JPS63111905A - Membrane separator - Google Patents
Membrane separatorInfo
- Publication number
- JPS63111905A JPS63111905A JP25663386A JP25663386A JPS63111905A JP S63111905 A JPS63111905 A JP S63111905A JP 25663386 A JP25663386 A JP 25663386A JP 25663386 A JP25663386 A JP 25663386A JP S63111905 A JPS63111905 A JP S63111905A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- treated
- tank
- solvent
- membrane module
- 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
- 239000012528 membrane Substances 0.000 title claims abstract description 56
- 239000007788 liquid Substances 0.000 claims abstract description 123
- 239000002904 solvent Substances 0.000 claims abstract description 33
- 238000000926 separation method Methods 0.000 claims description 19
- 238000007865 diluting Methods 0.000 claims description 7
- 239000004382 Amylase Substances 0.000 abstract description 5
- 102000013142 Amylases Human genes 0.000 abstract description 5
- 108010065511 Amylases Proteins 0.000 abstract description 5
- 235000019418 amylase Nutrition 0.000 abstract description 5
- 238000010790 dilution Methods 0.000 abstract description 2
- 239000012895 dilution Substances 0.000 abstract description 2
- 230000005587 bubbling Effects 0.000 abstract 4
- 241000894006 Bacteria Species 0.000 abstract 1
- 238000000034 method Methods 0.000 description 15
- 238000005187 foaming Methods 0.000 description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000000243 solution Substances 0.000 description 7
- 238000011026 diafiltration Methods 0.000 description 6
- 239000012466 permeate Substances 0.000 description 6
- 238000001914 filtration Methods 0.000 description 4
- 108091005804 Peptidases Proteins 0.000 description 3
- 239000004365 Protease Substances 0.000 description 3
- 102100037486 Reverse transcriptase/ribonuclease H Human genes 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000003085 diluting agent Substances 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- 230000004151 fermentation Effects 0.000 description 3
- 238000011282 treatment Methods 0.000 description 3
- 102000004190 Enzymes Human genes 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000012510 hollow fiber Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000013076 target substance Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 239000003242 anti bacterial agent Substances 0.000 description 1
- 229940088710 antibiotic agent Drugs 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000011550 stock solution Substances 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
［産業上の利用分野］
本発明は膜分離装置に係り、特に被処理液に溶媒を加え
ながら膜分離を行い、目的とする物質を分離・精製する
方法（ダイアフィルトレージョン法）により処理を行う
際に、発泡性の被処理液であっても被処理液タンクでの
発泡を抑え、良好な溶媒の注入が行なえる、改良された
膜分離装置に関する。Detailed Description of the Invention [Industrial Application Field] The present invention relates to a membrane separation device, and in particular a method (diafiltration method) for separating and purifying a target substance by performing membrane separation while adding a solvent to a liquid to be treated. The present invention relates to an improved membrane separation device that suppresses foaming in a tank of a liquid to be treated and enables good solvent injection even when the liquid to be treated is foamable when treated by the tresion method.
［従来の技術］
被処理液を溶媒（主として水）で希釈しながら、あるい
は、予め希釈しておいて、膜分離を行うことにより、目
的とする物質を濃縮液側又は透過液側に分離・精製する
方法がダイアフィルトレージョン法として従来より知ら
れている。ダイアフィルトレージョン法には、第２図に
示すようなフローが用いられている。[Prior art] By diluting the liquid to be treated with a solvent (mainly water) or diluting it in advance and performing membrane separation, the target substance can be separated into the concentrated liquid side or the permeated liquid side. The purification method is conventionally known as the diafiltration method. The diafiltration method uses a flow as shown in FIG.
第２図に示す装置は回分式のものであって、被処理液タ
ンク２０内の被処理液はポンプ２１により併給配管２２
を経て膜モジュール２３に送給され、透過液は配管２４
より排出され、濃縮液は配管２５より被処理液タンク２
０に返送されるように構成されている。しかして、被処
理液タンク２０の液面レベル２０ａを一定に保つように
、溶媒をバルブ２６を有する配管２７より被処理液タン
ク２０に加える。従って、この加える溶媒の量は膜モジ
ュール２３より排出される透過液量に等しい量となる。The apparatus shown in FIG. 2 is of a batch type, and the liquid to be treated in the liquid to be treated tank 20 is pumped through a simultaneous supply pipe 22 by a pump 21.
The permeate is sent to the membrane module 23 through the pipe 24.
The concentrated liquid is discharged from the pipe 25 to the liquid to be treated tank 2.
It is configured to return to 0. Then, the solvent is added to the liquid to be treated tank 20 through the pipe 27 having the valve 26 so as to keep the liquid level 20a of the liquid to be treated tank 20 constant. Therefore, the amount of solvent added is equal to the amount of permeate discharged from the membrane module 23.
図中、２９は熱交換器である。In the figure, 29 is a heat exchanger.
従来、被処理液タンク２０への溶媒供給量の制御は、第
２図に示す如く、被処理液タンク２０に設置した液面調
節器２８等により、溶媒供給配管２７のバルブ２６の開
閉により、あるいは、溶媒供給ポンプ（図示せず）の起
動、停止により行っている。Conventionally, the amount of solvent supplied to the liquid to be treated tank 20 has been controlled by opening and closing the valve 26 of the solvent supply piping 27 using a liquid level regulator 28 or the like installed in the liquid to be treated tank 20, as shown in FIG. Alternatively, this is carried out by starting and stopping a solvent supply pump (not shown).
［発明が解決しようとする問題点］
このような従来の装置では、一般にダイアフィルトレー
ジョン法の対象となる被処理液（原液）は、高濃度の有
機物溶液である場合が多く、このような溶液は被処理液
タンクの中で発泡し易いことから、液面調節器でのコン
トロールが困難になったり、定量的な供給ができなくな
る。また、泡が被処理液タンク上部から流出したりする
などの問題もある。[Problems to be solved by the invention] In such conventional devices, the liquid to be treated (undiluted solution) that is generally subjected to the diafiltration method is often a highly concentrated organic solution; Since the solution tends to foam in the tank of the liquid to be treated, it becomes difficult to control it with a liquid level regulator and it becomes impossible to supply it quantitatively. Further, there are also problems such as bubbles flowing out from the upper part of the liquid to be treated tank.
［問題点を解決するための手段］
本発明は上記従来の問題点を解決し、発泡性の被処理液
でも被処理液タンクでの発泡を抑えて、効率的に処理す
ることができる膜分離装置を提供するものである。[Means for Solving the Problems] The present invention solves the above-mentioned conventional problems and provides a membrane separation system that can efficiently process even foaming liquids by suppressing foaming in the liquid tank. It provides equipment.
本発明の膜分離装置は、
ａ、被処理液タンクと、
ｂ、被処理液を濃縮液と透過液とに分離する膜モジュー
ルと、
Ｃ８被処理液タンクから膜モジュールへ？ｌＳ理液を供
給する供給管路及び供給ポンプと、ｄ、被処理液を希釈
する溶媒の供給手段と、ｅ、濃縮液を前記被処理液タン
クへ返送する返送管路と、
を備えてなる膜分離装置において、
前記返送管路と供給ポンプ入口側の供給管路とを連絡す
る連絡管路を設けたものである。The membrane separation device of the present invention includes: a) a liquid to be treated tank; b) a membrane module that separates the liquid to be treated into a concentrated liquid and a permeate; and from the C8 liquid to be treated tank to the membrane module? A supply pipe and a supply pump for supplying the IS physical solution; d. A means for supplying a solvent for diluting the liquid to be treated; and e. A return pipe for returning the concentrated liquid to the liquid to be treated tank. The membrane separator is provided with a connecting pipe that connects the return pipe with the supply pipe on the inlet side of the supply pump.
［作用］
本発明の膜分離装置は、膜モジュールからの濃縮液を被
処理液タンクへ返送する返送管路と、被処理液タンクか
ら膜モジュールへ被処理液を供給する供給管路の供給ポ
ンプ入口側の管路とを連絡する連絡管路を有するため、
膜モジュールの濃縮液の少なくとも一部を被処理液タン
クに返送することなく膜モジュールに循環させることが
できる。[Function] The membrane separation device of the present invention includes a return pipeline that returns the concentrated liquid from the membrane module to the liquid to be treated tank, and a supply pump for the supply line that supplies the liquid to be treated from the liquid to be treated tank to the membrane module. Because it has a connecting pipe that connects with the pipe on the inlet side,
At least a portion of the concentrated liquid in the membrane module can be circulated through the membrane module without being returned to the liquid to be treated tank.
このため、返送される濃縮液と被処理液タンク内の被処
理液とが強くぶつかりあうことがなく、発泡性の被処理
液であっても、被処理液タンク内の発泡が防止され、発
泡の非常に少ない状態で、希釈溶媒の供給及び供給制御
を行うことができる。Therefore, the returned concentrated liquid and the liquid to be treated in the liquid to be treated tank do not collide strongly, and even if the liquid to be treated is foaming, it is prevented from foaming in the liquid to be treated tank. The supply and supply control of the diluting solvent can be performed with very little amount of diluent.
［実施例コ 以下に図面を参照して本発明の詳細な説明する。[Example code] The present invention will be described in detail below with reference to the drawings.
第１図は本発明の膜分離装置の一実施例を示す系統図で
ある。FIG. 1 is a system diagram showing an embodiment of the membrane separation apparatus of the present invention.
第１図に示す如く、本発明の膜分離装置は、被処理液タ
ンク１、被処理液タンク１内の被処理液を濃縮液と透過
液とに分離する膜モジュール２、被処理液タンク１から
膜モジュール２へ被ＪＡＮ 液を供給する供給ポンプＰ
Ｉ及び配管１１．１２、膜モジュール２からの濃縮液を
被処理液タンク１へ返送するバルブＶ１％ｖ２を有する
配管１３、透過液を排出する配管１４、溶媒タンク３か
ら被・処理液タンク１へ溶媒を供給するコントロールバ
ルブｖ３、ポンプＰ２及び分岐管路１５を僅えた配管１
６、被処理液タンク１の液面を検出して溶媒供給コント
ロールバルブｖ３の開閉を行う液面調節器４を備えてお
り、前記濃縮液返送配管１３と供給配管１１とを連絡す
るバルブｖ４を有する配管１７が設けられている。図中
、５は熱交換器である。As shown in FIG. 1, the membrane separation apparatus of the present invention includes a liquid to be treated tank 1, a membrane module 2 for separating the liquid to be treated in the liquid to be treated tank 1 into a concentrated liquid and a permeated liquid, and a tank for liquid to be treated 1. Supply pump P that supplies the JAN liquid from to the membrane module 2
I and piping 11, 12, piping 13 with valve V1%v2 for returning the concentrated liquid from the membrane module 2 to the liquid to be treated tank 1, piping 14 for discharging the permeated liquid, from the solvent tank 3 to the liquid to be treated tank 1 Piping 1 with control valve v3, pump P2, and branch pipe 15 for supplying solvent to
6. It is equipped with a liquid level regulator 4 that detects the liquid level of the liquid to be treated tank 1 and opens and closes the solvent supply control valve v3, and a valve v4 that connects the concentrated liquid return pipe 13 and the supply pipe 11. A piping 17 is provided. In the figure, 5 is a heat exchanger.
即ち、この膜分離装置では、膜モジュール２の濃縮液の
少なくとも一部が、被処理液タンク１を経ることなく膜
モジュール２に循環供給される。That is, in this membrane separation apparatus, at least a part of the concentrated liquid in the membrane module 2 is circulated and supplied to the membrane module 2 without passing through the liquid to be treated tank 1.
次に、このような本発明の膜分離装置により、例えば菌
体とアミラーゼを含む発酵ブロスを被処理液として膜分
離処理する方法について説明する。Next, a method will be described in which a fermentation broth containing, for example, bacterial cells and amylase is subjected to membrane separation treatment using the membrane separation apparatus of the present invention as a liquid to be treated.
まず、被処理液タンク１内の被処理液をポンプＰＩの動
力で配管１１．１２を経て膜モジュール２へ送給し、ア
ミラーゼを含む透過液は配管１４を経て系外へ排出し、
濃縮液は配管１３より被処理液タンク１へ返送する。そ
の際、バルブｖ１により膜モジュール２での濃縮液の圧
力を調節する。First, the liquid to be treated in the liquid to be treated tank 1 is fed to the membrane module 2 through the piping 11 and 12 using the power of the pump PI, and the permeate containing amylase is discharged outside the system through the piping 14.
The concentrated liquid is returned to the liquid to be treated tank 1 through the pipe 13. At that time, the pressure of the concentrated liquid in the membrane module 2 is adjusted by the valve v1.
被処理液タンク１に返送された濃縮液は被処理液と混合
して膜モジュール２に供給して更に濃縮し、供給が困難
になった時点でポンプＰ２の起動により配管１６を経て
溶媒タンク３より溶媒を供給して希釈する。その際、供
給する溶媒の量は液面調節器４でコントロールバルブ■
３を開閉することにより調節し、過剰の溶媒は分岐管路
１５により溶媒タンク３に返送する。The concentrated liquid returned to the liquid to be treated tank 1 is mixed with the liquid to be treated and supplied to the membrane module 2 for further concentration. When the supply becomes difficult, the pump P2 is activated to send it to the solvent tank 3 via the pipe 16. Supply more solvent to dilute. At that time, the amount of solvent to be supplied is controlled by the liquid level regulator 4 using the control valve ■
3, and excess solvent is returned to the solvent tank 3 via a branch line 15.
なお、溶媒供給手段は、図示のようなポンプを用いるの
が最も良いが、他の加圧法、例えば気体による加圧法、
ヘッドによる加圧法を採用することもできる。また、溶
媒の供給は、被処理液タンク１に直接供給する他、返送
配管１３のバルブｖ２以降の配管に供給しても良い。It is best to use a pump as shown in the figure as the solvent supply means, but other pressurizing methods such as gas pressurizing,
A pressurization method using a head can also be adopted. Further, the solvent may be supplied not only directly to the liquid to be treated tank 1 but also to the pipe after the valve v2 of the return pipe 13.
本発明の装置においては、このように溶媒による希釈を
行う際、被処理液タンク１内の発泡を抑えるために、膜
モジュール２からの濃縮液の少なくとも一部を配管１７
により、被処理液の供給配管１１へ送給して循環させる
。この場合、好ましくは返送する濃縮液の全量を供給配
管１１へ送給、循環するのが良いが、一部を被処理液タ
ンク１に戻しても良い。この濃縮液の送給液量はバルブ
■２及びｖ４で調節する。In the apparatus of the present invention, when diluting with a solvent in this way, in order to suppress foaming in the liquid to be treated tank 1, at least a part of the concentrated liquid from the membrane module 2 is transferred to the pipe 17.
As a result, the liquid to be treated is fed to the supply pipe 11 and circulated. In this case, preferably, the entire amount of the concentrated liquid to be returned is fed to the supply pipe 11 and circulated, but a portion may be returned to the liquid to be treated tank 1. The amount of concentrated liquid to be fed is adjusted by valves 2 and v4.
このように、本発明の装置においては、濃縮液を被処理
液タンク１を経ずに循環することができるため、返送さ
れる濃縮液と被処理液タンク内の被処理液とが強くぶつ
かりあうことがなく、発泡が抑えられる。しかも濃縮液
は配管１１にて被処理液タンクからの希釈溶媒で希釈さ
れた被処理液で希釈されるため、膜モジュール２には希
釈された液として循環され、効率的に処理される。In this way, in the apparatus of the present invention, the concentrated liquid can be circulated without passing through the liquid to be treated tank 1, so that the concentrated liquid to be returned and the liquid to be treated in the liquid to be treated tank collide strongly. foaming is suppressed. Moreover, since the concentrated liquid is diluted in the pipe 11 with the liquid to be treated diluted with the diluting solvent from the liquid to be treated tank, it is circulated to the membrane module 2 as a diluted liquid and is efficiently processed.
溶媒で希釈した濃縮液ないし被処理液は前記と同様の手
順で膜モジュール２に供給して処理し、アミラーゼを更
に回収する。The concentrated liquid or liquid to be treated diluted with a solvent is supplied to the membrane module 2 and treated in the same manner as described above, and amylase is further recovered.
なお、以上の説明では、被処理液をある程度処理して濃
縮してから溶媒による希釈を行う例を説明したが、溶媒
による希釈は処理開始と共に行っても良い。しかしなが
ら、一般には、予め被処理液を濃縮し、液量を減少させ
た後、溶媒を供給する方が、溶媒供給量が少なくなり効
率的である。In addition, in the above description, an example was explained in which the liquid to be treated is processed to some extent and concentrated, and then diluted with a solvent, but the dilution with a solvent may be performed at the same time as the start of the treatment. However, in general, it is more efficient to supply the solvent after concentrating the liquid to be treated in advance to reduce the amount of the liquid, since the amount of solvent supplied is smaller.
本発明の膜分離装置において、膜モジュールとしては特
に制限はなく、逆浸透膜モジュール、限外濾過膜モジュ
ール、精密濾過膜モジュール等のいずれをも用いること
ができる。また、モジュールの型式も、渦巻型、中空糸
型、管状型、平板型のいずれでも良い。In the membrane separation apparatus of the present invention, the membrane module is not particularly limited, and any of a reverse osmosis membrane module, an ultrafiltration membrane module, a precision filtration membrane module, etc. can be used. Further, the type of module may be any of a spiral type, a hollow fiber type, a tubular type, and a flat plate type.
このような本発明の膜分離装置は、発泡性のある発酵液
等を処理する装置として極めて好適であり、菌体、その
破片、蛋白質、酵素、アルコール有ｍｒＭ、アミノ酸、
抗生物質等の分離に有効である。勿論、本発明の膜分離
装置は、発酵液等からこれらの物質を分離する以外にも
、あらゆるダイアフィルトレージョン法を採用する処理
に用いることができる。なお、希釈溶媒としては、水の
他、有機溶媒等を用いることもできる。Such a membrane separation device of the present invention is extremely suitable as a device for treating foaming fermentation liquor, etc., and can be used to process bacterial cells, fragments thereof, proteins, enzymes, alcohol-containing mrM, amino acids,
Effective for separating antibiotics, etc. Of course, the membrane separator of the present invention can be used not only for separating these substances from fermentation liquid and the like, but also for treatments that employ any diafiltration method. Note that as the diluent solvent, in addition to water, an organic solvent or the like can also be used.
以下、実験例について説明する。An experimental example will be explained below.
実験例１
プロテアーゼと菌体の分離を目的とし、第１図に示す本
発明の装置と第２図に示す従来の装置を用いてそれぞれ
実験を行なった。実験は次のようにして行なった。即ち
、３００ｆｔの原液をポンプが発泡によりキャビテーシ
ョンをおこし、送液困難になるまで濃縮し、その後加水
循環（加水は濃縮液量の倍量まで行ない、もとの濃縮液
量まで濾過する）を行なった。これを数回繰り返して、
加水量と酵素の収率のデータを取った。Experimental Example 1 For the purpose of separating protease and bacterial cells, experiments were conducted using the apparatus of the present invention shown in FIG. 1 and the conventional apparatus shown in FIG. 2, respectively. The experiment was conducted as follows. In other words, the pump concentrates 300 ft of stock solution until cavitation occurs due to foaming, making it difficult to send the solution, and then water is added and circulated (water is added to double the amount of concentrated solution, and then filtered to the original amount of concentrated solution). Ta. Repeat this several times,
Data on the amount of water added and the yield of enzyme were collected.
なお、膜モジュールの膜は精密濾過膜であり、詳細な試
験条件は下記の通りである。The membrane of the membrane module is a precision filtration membrane, and the detailed test conditions are as follows.
■運転圧力 入口 １．０ｋｇｆ／ｃｒｒ？出口 ０
．４ｋｇｆ／ｃｒｎ’
■循環流量 ４ｄ／ｈ
■返送濃縮液量 ３．８５〜３．９ｄ／ｈ■温 度
１０℃
■使用膜 中空糸内圧型、孔径０．４５μｍ相当、
膜面積３ｒｒ？
■目標収率 プロテアーゼ収率９８％以上なお、第２
図に示す装置においては、返送する濃縮液のうち３．５
〜３．６ゴ／ｈを配管１７より供給配管１１に送給し、
残る約０．４ｒｎ”／ｈを被処理液タンク１に送給した
。また、被処理液タンク１からは０．４〜０．５ｍ’／
ｈの割合で供給を行なった。■Operating pressure Inlet 1.0kgf/crr? Exit 0
．． 4kgf/crn' ■Circulation flow rate 4d/h ■Return concentrated liquid volume 3.85-3.9d/h ■Temperature
10℃ ■Membrane used Hollow fiber internal pressure type, pore size equivalent to 0.45μm,
Membrane area 3rr? ■Target yield Protease yield of 98% or more.
In the device shown in the figure, 3.5% of the concentrated liquid to be returned is
~3.6 go/h is sent from the pipe 17 to the supply pipe 11,
The remaining approximately 0.4 m'/h was fed to the liquid to be treated tank 1. Also, from the liquid to be treated tank 1, 0.4 to 0.5 m'/h was fed to the liquid to be treated tank 1.
The feed was carried out at a rate of h.
第 １ 表
第１表より、プロテアーゼの収率９８％を得るためには
、本発明の装置では加水量８８ＪＺ必要であるのに対し
、従来の装置では２２５１の加水量が必要である。即ち
、本発明によれば従来の装置と比較して４０％の加水量
ですんだ。又、全濾過量は本発明では２１６１であり、
従来装置では３３０ｊＺであった。即ち、本発明によれ
ば全濾過量が、従来の６５％で済むことが判明し、次工
程の濃縮工程が小さくてすむことが明らかである。Table 1 From Table 1, in order to obtain a protease yield of 98%, the apparatus of the present invention requires an amount of water added of 88 JZ, while the conventional apparatus requires an amount of water added of 2251 JZ. That is, according to the present invention, the amount of water added is 40% compared to the conventional device. In addition, the total filtration amount is 2161 in the present invention,
In the conventional device, it was 330jZ. That is, it has been found that according to the present invention, the total filtration amount is only 65% of the conventional amount, and it is clear that the subsequent concentration step can be reduced.
［発明の効果］
以上詳述した通り、本発明の膜分離装置によれば、ダイ
アフィルトレージョン法による処理において、発泡性の
被処理液を処理する場合においても、被処理液タンク内
の発泡を抑えることができる。[Effects of the Invention] As detailed above, according to the membrane separation apparatus of the present invention, even when a foaming liquid to be treated is treated by the diafiltration method, foaming in the liquid to be treated tank is prevented. can be suppressed.
このため、従来より効率的な処理が困難とされていた発
泡性被処理液であっても、
■ 高度に濃縮できる。Therefore, even foaming liquids to be treated, which have traditionally been difficult to treat efficiently, can be highly concentrated.
■ 希釈液（溶媒）量が少なくなる。■ The amount of diluent (solvent) decreases.
■ 透過液中の有価物濃度が高い。■ The concentration of valuable substances in the permeate is high.
■ 透過液を次工程で晶析等により容易に？！ＡＮする
ことができる。■ Can the permeate be easily crystallized in the next process? ! AN can be done.
等の効果が奏され、低コストで容易かつ効率的に処理を
行うことが可能とされる。Effects such as these are achieved, and processing can be performed easily and efficiently at low cost.
第１図の本発明の膜分離装置の一実施例を示す系統図、
第２図は従来の装置を示す系統図である。
１・・・被処理液タンク、 ２・・・膜モジュール、
３・・・濃縮タンク、 ４・・・液面調節器、Ｐ
Ｉ ％ Ｐ ２・・・ポンプ、 Ｖｌ〜Ｖ４・・・
バルブ。A system diagram showing an embodiment of the membrane separation device of the present invention shown in FIG.
FIG. 2 is a system diagram showing a conventional device. 1... Liquid tank to be treated, 2... Membrane module,
3...Concentration tank, 4...Liquid level regulator, P
I% P2...Pump, Vl~V4...
valve.
Claims (2)
ルと、 ｃ、被処理液タンクから膜モジュールへ被処理液を供給
する供給管路及び供給ポンプと、 ｄ、被処理液を希釈する溶媒の供給手段と、ｅ、濃縮液
を前記被処理液タンクへ返送する返送管路と、 を備えてなる膜分離装置において、 前記返送管路と供給ポンプ入口側の供給管路とを連絡す
る連絡管路を設けたことを特徴する膜分離装置。(1) The following a to e, namely: a. A tank for the liquid to be treated; b. A membrane module that separates the liquid to be treated into a concentrated liquid and a permeated liquid; and c. Transferring the liquid to be treated from the tank to the membrane module. A membrane separation system comprising: a supply pipe and a supply pump for supplying a liquid; d) a means for supplying a solvent for diluting the liquid to be treated; and e) a return pipe for returning the concentrated liquid to the tank for the liquid to be treated. A membrane separation device, characterized in that the device is provided with a communication pipe that connects the return pipe and a supply pipe on the inlet side of the supply pump.
面調節器を備えていることを特徴とする特許請求の範囲
第１項に記載の膜分離装置。(2) The membrane separation apparatus according to claim 1, wherein the liquid to be treated tank is equipped with a liquid level regulator that is linked to a solvent supply means.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25663386A JPS63111905A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25663386A JPS63111905A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63111905A true JPS63111905A (en) | 1988-05-17 |
Family
ID=17295319
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25663386A Pending JPS63111905A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63111905A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008073670A (en) * | 2006-09-25 | 2008-04-03 | Tomoe Engineering Co Ltd | Belt-type concentrator |
| WO2011099578A1 (en) * | 2010-02-13 | 2011-08-18 | Yamanaka Kunihiko | Water purification device |
-
1986
- 1986-10-28 JP JP25663386A patent/JPS63111905A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008073670A (en) * | 2006-09-25 | 2008-04-03 | Tomoe Engineering Co Ltd | Belt-type concentrator |
| WO2011099578A1 (en) * | 2010-02-13 | 2011-08-18 | Yamanaka Kunihiko | Water purification device |
| JP5563604B2 (en) * | 2010-02-13 | 2014-07-30 | 邦彦 山中 | Water purifier |
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