JPS63111904A - Membrane separator - Google Patents
Membrane separatorInfo
- Publication number
- JPS63111904A JPS63111904A JP25663286A JP25663286A JPS63111904A JP S63111904 A JPS63111904 A JP S63111904A JP 25663286 A JP25663286 A JP 25663286A JP 25663286 A JP25663286 A JP 25663286A JP S63111904 A JPS63111904 A JP S63111904A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- supply
- tank
- solvent
- treated
- 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 49
- 239000007788 liquid Substances 0.000 claims abstract description 103
- 239000002904 solvent Substances 0.000 claims abstract description 33
- 238000000926 separation method Methods 0.000 claims description 17
- 239000012466 permeate Substances 0.000 claims description 9
- 239000012141 concentrate Substances 0.000 claims description 3
- 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
- 230000007423 decrease Effects 0.000 abstract description 2
- 241000894006 Bacteria Species 0.000 abstract 1
- 230000005587 bubbling Effects 0.000 abstract 1
- 238000000034 method Methods 0.000 description 13
- 238000011026 diafiltration Methods 0.000 description 6
- 238000005187 foaming Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 3
- 238000000855 fermentation Methods 0.000 description 3
- 230000004151 fermentation Effects 0.000 description 3
- 230000001580 bacterial effect Effects 0.000 description 2
- 238000007865 diluting Methods 0.000 description 2
- 239000003085 diluting agent Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000013076 target substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 101000623895 Bos taurus Mucin-15 Proteins 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000001476 alcoholic effect Effects 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
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000006260 foam Substances 0.000 description 1
- 239000012634 fragment Substances 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 150000007524 organic acids Chemical class 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 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】
［産業上の利用分野コ
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、溶媒を容易かつ効率的に定量注入することができ
る、改良された膜分離装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] 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 can easily and efficiently inject a fixed amount of a solvent during processing using 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、予め希釈しておき、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] The target substance is separated and purified into the concentrated liquid side or the permeated liquid side by diluting the liquid to be treated with a solvent (mainly water) or diluting it in advance and performing membrane separation. This method has been 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、供給液タン
ク２０内の被処理液はポンプ２１により供給配管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より供給液タンク２０に
返送されるように構成されている。しかして、供給液タ
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より供給液タンク２０に
加える。従って、この加える溶媒の量は膜モジュール２
３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, in which the liquid to be treated in the supply liquid tank 20 is fed to the membrane module 23 via the supply pipe 22 by a pump 21, and the permeate is discharged from the pipe 24. The concentrated liquid is configured to be returned to the supply liquid tank 20 via piping 25. Thus, the solvent is added to the supply liquid tank 20 through the pipe 27 having the valve 26 so as to keep the liquid level 20a of the supply liquid tank 20 constant. Therefore, the amount of solvent added is
The amount is equal to the amount of permeate discharged from 3.
従来、供給液タンク２０への溶媒供給量の制御は、第２
図に示す如く、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 supply liquid tank 20 is controlled by the second
As shown in the figure, by opening and closing the valve 26 of the solvent supply piping 27 using the liquid level regulator 28 installed in the tank 20, etc.
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、液面調節器等の制御機器を
必要とする上に、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、このような溶液は供給液タンクの中で
発泡し、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、泡が供給液タン
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] Such conventional devices require control equipment such as a liquid level regulator, and generally the liquid to be treated (undiluted solution) that is subject to the diafiltration method is In many cases, it is a highly concentrated organic solution, and such a solution foams in the supply liquid tank, making it difficult to control with a liquid level regulator or making it impossible to supply quantitatively. Further, there are also problems such as bubbles flowing out from the upper part of the supply liquid 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、液面調節器等の制
御機器を必要とせず、発泡性の被処理液でも供給液タン
クで発泡することなく、透過量に相当する溶媒を容易か
つ確実に定量的に供給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 eliminates the need for control equipment such as a liquid level regulator, and eliminates the need for foaming liquids to be treated in the supply liquid tank. The present invention provides a membrane separation device that can easily and reliably quantitatively supply a solvent corresponding to the amount of permeation.
本発明の膜分離装置は、
ａ、密閉された耐圧性の供給液タンクと、ｂ、供給液タ
ンク内の被処理液を濃縮液と透過液とに分離する膜モジ
ュールと、
Ｃ０供給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、被処理液を前記供給
液タンクへ供給する手段と、
ｅ、溶媒を前記供給液タンク又は供給管路へ供給する手
段と、
ｆ、膜モジュールからの濃縮液を前記供給タンクへ返送
する返送管路と、
を備えてなる。The membrane separator of the present invention comprises: a) a sealed pressure-resistant feed liquid tank; b) a membrane module that separates the liquid to be treated in the feed liquid tank into a concentrate and a permeate; and from the C0 feed liquid tank. a supply pipe and a supply pump for supplying the liquid to be treated to the membrane module; d. means for supplying the liquid to be treated to the supply liquid tank; e. means for supplying the solvent to the supply liquid tank or the supply pipe. , f, a return conduit for returning the concentrate from the membrane module to the supply tank.
［作用］
本発明の膜分離装置では、供給液タンク、供給管路、膜
モジュール及び返送管路で密閉系が形成されるため、処
理を継続してゆくと系外へ排出された膜モジュールの透
過液量の分だけ系内が減圧となる。従って、溶媒供給手
段と密閉系とを連絡することにより、自動釣に透過液量
に相当する溶媒が供給されることとなる。[Function] In the membrane separation apparatus of the present invention, a closed system is formed by the feed liquid tank, the supply pipe line, the membrane module, and the return pipe line, so as the treatment continues, the membrane modules discharged outside the system will be removed. The pressure inside the system is reduced by the amount of permeated liquid. Therefore, by communicating the solvent supply means with the closed system, a solvent corresponding to the amount of permeated liquid is supplied to the automatic fishing rod.
また、本発明の膜分離装置においては、供給液タンクが
密閉されていることから、発泡性の被処理液であフても
、発泡を抑えることができ、処理効率が高められる。Furthermore, in the membrane separation apparatus of the present invention, since the supply liquid tank is sealed, even if the liquid to be treated is foamable, foaming can be suppressed and treatment efficiency can be improved.
［実施例］ 以下に図面を参照して本発明の詳細な説明する。[Example] 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.
この膜分離装置は、密閉された耐圧性の供給液タンク１
、供給液タンク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、供給液タンク１から膜モ
ジュール２へ被処理液を供給する供給ポンプＰ１を有す
る供給配管１１、被処理液を被処理液タンク３から供給
液タンク１へ供給するためのポンプＰ２及びバルブＶｌ
を有する配管１２、溶媒夕・ンク４から溶媒を供給液タ
ンク１へ供給するためのポンプＰ３を有する配管１３、
膜モジュール２からの濃縮液を供給液タンク１へ返送す
るバルブｖ２を有する配管１４、透過液を排出する配管
１５、供給液タンク１の通気を行うためのバルブｖ３を
有する配管１６を備えている。This membrane separator consists of a sealed pressure-resistant feed liquid tank 1
, a membrane module 2 that separates the liquid to be treated in the supply liquid tank 1 into a concentrated liquid and a permeated liquid, a supply pipe 11 having a supply pump P1 that supplies the liquid to be treated from the supply liquid tank 1 to the membrane module 2, Pump P2 and valve Vl for supplying the processing liquid from the liquid to be treated tank 3 to the supply liquid tank 1
a pipe 12 having a pump P3, a pipe 13 having a pump P3 for supplying the solvent from the solvent tank 4 to the feed liquid tank 1;
It is equipped with a pipe 14 having a valve v2 for returning the concentrated liquid from the membrane module 2 to the supply liquid tank 1, a pipe 15 for discharging the permeated liquid, and a pipe 16 having a valve v3 for ventilating the supply liquid tank 1. .
なお、本実施例においては、溶媒供給配管１３は濃縮液
返送配管１４に接続されている。In this embodiment, the solvent supply pipe 13 is connected to the concentrated liquid return pipe 14.
かかる本実施例の膜分離装置では、密閉型供給液タンク
１と膜モジュール２、これらの間の供給ポンプＰ１を有
する配管１１及び膜モジュール２の濃縮液を返送するバ
ルブｖ２を有する配管１４で、密閉循環系が形成されて
いる。In the membrane separation apparatus of this embodiment, the closed type supply liquid tank 1 and the membrane module 2, the piping 11 having the supply pump P1 between them, and the piping 14 having the valve v2 for returning the concentrated liquid of the membrane module 2, A closed circulation system is formed.
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酸分
ＩＩ処理する方法につい゛て説明する。Next, a method for treating a fermentation broth containing bacterial cells and amylase with acid component II using the membrane separation apparatus of the present invention as a liquid to be treated will be described.
まず、バルブＶ＋及びバルブｖ３を開として、ポンプＰ
２の作動により、配管１２を経て被処理液タンク３より
被処理液を供給液タンク１に供給する。供給時の供給液
タンク１内の排気は配管１６により行われる。次にバル
ブｖ１及びｖ３は閉、バルブｖ２は開の状態で、供給液
タンク１内の被処理液をポンプＰＩの動力で配管１１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１５を経て回収系へ送り、濃縮液は配管１４より
供給液タンク１べ返送する。その際、バルブｖ２により
膜モジュール２での濃縮液の圧力を調節する。First, open valve V+ and valve v3, and pump P
2, the liquid to be treated is supplied from the liquid to be treated tank 3 to the supply liquid tank 1 via the pipe 12. The supply liquid tank 1 is evacuated through the piping 16 during supply. Next, with valves v1 and v3 closed and valve v2 open, the liquid to be treated in the supply liquid tank 1 is fed to the membrane module 2 via the piping 11 using the power of the pump PI, and the permeate containing amylase is The concentrated liquid is sent to the recovery system via the pipe 15, and the concentrated liquid is returned to the supply liquid tank 1 via the pipe 14. At that time, the pressure of the concentrated liquid in the membrane module 2 is adjusted by the valve v2.
供給タンク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Ｐ３の起動により配管１３を経て溶媒
タンク４より溶媒を供給して希釈する。The concentrated liquid returned to the supply 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 P3 is activated to supply the solvent from the solvent tank 4 via the pipe 13. Supply and dilute.
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等を採用することもできる。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,
It is also possible to employ a pressure method using a head.
また、溶媒の供給箇所としては、返送配管１４、特にバ
ルブｖ２以降の返送配管、供給液タンク１、あるいは供
給配管１１が、他の箇所より液の圧力が低いところから
好ましく、とりわけ、図示の如くバルブ■２以降の返送
配管１４とするのが循環濃縮液と溶媒との混合が良くな
ることから最適である。In addition, as the solvent supply point, the return pipe 14, especially the return pipe after valve v2, the supply liquid tank 1, or the supply pipe 11 is preferable because the pressure of the liquid is lower than other places. It is optimal to use the return pipe 14 after the valve (2) because it improves the mixing of the circulating concentrated liquid and the solvent.
上記実施例の膜分離装置においては、供給液タンク１、
配管１１、膜モジュール２、配管１４で密閉系が形成さ
れているため、膜モジュール２で分列され系外へ排出さ
れた透過液分だけ、系内の圧力は低くなっている。この
ため、ポンプＰ３を作動させることにより、溶媒タンク
４の溶媒は配管１３より自動的に圧力の低い分だけ、即
ち排出された透過液分だけ供給液タンク内に供給される
こととなる。In the membrane separator of the above embodiment, the feed liquid tank 1,
Since the piping 11, the membrane module 2, and the piping 14 form a closed system, the pressure in the system is lowered by the amount of permeate that is separated by the membrane module 2 and discharged to the outside of the system. Therefore, by operating the pump P3, the solvent in the solvent tank 4 is automatically supplied into the supply liquid tank by an amount lower in pressure than the pipe 13, that is, by the amount of the discharged permeate.
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.
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、いずれでも用いること
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、アルコール有機酸、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 liquid, etc., and is suitable for separating bacterial cells, fragments thereof, proteins, enzymes, alcoholic organic acids, amino acids, antibiotics, etc. It is valid. Of course, the membrane separation device of the present invention can be used not only to separate these substances from fermentation liquid etc.
It can be used in any process that employs diafiltration methods. Note that as the diluent solvent, in addition to water, an organic solvent or the like can also be used.
［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、液面調節
器等の制御器を必要とせず、容易かつ確実に透過量に相
当する溶媒を定量的に供給することができる。また、発
泡性の被処理液を処理する場合においても、装置の処理
系統が密閉系であることから、発泡を抑えることができ
る。[Effects of the Invention] As detailed above, according to the membrane separation device of the present invention, the amount of permeation can be easily and reliably adjusted without the need for a controller such as a liquid level regulator in treatment by the diafiltration method. The corresponding solvent can be supplied quantitatively. Furthermore, even when processing a foaming liquid to be processed, since the processing system of the apparatus is a closed system, foaming 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濃縮すること
ができる。(2) The permeate can be easily concentrated by crystallization in the next step.
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・・・供給液タンク、 ２・・・膜モジュール、
３・・・被処理液タンク、 ４・・・溶媒タンク、Ｐ
、〜Ｐ３・・・ポンプ％ Ｖｌ〜■３・・・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... Supply liquid tank, 2... Membrane module,
3... Liquid tank to be treated, 4... Solvent tank, P
,~P3...Pump% Vl~■3...Valve.
Claims (2)
離する膜モジュールと、 ｃ、供給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、被処理液を前記供給液タンクへ供給する手段と、 ｅ、溶媒を前記供給液タンク又は供給管路へ供給する手
段と、 ｆ、膜モジュールからの濃縮液を前記供給タンクへ返送
する返送管路と、 を備えてなることを特徴とする膜分離装置。(1) The following a to f: a. A sealed pressure-resistant feed liquid tank; b. A membrane module that separates the liquid to be treated in the feed liquid tank into a concentrate and a permeate; c. a supply pipe line and a supply pump for supplying the liquid to be treated from the supply liquid tank to the membrane module; d. means for supplying the liquid to be treated to the supply liquid tank; e. a solvent to the supply liquid tank or the supply pipe line. A membrane separation device comprising: supply means; f. a return pipe line for returning the concentrated liquid from the membrane module to the supply tank.
返送管路に連結され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 means for supplying the solvent to the supply liquid tank is connected to a return pipe for the concentrated liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25663286A JPS63111904A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25663286A JPS63111904A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63111904A true JPS63111904A (en) | 1988-05-17 |
Family
ID=17295306
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25663286A Pending JPS63111904A (en) | 1986-10-28 | 1986-10-28 | Membrane separator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63111904A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5685990A (en) * | 1992-05-04 | 1997-11-11 | Md Foods A.M.B.A. | System and a process for membrane filtration of a dispersion |
| JP2007160253A (en) * | 2005-12-15 | 2007-06-28 | Kazuyuki Ogawa | Ultrafiltration apparatus |
-
1986
- 1986-10-28 JP JP25663286A patent/JPS63111904A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5685990A (en) * | 1992-05-04 | 1997-11-11 | Md Foods A.M.B.A. | System and a process for membrane filtration of a dispersion |
| JP2007160253A (en) * | 2005-12-15 | 2007-06-28 | Kazuyuki Ogawa | Ultrafiltration apparatus |
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