JPS6223404A - Membrane separation apparatus - Google Patents
Membrane separation apparatusInfo
- Publication number
- JPS6223404A JPS6223404A JP60161234A JP16123485A JPS6223404A JP S6223404 A JPS6223404 A JP S6223404A JP 60161234 A JP60161234 A JP 60161234A JP 16123485 A JP16123485 A JP 16123485A JP S6223404 A JPS6223404 A JP S6223404A
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- section
- sections
- separation
- liquid
- 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 70
- 238000000926 separation method Methods 0.000 title claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 16
- 239000012466 permeate Substances 0.000 claims description 18
- 239000007788 liquid Substances 0.000 abstract description 18
- 239000000203 mixture Substances 0.000 abstract description 6
- 239000012888 bovine serum Substances 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 108010074605 gamma-Globulins Proteins 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000012488 sample solution Substances 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 108010044091 Globulins Proteins 0.000 description 1
- 102000006395 Globulins Human genes 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 230000009193 crawling Effects 0.000 description 1
- 239000010432 diamond Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 238000001471 micro-filtration Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000002504 physiological saline solution Substances 0.000 description 1
- -1 polyethylene Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/145—Ultrafiltration
- B01D61/146—Ultrafiltration comprising multiple ultrafiltration steps
Landscapes
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は限外濾過膜あるいは精密濾過膜を装着アンドフ
レーム型の４種に大別されるが、本発明〔従来の技術〕
プレートアンドフレーム型膜分離装置の代表的な形態は
、例えば特公昭５５−３５５５３号公報あるいは特公昭
５５−１７６０８号公報等に記載されている。この装置
は、シート状の分離膜を多数装着し、必要膜面積を確保
することに最大の特徴を持つ。通常プレートアンドフレ
ーム型膜分離装置は、該膜分離装置内が複数のセクショ
ンに区切られ、各セクションは実質的に直列に配置され
た構造をとると共に各セクション内には複数の膜が並列
に配置されている。該装置内を複数のセクションに区切
る理由は、該分離装置内への送液量を低減せしめるため
である。従来のプレートアンドフレーム型膜分離システ
ムは、供給液タンク。[Detailed Description of the Invention] [Industrial Field of Application] The present invention can be roughly divided into four types: a plate-and-frame type equipped with an ultrafiltration membrane or a microfiltration membrane. Typical forms of membrane separation devices are described, for example, in Japanese Patent Publication No. 55-35553 or Japanese Patent Publication No. 55-17608. The main feature of this device is that it is equipped with a large number of sheet-like separation membranes to ensure the necessary membrane area. Normally, a plate-and-frame membrane separator has a structure in which the inside of the membrane separator is divided into multiple sections, each section is substantially arranged in series, and each section has multiple membranes arranged in parallel. has been done. The reason for dividing the inside of the device into a plurality of sections is to reduce the amount of liquid fed into the separation device. Traditional plate-and-frame membrane separation systems use a feed tank.
供給液圧送ポンプ、膜分離装置（モジュールと呼ぶ場合
もある）、および圧力計、流量計、配管類より構成され
る。そして、分離に供される供給液は、タンクからポン
プにより膜分離装置内へ圧送され、膜分離装置内の各セ
クションを通り、膜分の大部分は、システム内を循環し
ていることになる。一方、膜分離装置内を供給液が通過
する際、該供給液の一部は膜を通過し、膜を支持してい
る多孔性の支持板側へ移る。これが膜透過液である。It consists of a feed liquid pressure pump, a membrane separation device (sometimes called a module), a pressure gauge, a flow meter, and piping. Then, the feed liquid to be separated is pumped from the tank into the membrane separator, passes through each section of the membrane separator, and most of the membrane content is circulated within the system. . On the other hand, when the feed liquid passes through the membrane separation device, a portion of the feed liquid passes through the membrane and moves to the porous support plate that supports the membrane. This is the membrane permeate.
膜透過液は支持板からチューブを通して外部へ導出され
、全支持板から導出された膜透過液は一本の集水管へ集
められる。The membrane permeate liquid is led out from the support plate through the tube, and the membrane permeate liquid led out from all the support plates is collected into one water collecting pipe.
このような膜分離装置では、装置内部で複数のセクショ
ンが直列につながれているために圧力損失が大きく１．
装置の入口側のセクションから得られる透水量と、出口
側から得られる透水量に差が生じる傾向がある。In such a membrane separation device, pressure loss is large because multiple sections are connected in series inside the device.
There tends to be a difference between the amount of water permeable from the inlet section of the device and the amount of water permeable from the outlet side.
また、膜透過流速の違いが、膜分離結果に大きな影響を
及ぼすことを見い出した。したがって、従来使用されて
来た装置では、装置内に仕切られた各セクション間の膜
透過液の組成に互に差があり、一定の組成をもつ膜透過
液が得られ難い。We also found that the difference in membrane permeation flow rate has a large effect on the membrane separation results. Therefore, in conventionally used devices, there are differences in the composition of the membrane permeate between the sections partitioned within the device, making it difficult to obtain a membrane permeate having a constant composition.
本発明は、該各セクシコンにおける分離膜の表裏間の圧
力を一定とし、各セクションの分離結果の差を実質的に
無くすことを目的とするものである。An object of the present invention is to make constant the pressure between the front and back surfaces of the separation membrane in each section, and to substantially eliminate differences in the separation results of each section.
本発明者らは、プレートアンドフレーム型膜分離装置の
各セクションにおける圧力を同一にするためには、膜透
過流速を同一にすれば良いと考え、各セクション毎に透
水量調節バルブを設けることにより、本発明を完成する
に至った。The present inventors believed that in order to equalize the pressure in each section of a plate-and-frame membrane separator, it would be sufficient to make the membrane permeation flow rate the same, and by providing a water permeation amount adjustment valve for each section. , we have completed the present invention.
すなわち、本発明は複数のセクションに区切られ、かつ
該複数のセクションが直列に配列された構造を有するプ
レートアンドフレーム型膜モジュールの各セクションの
膜透過液出口が、膜透水量調節バルブを有する膜分離装
置に関するものである。That is, the present invention provides a plate-and-frame membrane module having a structure in which the plurality of sections are divided into a plurality of sections and arranged in series. This relates to a separation device.
以下、本発明を図面により説明する。Hereinafter, the present invention will be explained with reference to the drawings.
第１図は本発明の一実施態様を被処理液の流れで示した
模式図である。FIG. 1 is a schematic diagram showing an embodiment of the present invention in terms of the flow of the liquid to be treated.
第１図において、腹這水量調節パルプ（ａ）〜（ｄ）は
４つのセクションＳ−１〜Ｓ−４に仕切られ、かつ、該
セクションＳ−１〜Ｓ−４が直列に配列されたプレート
アンドフレーム型膜モジュールの各膜透過液出口に設置
された構成をなすものである。In FIG. 1, the pulps (a) to (d) for regulating the amount of water crawling are divided into four sections S-1 to S-4, and the sections S-1 to S-4 are arranged in series on a plate. It is installed at each membrane permeate outlet of an and frame type membrane module.
そして、被処理液Ａはポンプにより供給され、セクショ
ンＳ−１〜Ｓ−４の４＠つに区切られた膜分離モジュー
ルをセクションＳ−４より順にセクションＳ−１まで通
過しモジニール外へ出る。Then, the liquid to be treated A is supplied by a pump, passes through the membrane separation module divided into four sections S-1 to S-4 in order from section S-4 to section S-1, and exits outside the module.
一方、膜透過液Ｂは各膜の支持体へ流れ込み、支持体か
ら配管によって各セクションより別々にモジュール外へ
取り出される。すなわち、膜透過液Ｂはその膜透過液出
口に設けられた各バルブ（ａ）〜（、ｉ）を通り、流量
計（１）〜（４）をそれぞれ通過し、取り出され、その
後、全セクションからの膜透過液Ｂは、一本の配管にま
とめられ、流量計（５）を通過する。このとき各セクシ
ョンよりの膜透過流速は、バルブ（ａＬ （ｂ）、 （
Ｑ）、 （ｄ）の操作により最適条件に設定することに
より、各セクションよりの組成を一定とするものである
。On the other hand, the membrane permeate B flows into the support of each membrane, and is separately taken out of the module from each section via piping from the support. That is, the membrane permeate B passes through the valves (a) to (i) provided at the membrane permeate outlet, passes through the flowmeters (1) to (4), and is taken out. The membrane permeate liquid B is collected into one pipe and passes through a flow meter (5). At this time, the membrane permeation flow rate from each section is determined by the valve (aL (b), (
By setting the optimal conditions through the operations in Q) and (d), the composition from each section is made constant.
本発明では、該膜透過液を各セクション毎に一カ所にま
とめ、各一本の配管とし、該各配管毎に流量調節バルブ
を設けるものである。各セクションから膜透水量調節バ
ルブまでの配管は耐圧性のものが望ましい。この長なも
のとして、四弗化エチレンチューブ、網入りポリエチレ
ンチューブ、ステンレスチューブ等が好ましい。また、
膜透水量調節バルブは微量調整の可能なニードルバルブ
が最も望ましいが、その他にボールバルブ、ダイアｎ叉
〒１−“ｍため、各腹這水量調
節パルプを出た膜透過液は、各調整バルブ専用の流量計
を通過することが望ましい。該流量計の読みにより流量
調整が簡単になる。In the present invention, the membrane-permeated liquid is collected in one place for each section, each section is connected to one pipe, and each pipe is provided with a flow rate regulating valve. It is desirable that the piping from each section to the membrane water permeation control valve be pressure resistant. Preferred examples of such long tubes include tetrafluoroethylene tubes, wired polyethylene tubes, and stainless steel tubes. Also,
The most desirable membrane water permeation rate adjustment valve is a needle valve that allows for minute adjustments, but other methods include ball valves and diamonds. It is desirable to pass through a dedicated flow meter, the reading of which simplifies flow adjustment.
本発明による膜分離装置は、膜モジエール内に仕切られ
た複数のセクションがすべて実質的に同一の分離挙動を
示す。したがって、本装置は最も望ましい分離挙動を全
てのセクションにおいて実現することを可能とするもの
である。In the membrane separation device according to the present invention, the plurality of sections partitioned into the membrane module all exhibit substantially the same separation behavior. The device therefore makes it possible to achieve the most desirable separation behavior in all sections.
実施例
有効膜面積がＱ、０１ｆｆ／の膜１００枚を装着し、膜
２０枚毎に仕切りを入れることにより、有効膜面積（Ｌ
２ｙｙ／のセクションを５基所有するプレートアンドフ
レーム型限外濾過モジ為−ル（東洋曹達工業製、商品名
ｓｏ−１００Ｍ）を用い、ウシ血清γ−グロブリン（分
子ｉ１．６×ｔｏ’）の脱ポリマー櫂みた。ウシ血清ｒ
−グロブリン中には、精製工程中に生成したγ−グロブ
リン凝集体（分子ｉ１×１ｃｌ’以上）が１６５％含有
されていた。用いた膜は、分画分子量３ Ｘ １０’の
限外濾過膜（東洋曹達工業製、商品名ＴＳ−ｓｏｏｎ＞
である。Example: By installing 100 membranes with an effective membrane area of Q, 01ff/, and inserting a partition every 20 membranes, the effective membrane area (L
Bovine serum γ-globulin (molecule i1.6 I saw a depolymer paddle. bovine serum r
- The globulin contained 165% of γ-globulin aggregates (molecules i1 x 1 cl' or more) generated during the purification process. The membrane used was an ultrafiltration membrane with a molecular weight cut off of 3 x 10' (manufactured by Toyo Soda Kogyo, trade name: TS-soon).
It is.
ウシ血清ｒ−グロブリン５０９を５ｔの生理食塩水に溶
解し、試料液とした。試料液をタンクへ入れ、ロータリ
ーポンプにより、１０ｔ／分の流速でモジュール内へ圧
送した。この時、モジュール入口圧は１．２ ｋｇ／７
．出口圧は０．２に９／ａｄであった０
上記操作において、各セクションの透過液調整パルプを
全開とした時の膜透過液組成、膜透過流速を比較例とし
て表１に示す。表中、セクション番号は、最高圧セクシ
ョンを１としている。膜透過液組成が各セクションで異
なること、有効に利用されているセクションが少ないこ
とがわかる。Bovine serum r-globulin 509 was dissolved in 5 t of physiological saline and used as a sample solution. The sample solution was placed in a tank and was pumped into the module at a flow rate of 10 t/min using a rotary pump. At this time, the module inlet pressure is 1.2 kg/7
．． The outlet pressure was 0.2 to 9/ad. In the above operation, the membrane permeate composition and membrane permeation flow rate when the permeate adjustment pulp of each section was fully opened are shown in Table 1 as a comparative example. In the table, the section number is 1 for the highest pressure section. It can be seen that the membrane permeate composition differs in each section, and that only a few sections are effectively utilized.
本操作は、各セクションに透過液調整バルブが設けられ
ているものの、該バルブはすべて全開であり、実質的に
従来の膜分離方法と同じである。Although each section is provided with a permeate adjustment valve, this operation is substantially the same as the conventional membrane separation method, with all the valves being fully open.
次に、比較例で最も良い分離結果を与えたのはセクシ舊
ン５（最低圧セクション）であった。よって、各セクシ
ョンの透過液調整パルプの操作により、比較例における
セクション５の透水速度である９、５Ｌ／ｆｆ１″・時
にすべてのセクションの透水量を脱退水撒調節バルブで
あるニードルバルブで調整した。結果を実施例として表
１に示す。本操作の脱退水速度の調節により、高濃度の
膜透過液が得られ、また、すべての膜が有効にその分離
性能を発揮することがわかる。Next, in the comparative example, it was Section 5 (lowest pressure section) that gave the best separation results. Therefore, by operating the permeate adjustment pulp of each section, the water permeation amount of all sections was adjusted with the needle valve, which is the withdrawal water distribution control valve, when the water permeation rate of section 5 in the comparative example was 9.5L/ff1''. The results are shown in Table 1 as an example.It can be seen that by adjusting the rate of desorbed water in this operation, a highly concentrated membrane permeate liquid was obtained, and all the membranes effectively exhibited their separation performance.
第１図は本発明の一実施態様を示す模式図である。
Ｓ−１，Ｓ−２，Ｓ−３，Ｓ−４セクションａ、ｂ、ｃ
、ｄ 膜透水量調節バルブ１、２．６．４．
５ 流量計Ａ 被処理水
Ｂ 膜透過液FIG. 1 is a schematic diagram showing one embodiment of the present invention. S-1, S-2, S-3, S-4 sections a, b, c
, d Membrane water permeation rate adjustment valve 1, 2.6.4.
5 Flowmeter A Treated water B Membrane permeate liquid
Claims (1)
ションが直列に配列された構造を有するプレートアンド
フレーム型膜分離装置において、各セクションの膜透過
液出口が膜透水量調節バルブを有することを特徴とする
膜分離装置。1. In a plate-and-frame membrane separator that is partitioned into a plurality of sections and has a structure in which the plurality of sections are arranged in series, the membrane permeate outlet of each section has a membrane water permeation amount adjustment valve. Features of membrane separation equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60161234A JPS6223404A (en) | 1985-07-23 | 1985-07-23 | Membrane separation apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60161234A JPS6223404A (en) | 1985-07-23 | 1985-07-23 | Membrane separation apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6223404A true JPS6223404A (en) | 1987-01-31 |
Family
ID=15731184
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60161234A Pending JPS6223404A (en) | 1985-07-23 | 1985-07-23 | Membrane separation apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6223404A (en) |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5824313A (en) * | 1981-08-05 | 1983-02-14 | Sanyo Kokusaku Pulp Co Ltd | Preventing method for clogging of flat plate type ultrafiltration device |
| JPS59179110A (en) * | 1983-03-30 | 1984-10-11 | Nitto Electric Ind Co Ltd | Operating method of filter module |
-
1985
- 1985-07-23 JP JP60161234A patent/JPS6223404A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5824313A (en) * | 1981-08-05 | 1983-02-14 | Sanyo Kokusaku Pulp Co Ltd | Preventing method for clogging of flat plate type ultrafiltration device |
| JPS59179110A (en) * | 1983-03-30 | 1984-10-11 | Nitto Electric Ind Co Ltd | Operating method of filter module |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5690830A (en) | Waste water treatment apparatus and washing method thereof | |
| US7938956B2 (en) | Water purification system and method, and module for the system | |
| US11975293B2 (en) | Tangential flow filtration device for perfusion applications | |
| EP1210298B1 (en) | System for operation of multiple membrane filtration assemblies | |
| RU2003107099A (en) | PROCESS AND DEVICE FOR MIXING LIQUIDS WHILE PROCESSING VARIOUS TFC-MEMBRANES | |
| JPS614591A (en) | Reverse osmosis system | |
| EP2119492A1 (en) | Tangential flow filtration system | |
| KR910009327A (en) | Membrane Separation System and Its Usage | |
| JPH05123537A (en) | Device and method for separation in ultrafiltration system | |
| IE49608B1 (en) | Reducing the alcohol content in fermented drinks by dialysis | |
| WO2004069391A1 (en) | Hollow fiber membrane module and module arrangement group thereof | |
| JPH03272676A (en) | Precise filtration process, and apparatus therefor | |
| KR100346018B1 (en) | A Plate-and-Frame Type Membrane Module System Inserted Durable Balls with Vortex Flow | |
| JPH0295422A (en) | Operating method for hollow yarn membrane module | |
| JPS6223404A (en) | Membrane separation apparatus | |
| JP2852958B2 (en) | Operating method of membrane module | |
| KR101256704B1 (en) | System and Method for Filtering | |
| WO1997004857A1 (en) | Membrane filtration apparatus | |
| JPS60129106A (en) | Operation of ultrafiltration module | |
| JPS62286586A (en) | Water treatment plant | |
| JPS581913B2 (en) | Method and apparatus for producing fermented beverages with reduced alcohol content | |
| RU2047330C1 (en) | Method for producing potable water | |
| US20240246034A1 (en) | Tangential flow filtration device for perfusion applications | |
| JPS63221805A (en) | Filter | |
| WO2023187064A1 (en) | Separation system for separating and purifying a target component |