合溶液を張り込み、当該
混合溶液を前記低脱塩率の逆浸透膜を挿着した透
過装置に加圧下で供給し、無機塩類と低分子有機
物を含む透過液を系外に排出するとともに、高分
子有機物と残留する無機塩類および低分子有機物
を含む非透過液を循環槽にもどして、非透過液を
循環しながら無機塩類と低分子有機物を段階的に
透過させるという循環透過処理を行なう必要があ
る。
しかしながらこのような循環処理を続行してい
くと、循環液中の無機塩類および低分子有機物が
透過液側へ透過するとともに水分も透過液側へ透
過するので、このため循環液中の無機塩類に注目
するとその絶対量は低下するもののそれ以上に液
溶量が低下するため循環液側、換言すれば非透過
液側の無機塩類濃度がしだいに増加するという現
象を生ずる。このように循環液側の無機塩類濃度
が増加すると、その浸透圧も比例的に増加し、そ
の浸透圧に打勝つだけの逆浸透圧をかけねば透過
処理ができなくなり、遂には当該操作圧力が膜の
物理的強度を陵駕し、透過処理の続行が不可能と
なつてしまう。
本発明はここにおいて循環系統、たとえば循環
槽に系外から水を加えて循環液側の液を希釈して
透過処理を続行することを第２の特徴とするもの
である。
このように循環液を希釈することにより循環液
中の無機塩類の濃度を低下せしめることができ、
その濃度の低下に伴ない浸透圧も低下するので、
比較的低圧力下でも透過処理を続行することが可
能となる。
本発明においては濃縮すべき液側へ系外から水
を加えてその液を希釈するので、濃縮操作におい
ては不経済のように思えるが、本手段によつて透
過処理の続行が可能となり、高分子有機物の濃縮
液を得るという所期の目的を達成することができ
る。なお加えた水は透過処理中に無機塩類および
低分子有機物とともに極めて容易に透過液側へ透
過するので、高分子有機物の濃縮液を得るという
目的を阻害することもない。また本発明において
は希釈水を加えて循環する操作を長時間行なう
程、得られる高分子有機物の濃縮液の純度が上昇
するので、当該操作の続行は高分子有機物の濃縮
液の希望する純度によつて任意に行なえばよい。
次に本発明に用いる逆浸透膜について説明す
る。
前述したように本発明においては、従来脱塩の
目的で用いられている逆浸透膜より脱塩率の小さ
い逆浸透膜を用い、脱塩率が50％以下の逆浸透膜
を用いる。
脱塩率が50％以上の逆浸透膜では特に高分子有
機物と低分子有機物の分離が不充分となつて好ま
しくない。
本発明の用途に適した低脱塩率の逆浸透膜の一
例を挙げると、デサリネーシヨン社製Ｇ−５、Ｇ
−20、Ｇ−50（いずれも商品名）、日東電工(株)製
NTR−7250、NTR−1530、NTR−1510（いずれ
も商品名）、住友化学(株)製ソルコンSC−5000、ソ
ルコンSC−8000（いずれも商品名）、ダイセル工
業(株)製DRS−50、DRS−10（いずれも商品名）な
どがあり、これらの逆浸透膜はいずれも脱塩率が
50％以下のものであり、その材質はスルホン化ポ
リスルホン、ポリビニールアルコール、酢酸セル
ローズ等であり、被処理対象有機物の分子量ある
いは種類によつて最適のものを選択するとよい。
以下に本発明の実施例態様を図面に従つて説明
する。
図面は本発明の実施例態様の一例を示すフロー
の説明図であり、１は循環槽、２はポンプ、３は
低脱塩率の逆浸透膜を挿着した透過装置である。
本発明のひとつの操作法として循環槽１に高分
子有機物と低分子有機物と無機塩類との混合溶液
を受け入れ、ポンプ２を用いてそのまま透過処理
を行なう。なお透過圧力は当該混合液の濃度によ
つて相違するが、通常10〜50Kg／cm2にて行なう。
このような透過処理により混合液中の無機塩類
と低分子有機物の一部と水分が透過液Ａ側に透過
し、高分子有機物と残留塩類および残留低分子有
機物を含む非透過液Ｂを循環槽１に循環する。循
環透過処理を続行していくと、透過液側Ａに透過
した水量だけ循環槽１内の液面が低下することと
なり、これに伴ない循環する非透過液Ｂ側の無機
塩類の濃度も増加し、浸透圧が増大する。したが
つて一定流量の透過液を得ようとすればその操作
圧力を高める必要が生じてくる。このような状態
に至つたら、循環槽１内に透過液Ａの流量に相当
する流量の脱塩水あるいは水道水などの水Ｃを流
入しながら前記循環処理を行なう。このような操
作により循環槽１内の無機塩類濃度が増加するこ
とがないので、当初の透過圧力にほぼ近い透過圧
力で透過処理を続行することができる。また処理
の続行により、循環槽１内に滞留する溶液の無機
塩類と低分子有機物の含有量がしだいに低下する
ので、希望とする純度になつた点で水Ｃの流入を
中断するとともに透過処理を終了するとよい。あ
るいは水Ｃの流入を中断したままで透過液流量が
ある程度低下する点まで循環透過処理を続行して
もよい。また他の操作法として透過装置により循
環槽１内の液面が低下した時点で水Ｃを流入して
循環槽１内の液面をもとのレベルに復帰させ、循
環透過処理を続行するというように、水Ｃを加え
る操作を段階的に行なつてもよく、あるいは当初
から水Ｃを加えながら循環透過処理を行なつても
よい。さらに水Ｃを加える位置としては循環槽１
にかぎらず非透過液が循環する循環系統であれば
どの位置でもさしつかえない。
以上説明したように本発明によつて高分子有機
物と低分子有機物と無機塩類との混合溶液から、
回収率を低下させることなく高濃度でかつ高純度
の高分子有機物を回収することができるので、発
酵工業、製糖工業あるいは製薬工業等に裨益する
ところが大きい。
以下に本発明の効果をより明確にするために実
施例を説明する。
実施例
分子量1295を主体とする着色物質が0.5％、分
子量147のアミノ酸が0.3％、食塩が0.5％である
混合溶液を、脱塩率20％の住友電工(株)製チユーブ
ラ型逆浸透膜ソルコンSC−8000（商品名）を１本
装着した透過装置で本発明の方法によつて処理し
た。すなわち前記混合溶液１m3を循環槽に受け、
圧力50Kg／cm2、温度15℃、初期透過流量150／
Ｈで透過処理し、濃縮度３すなわち着色物質濃度
が３倍となつた時点で脱塩水を200／Ｈで循環
槽に補給しながら透過処理を行ない、累計脱塩水
補給量が１m3となつた点で脱塩水の補給を止めて
循環槽内の液を15倍濃縮した。一方比較のために
循環槽に脱塩水を全く加えない循環透過処理も行
ない、その結果も第一表に示した。第一表に見ら
れるごとく脱塩水を加えない場合は６〜７倍濃縮
までしかできずかつ濃縮液中のアミノ酸量も大き
かつた。
【表】Detailed Description of the Invention The present invention is a method for mixing high molecular weight organic substances with a molecular weight of 1000 to 5000, low molecular weight organic substances with a molecular weight of 200 or less, and inorganic salts by pressure permeation treatment using a reverse osmosis membrane with a low salt removal rate. The present invention relates to a method for selectively separating the polymeric organic substance from a solution. In recent years, in the fermentation industry, pharmaceutical industry, sugar refining industry, etc., high molecular weight organic substances with a molecular weight of 1000 to 5000, such as sugars, antibiotics, vitamins, coloring substances, and
There is a need to selectively separate the high molecular weight organic matter from a mixed solution of low molecular weight organic matter of 200 or less, such as amino acids and inorganic salts. Separation has been carried out using an adsorbent that can adsorb low-molecular organic substances and inorganic salts, or conversely, an adsorbent that can selectively adsorb low-molecular organic substances and inorganic salts without adsorbing the high-molecular organic substances. However, with methods using such adsorbents, it is difficult to select an adsorbent suitable for the separation, and even if an adsorbent is selected, the deterioration of the adsorbent is significant and the processing operations are complicated. However, it also has drawbacks such as the generation of excess waste liquid. On the other hand, a pressurized permeation method using an ultrafiltration membrane has conventionally been used to separate organic substances and inorganic salts, but the ultrafiltration membrane is used to filter proteins with larger molecular weights than the above-mentioned high-molecular organic substances, such as milk proteins and albumins with a molecular weight of 10,000 or more. However, it is not suitable for separating the above-mentioned high-molecular organic substances having a molecular weight of about 1,000 to 5,000. In other words, if the molecular weight is at this level, it cannot be blocked by the ultra-filtration membrane, and the high-molecular organic substance passes through the ultra-filtration membrane together with the coexisting low-molecular organic substances and inorganic salts, resulting in a decrease in the recovery rate of the high-molecular organic substance. is drastically reduced. The present invention has been made in view of this point, and is to selectively separate a high molecular weight organic substance using a membrane from a mixed solution of a high molecular weight organic substance having a molecular weight of 1000 to 5000, a low molecular weight organic substance having a molecular weight of 200 or less, and inorganic salts. The purpose is to pass the mixed solution through a circulation tank.
The rejection rate of NaCl in 1000-1500 ppm NaCl solution is
The water is supplied under pressure to a permeation device equipped with a reverse osmosis membrane with a property of 50% or less, and the permeated water containing inorganic salts and low-molecular organic matter is discharged from the system, while the non-permeated water containing high-molecular organic matter is discharged from the system. This is a method for separating high-molecular organic substances using a reverse osmosis membrane, which is characterized in that permeation treatment is performed by circulating water in a circulation tank and adding water from outside the circulation system. The present invention will be explained in detail below. The first feature of the present invention is that a reverse osmosis membrane is used in place of a conventional ultrafiltration membrane to separate high-molecular organic substances from low-molecular organic substances and inorganic salts. Reverse osmosis membranes have traditionally been used to separate inorganic ions in desalination of seawater and desalination of industrial water.
Unlike ultrafiltration membranes, it is said that there are no physical pores on the membrane surface, and the separation mechanism of inorganic ions and water by the membrane is said to be based on the reverse osmosis effect of water. That is, a pressure higher than the osmotic pressure at the inorganic salt concentration is applied to the inorganic salt solution side through the reverse osmosis membrane to reverse osmosis of water. Therefore, the higher the salt concentration of the solution to be treated, the higher the operating pressure necessarily becomes. By the way, reverse osmosis membranes conventionally used for the purpose of desalination are
Normally, it has the property of eliminating 95 to 98% of NaCl (hereinafter referred to as salt removal rate), but recently various low salt removal rate reverse osmosis membranes with a salt removal rate of 95% or less have appeared. It has become like that. The lower the salt removal rate of such a reverse osmosis membrane is, the more inorganic salts permeate through it, and the more low-molecular organic substances permeate therethrough. The present inventors have developed various types of reverse osmosis membranes that allow low molecular weight organic substances and inorganic salts with a molecular weight of 200 or less to pass through, while not allowing high molecular weight organic substances with a molecular weight of 1000 to 5000 to pass through. As a result of the selection conducted through experiments, it was found that a reverse osmosis membrane with a salt removal rate of 50% or less would meet the above objective. However, even if the reverse osmosis membrane is used, the intended purpose cannot be achieved even if a mixed solution of both organic substances and inorganic salts is treated temporarily. For example, when using a reverse osmosis membrane with a desalination rate of 50% and focusing only on inorganic salts, transient permeation treatment can eliminate 50% of the inorganic salts in the mixed solution, but the remaining 50%
will remain. Therefore, a mixed solution is filled in a circulation tank, and the mixed solution is supplied under pressure to a permeation device equipped with the above-mentioned reverse osmosis membrane with a low salt removal rate, and the permeate containing inorganic salts and low-molecular organic substances is removed from the system. In this cycle, the non-permeate liquid containing high-molecular organic substances and remaining inorganic salts and low-molecular-weight organic substances is returned to the circulation tank, and the inorganic salts and low-molecular organic substances are permeated in stages while the non-permeate liquid is circulated. It is necessary to perform transparent processing. However, as this circulation process continues, inorganic salts and low-molecular-weight organic substances in the circulating fluid permeate to the permeate side, and water also permeates to the permeate side. It is noted that although the absolute amount decreases, the amount of the solution decreases more than that, resulting in a phenomenon in which the concentration of inorganic salts on the circulating fluid side, in other words, on the non-permeated fluid side gradually increases. When the concentration of inorganic salts on the circulating fluid side increases in this way, the osmotic pressure also increases proportionally, and unless a reverse osmotic pressure is applied that is sufficient to overcome the osmotic pressure, permeation treatment cannot be performed, and eventually the operating pressure increases. This impairs the physical strength of the membrane, making it impossible to continue permeation treatment. The second feature of the present invention is that water is added to the circulation system, for example, a circulation tank, from outside the system to dilute the liquid on the circulating liquid side and continue the permeation treatment. By diluting the circulating fluid in this way, the concentration of inorganic salts in the circulating fluid can be reduced,
As the concentration decreases, the osmotic pressure also decreases,
It becomes possible to continue permeation treatment even under relatively low pressure. In the present invention, water is added from outside the system to the liquid to be concentrated to dilute the liquid, which may seem uneconomical in the concentration operation, but this method makes it possible to continue the permeation treatment, resulting in high The intended purpose of obtaining a concentrated solution of molecular organic substances can be achieved. Note that the added water very easily permeates into the permeate side together with inorganic salts and low-molecular-weight organic substances during permeation treatment, so that it does not impede the purpose of obtaining a concentrated liquid of high-molecular-weight organic substances. In addition, in the present invention, the longer the operation of adding and circulating dilution water is performed, the higher the purity of the obtained concentrated solution of polymeric organic matter increases. Therefore, you can do it as you like. Next, the reverse osmosis membrane used in the present invention will be explained. As mentioned above, in the present invention, a reverse osmosis membrane with a salt removal rate lower than that of reverse osmosis membranes conventionally used for the purpose of desalination is used, and a reverse osmosis membrane with a salt removal rate of 50% or less is used. A reverse osmosis membrane with a desalination rate of 50% or more is not preferable because the separation of high-molecular organic substances and low-molecular organic substances is particularly insufficient. Examples of reverse osmosis membranes with low salt removal rates suitable for use in the present invention include G-5 and G
-20, G-50 (all product names), manufactured by Nitto Denko Corporation
NTR-7250, NTR-1530, NTR-1510 (all trade names), Sumitomo Chemical Co., Ltd. Solcon SC-5000, Solcon SC-8000 (all trade names), Daicel Industries Co., Ltd. DRS-50, DRS-10 (all product names), and all of these reverse osmosis membranes have a low salt removal rate.
50% or less, and the material is sulfonated polysulfone, polyvinyl alcohol, cellulose acetate, etc., and the optimal one should be selected depending on the molecular weight or type of the organic substance to be treated. Embodiments of the present invention will be described below with reference to the drawings. The drawing is a flow explanatory diagram showing an example of an embodiment of the present invention, in which 1 is a circulation tank, 2 is a pump, and 3 is a permeation device in which a reverse osmosis membrane with a low salt removal rate is inserted. As one method of operation of the present invention, a mixed solution of a high molecular organic substance, a low molecular organic substance, and an inorganic salt is received in the circulation tank 1, and the pump 2 is used to directly perform permeation treatment. Although the permeation pressure varies depending on the concentration of the mixed liquid, it is usually 10 to 50 kg/cm 2 . Through this permeation treatment, the inorganic salts, part of the low-molecular-weight organic matter, and water in the mixed liquid permeate to the permeated liquid A side, and the non-permeated liquid B containing the high-molecular organic substances, residual salts, and residual low-molecular-weight organic substances is sent to the circulation tank. Cycles to 1. As the circulating permeation treatment continues, the liquid level in the circulation tank 1 will decrease by the amount of water that has permeated into the permeated liquid side A, and the concentration of inorganic salts in the circulating non-permeated liquid B side will also increase accordingly. and the osmotic pressure increases. Therefore, in order to obtain a constant flow rate of permeate, it becomes necessary to increase the operating pressure. When such a state is reached, the circulation process is performed while flowing water C such as demineralized water or tap water into the circulation tank 1 at a flow rate corresponding to the flow rate of the permeated liquid A. Since the concentration of inorganic salts in the circulation tank 1 does not increase due to such an operation, the permeation treatment can be continued at a permeation pressure substantially close to the initial permeation pressure. In addition, as the treatment continues, the content of inorganic salts and low-molecular organic substances in the solution remaining in the circulation tank 1 gradually decreases, so when the desired purity is reached, the inflow of water C is stopped and the permeation treatment is carried out. It is a good idea to end it. Alternatively, the circulation permeation treatment may be continued until the permeate flow rate decreases to some extent while the inflow of water C is interrupted. Another operation method is to introduce water C when the liquid level in the circulation tank 1 is lowered by the permeation device to return the liquid level in the circulation tank 1 to the original level and continue the circulation permeation treatment. As shown, the operation of adding water C may be performed in stages, or the circulating permeation treatment may be performed while adding water C from the beginning. The location where water C is added is circulation tank 1.
Any position in the circulation system where the non-permeated liquid circulates may be used. As explained above, according to the present invention, from a mixed solution of high-molecular organic substances, low-molecular organic substances, and inorganic salts,
Since high-concentration and high-purity polymeric organic substances can be recovered without reducing the recovery rate, the fermentation industry, sugar manufacturing industry, pharmaceutical industry, etc. can greatly benefit from this method. Examples will be described below to make the effects of the present invention more clear. Example A mixed solution containing 0.5% of a colored substance with a molecular weight of 1295 as the main component, 0.3% of an amino acid with a molecular weight of 147, and 0.5% of common salt was transferred to a tubular type reverse osmosis membrane solcon manufactured by Sumitomo Electric Industries, Ltd. with a desalination rate of 20%. Treatment was carried out by the method of the present invention using a permeation device equipped with one SC-8000 (trade name). That is, 1 m 3 of the mixed solution is received in a circulation tank,
Pressure 50Kg/cm 2 , temperature 15℃, initial permeation flow rate 150/
When the concentration level reached 3, that is, the concentration of colored substances tripled, the permeation treatment was carried out while replenishing the circulation tank with desalinated water at 200/H, and the total amount of desalinated water replenished was 1 m3 . At this point, the supply of desalinated water was stopped and the liquid in the circulation tank was concentrated 15 times. On the other hand, for comparison, a circulation permeation treatment was also carried out in which no demineralized water was added to the circulation tank, and the results are also shown in Table 1. As shown in Table 1, when demineralized water was not added, it was only possible to concentrate up to 6 to 7 times, and the amount of amino acids in the concentrate was also large. 【table】
図面は本発明の実施態様の一例を示すフローの
説明図であり、１は循環槽、２はポンプ、３は透
過装置、Ａは透過液、Ｂは非透過液を、Ｃは水を
示す。
The drawing is an explanatory diagram of a flow showing an example of an embodiment of the present invention, in which 1 is a circulation tank, 2 is a pump, 3 is a permeation device, A is a permeated liquid, B is a non-permeated liquid, and C is water.
Claims (1)
200以下の低分子有機物と無機塩類との混合溶液
から当該高分子有機物を選択的に分離するにあた
り、当該混合溶液を循環槽を介して1000〜
1500ppmのNaCl溶液中のNaClの排除率が50％以
下の特性を有する逆浸透膜を挿着した透過装置に
加圧下で供給し、無機塩類と低分子有機物を含む
透過水を系外に排出するとともに、高分子有機物
を含む非透過水を循環槽に循環し、かつ循環系統
に系外から水を加える操作を介在させて透過処理
することを特徴とする逆浸透膜による高分子有機
物の分離方法。1 High-molecular organic substances and molecular weights with a molecular weight of 1000 to 5000
In selectively separating the high-molecular organic substance from a mixed solution of low-molecular-weight organic substances of 200 or less and inorganic salts, the mixed solution is passed through a circulation tank to
The solution is supplied under pressure to a permeation device equipped with a reverse osmosis membrane that has a characteristic that the rejection rate of NaCl in a 1500 ppm NaCl solution is 50% or less, and the permeated water containing inorganic salts and low-molecular organic matter is discharged from the system. In addition, a method for separating polymeric organic substances using a reverse osmosis membrane, characterized in that non-permeated water containing polymeric organic substances is circulated to a circulation tank, and permeation treatment is performed by intervening an operation of adding water to the circulation system from outside the system. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9805283A JPS6084108A (en) | 1983-06-03 | 1983-06-03 | Separation of high-molecular organic substance by reverse osmosis membrane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9805283A JPS6084108A (en) | 1983-06-03 | 1983-06-03 | Separation of high-molecular organic substance by reverse osmosis membrane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6084108A JPS6084108A (en) | 1985-05-13 |
| JPH0350571B2 true JPH0350571B2 (en) | 1991-08-02 |
Family
ID=14209459
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP9805283A Granted JPS6084108A (en) | 1983-06-03 | 1983-06-03 | Separation of high-molecular organic substance by reverse osmosis membrane |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6084108A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0763590B2 (en) * | 1985-03-28 | 1995-07-12 | 日東電工株式会社 | How to remove colored components |
| JP4678831B2 (en) * | 2004-03-30 | 2011-04-27 | 三井製糖株式会社 | Process for treating waste liquid from sugarmaking waste, sugar production liquid, or fermentation process of sugar production |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS54113498A (en) * | 1978-02-21 | 1979-09-05 | Nitto Electric Ind Co Ltd | Preparation of low salt soy |
| JPS55128000A (en) * | 1979-03-27 | 1980-10-03 | Nitto Electric Ind Co | Treating of broth |
| US4390342A (en) * | 1980-04-01 | 1983-06-28 | Ciba-Geigy Corporation | Process for the preparation of solid composition of water-soluble dyes |
| JPS5851874A (en) * | 1981-09-24 | 1983-03-26 | Nitto Electric Ind Co Ltd | Concentration of stickwater |
-
1983
- 1983-06-03 JP JP9805283A patent/JPS6084108A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6084108A (en) | 1985-05-13 |
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