JP2003275548A - Membrane separation device - Google Patents
Membrane separation deviceInfo
- Publication number
- JP2003275548A JP2003275548A JP2002077898A JP2002077898A JP2003275548A JP 2003275548 A JP2003275548 A JP 2003275548A JP 2002077898 A JP2002077898 A JP 2002077898A JP 2002077898 A JP2002077898 A JP 2002077898A JP 2003275548 A JP2003275548 A JP 2003275548A
- Authority
- JP
- Japan
- Prior art keywords
- filtration
- membrane
- time
- cycle
- 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.)
- Granted
Links
- 239000012528 membrane Substances 0.000 title claims abstract description 89
- 238000000926 separation method Methods 0.000 title claims description 16
- 238000001914 filtration Methods 0.000 claims abstract description 90
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 238000001514 detection method Methods 0.000 claims abstract description 9
- 238000000034 method Methods 0.000 claims 1
- 230000035939 shock Effects 0.000 abstract description 6
- 239000000126 substance Substances 0.000 description 17
- 239000012466 permeate Substances 0.000 description 16
- 238000004140 cleaning Methods 0.000 description 7
- 238000009792 diffusion process Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 238000001125 extrusion Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
(57)【要約】
【課題】 間欠運転を長期間継続しても運転操作が比較
的安定し、装置構成品に対する機械的なショックを比較
的小さくする。
【解決手段】 被処理液１４を満たした液槽１０に膜エ
レメント１６を浸漬し、この膜エレメント１６における
濾過操作と濾過停止とを繰り返す間欠運転を行うように
した膜分離装置において、膜エレメント１６の濾過操作
時における膜透過液の流量が一定となるように吸引す
る。この際の吸引圧力を圧力計２８で検出し、検出結果
に応じて制御器４２は間欠運転のサイクルを変化させ
る。
(57) [Summary] [PROBLEMS] To make operation operation relatively stable even if intermittent operation is continued for a long period of time, and to make mechanical shock to device components relatively small. SOLUTION: The membrane element 16 is immersed in a liquid tank 10 filled with a liquid 14 to be treated, and the membrane element 16 is intermittently operated in which a filtration operation and a filtration stop in the membrane element 16 are repeated. Is suctioned such that the flow rate of the membrane permeated liquid during the filtration operation is constant. The suction pressure at this time is detected by the pressure gauge 28, and the controller 42 changes the intermittent operation cycle according to the detection result.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は膜分離装置に係り、
特に被処理液を満たした液槽に膜エレメントを浸漬し、
被処理液を濾過するようにした膜分離装置に関する。TECHNICAL FIELD The present invention relates to a membrane separation device,
In particular, immerse the membrane element in a liquid tank filled with the liquid to be treated,
The present invention relates to a membrane separation device that filters a liquid to be treated.
【０００２】[0002]
【従来の技術】通常、この種の膜分離装置では、浸漬し
た膜エレメントの洗浄を目的として運転中に膜エレメン
トの下方に設置した散気手段から膜エレメントに向けて
散気を行う。また、散気による洗浄効果をより一層高め
るために、膜エレメントにおける濾過操作と濾過停止と
を頻繁に繰り返す間欠運転がしばしば採用されている。
間欠運転を行うと、濾過操作時に膜エレメントの膜面に
付着、堆積した付着物が濾過停止のたびに散気によって
膜面から剥離する。このため、運転を長時間継続しても
膜エレメントの閉塞の原因となるファウリング物質が蓄
積しにくく、膜透過液の透過流束を比較的安定に維持す
ることができる。このような間欠運転の効果は膜エレメ
ントに向けて散気を行わないにおいても程度の差はあ
れ、同様に得られると言われている。2. Description of the Related Art Generally, in this type of membrane separation device, air is diffused toward the membrane element from an air diffuser installed below the membrane element during operation for the purpose of cleaning the immersed membrane element. Further, in order to further enhance the cleaning effect by air diffusion, intermittent operation in which the filtration operation and the filtration stoppage in the membrane element are frequently repeated is often adopted.
When the intermittent operation is performed, the deposit adhered to and deposited on the membrane surface of the membrane element during the filtration operation is separated from the membrane surface by air diffusion every time filtration is stopped. Therefore, even if the operation is continued for a long time, the fouling substance that causes the clogging of the membrane element is hard to accumulate, and the permeation flux of the membrane permeate can be maintained relatively stable. It is said that the effect of such an intermittent operation can be obtained similarly to some extent even if air diffusion is not performed toward the membrane element.
【０００３】[0003]
【発明が解決しようとする課題】しかしながら、上述の
間欠運転を長期間継続すると、ファウリング物質が膜エ
レメントの濾過膜に徐々に蓄積し、濾過抵抗が次第に上
昇する傾向が見られる。濾過抵抗の上昇が進行すると、
上昇の程度が加速し正常な濾過操作を継続することが困
難になる場合がある。また、間欠運転のサイクルは被処
理液の性状や使用する濾過膜の種類などの処理条件によ
って決定されるが、運転初期に設定した間欠運転のサイ
クルが常に最適であるとは限らない。すなわち、間欠運
転のサイクル時間を長くすると運転操作が安定し、装置
構成品に対する機械的なショックが小さい利点がある反
面、濾過抵抗の上昇傾向が強まる欠点がある。一方、間
欠運転のサイクル時間を短くすると運転操作が煩雑化
し、装置構成品に対する機械的なショックが頻繁になる
欠点があるが、濾過抵抗の上昇傾向が比較的小さい利点
がある。本発明の目的は上記従来技術の問題点を改善
し、間欠運転のサイクルを適正に制御することによっ
て、間欠運転を長期間継続しても運転操作が比較的安定
し、装置構成品に対する機械的なショックが比較的小さ
く、かつ、濾過抵抗の上昇傾向が比較的小さい膜分離装
置を提供することにある。However, when the above intermittent operation is continued for a long period of time, the fouling substance gradually accumulates in the filtration membrane of the membrane element, and the filtration resistance tends to gradually increase. As the filtration resistance increases,
The degree of rise may be accelerated and it may be difficult to continue normal filtration operation. Further, the intermittent operation cycle is determined by the processing conditions such as the properties of the liquid to be treated and the type of filtration membrane used, but the intermittent operation cycle set at the initial stage of operation is not always optimal. That is, when the cycle time of the intermittent operation is lengthened, the operation is stabilized and the mechanical shock to the components of the apparatus is small, but on the other hand, there is the drawback that the tendency of the filtration resistance to increase increases. On the other hand, when the cycle time of the intermittent operation is shortened, the operation becomes complicated, and mechanical shocks to the components of the apparatus are frequently generated, but there is an advantage that the tendency of increasing the filtration resistance is relatively small. The object of the present invention is to improve the above-mentioned problems of the prior art, and by appropriately controlling the cycle of intermittent operation, the operation is relatively stable even when the intermittent operation is continued for a long period of time, and the mechanical components for the device components are mechanically controlled. The purpose of the present invention is to provide a membrane separation device having a relatively small shock and a relatively small tendency of increasing the filtration resistance.
【０００４】[0004]
【課題を解決するための手段】上記の課題を解決するた
めに、本発明に係る膜分離装置は、被処理液を満たした
液槽に膜エレメントを浸漬し、この膜エレメントにおけ
る濾過操作と濾過停止とを繰り返す間欠運転を行うよう
にした膜分離装置において、前記膜エレメントの濾過操
作時における濾過抵抗を検出する検出手段と、この検出
手段の検出結果に応じて前記間欠運転のサイクルを変化
させる制御手段とを具備したことを特徴とする。In order to solve the above-mentioned problems, the membrane separation apparatus according to the present invention immerses the membrane element in a liquid tank filled with the liquid to be treated, and performs filtration operation and filtration in this membrane element. In a membrane separation device configured to perform intermittent operation that repeats stopping and stopping, detecting means for detecting filtration resistance during filtration operation of the membrane element, and changing the cycle of intermittent operation according to the detection result of this detecting means. And a control means.
【０００５】前記検出手段は前記膜エレメントの濾過操
作時における膜透過液の流量が一定となるように吸引し
た際の吸引圧力を検出する手段であることが好ましい。
また、前記制御手段は膜エレメントの濾過抵抗が設定値
を超えた時に、１サイクルにおける濾過操作と濾過停止
の時間比を一定に維持しつつ、間欠運転のサイクル時間
を短縮するように制御することが好ましい。また、前記
制御手段は前記被処理液の性状を加味して前記サイクル
を制御することが好ましい。It is preferable that the detecting means is a means for detecting the suction pressure when the membrane permeate is sucked so that the flow rate of the membrane element during the filtration operation is constant.
Further, when the filtration resistance of the membrane element exceeds a set value, the control means controls so as to shorten the cycle time of intermittent operation while maintaining a constant time ratio of filtration operation and filtration stop in one cycle. Is preferred. Further, it is preferable that the control means controls the cycle in consideration of the properties of the liquid to be treated.
【０００６】[0006]
【発明の実施の形態】図１は本発明に係る膜分離装置の
実施形態を示す装置系統図である。液槽１０は液供給ラ
イン１２から供給された被処理液１４で満たされてい
る。液槽１０の内部には浸漬式の膜エレメント１６が配
設されている。膜エレメント１６を構成する濾過膜とし
ては、例えば平膜、中空糸膜が好ましく用いられる。膜
エレメント１６の下方には散気管１８が配設されてい
る。散気管１８は空気供給ライン２０を介してブロワ２
２に接続されている。ブロワ２２からの圧縮空気が散気
管１８に供給されると、散気管１８はこの空気を微細な
気泡として被処理液中に散気する。この時の散気エネル
ギによって被処理液が攪拌され、膜エレメント１６の膜
面が洗浄される。1 is a system diagram showing an embodiment of a membrane separation device according to the present invention. The liquid tank 10 is filled with the liquid to be treated 14 supplied from the liquid supply line 12. A submerged membrane element 16 is arranged inside the liquid tank 10. As the filtration membrane constituting the membrane element 16, for example, a flat membrane or a hollow fiber membrane is preferably used. An air diffuser 18 is arranged below the membrane element 16. The air diffuser 18 is connected to the blower 2 via the air supply line 20.
Connected to 2. When the compressed air from the blower 22 is supplied to the air diffusing tube 18, the air diffusing tube 18 diffuses this air into the liquid to be treated as fine bubbles. The liquid to be treated is stirred by the diffused energy at this time, and the membrane surface of the membrane element 16 is washed.
【０００７】膜エレメント１６の二次側２４には膜透過
液を抜き出すための透過液排出ライン２６が接続し、透
過液排出ライン２６には圧力計２８、切替弁３０、吸引
ポンプ３２及び流量計３４が設けられている。また、透
過液排出ライン２６には切替弁３６を介して薬液供給ラ
イン３８が接続され、薬液タンク４０内の薬液が膜エレ
メント１６の二次側２４に流入可能とされている。A permeate discharge line 26 for extracting the membrane permeate is connected to the secondary side 24 of the membrane element 16, and a pressure gauge 28, a switching valve 30, a suction pump 32 and a flow meter are connected to the permeate discharge line 26. 34 are provided. Further, a chemical liquid supply line 38 is connected to the permeated liquid discharge line 26 via a switching valve 36 so that the chemical liquid in the chemical liquid tank 40 can flow into the secondary side 24 of the membrane element 16.
【０００８】符号４２は間欠運転を実行するための制御
器であり、制御器４２には圧力計２８及び被処理液１４
の性状を把握するための計器４４の検出値が入力され、
制御器４２からの制御信号が切替弁３０、吸引ポンプ３
２及び切替弁３６に出力される。Reference numeral 42 is a controller for executing the intermittent operation, and the controller 42 has a pressure gauge 28 and a liquid 14 to be treated.
The detection value of the instrument 44 for grasping the property of
The control signal from the controller 42 is the switching valve 30, the suction pump 3
2 and the switching valve 36.
【０００９】上記の構成において、被処理液１４が液供
給ライン１２から一定流量で液槽１０に供給される。濾
過操作時には被処理液１４が吸引ポンプ３２の駆動によ
って膜エレメント１６の二次側２４に吸引され、濾過膜
を透過した膜透過液は透過液排出ライン２６、吸引ポン
プ３２、流量計３４を経て装置外に排出される。この
際、供給された被処理液１４と見合った量の膜透過液が
吸引されるように、すなわち、流量計３４の指示値が所
定の一定値となるように吸引ポンプ３２が回転数制御に
よって駆動される。したがって、液槽１０の液面はほぼ
一定のレベルに維持される。In the above structure, the liquid to be treated 14 is supplied from the liquid supply line 12 to the liquid tank 10 at a constant flow rate. During the filtration operation, the liquid to be treated 14 is sucked to the secondary side 24 of the membrane element 16 by driving the suction pump 32, and the membrane permeated liquid that has permeated the filtration membrane passes through the permeated liquid discharge line 26, the suction pump 32, and the flow meter 34. It is discharged to the outside of the device. At this time, the suction pump 32 is controlled by the rotation speed so that an amount of the membrane-permeated liquid corresponding to the supplied liquid to be treated 14 is sucked, that is, the indicated value of the flow meter 34 becomes a predetermined constant value. Driven. Therefore, the liquid level in the liquid tank 10 is maintained at a substantially constant level.
【００１０】制御器４２は膜分離装置を間欠運転するた
めに切替弁３０と吸引ポンプ３２のオンオフを制御す
る。すなわち、濾過操作時には切替弁３０を開とし、吸
引ポンプ３２を作動させる。濾過停止時には切替弁３０
を閉とし、吸引ポンプ３２を停止させる。制御器４０は
タイマを内蔵しており、濾過操作と濾過停止の時間を任
意に設定できる。濾過操作時おける吸引圧力は圧力計２
８によって検出され、検出値が制御器４０に入力され
る。この圧力計２８によって検出される吸引圧力が、膜
透過液の流量が所定の一定値となるように運転した際の
膜エレメント１６の濾過抵抗を間接的に意味している。
なお、上記の吸引圧力は相対的な指標であり、膜透過液
の流量に応じて大幅に変化することはいうまでもない。The controller 42 controls on / off of the switching valve 30 and the suction pump 32 in order to intermittently operate the membrane separation device. That is, during the filtering operation, the switching valve 30 is opened and the suction pump 32 is operated. Switching valve 30 when filtration is stopped
Is closed and the suction pump 32 is stopped. The controller 40 has a built-in timer so that the time for filtering operation and the time for stopping filtering can be set arbitrarily. The suction pressure during filtration operation is pressure gauge 2
8 and the detected value is input to the controller 40. The suction pressure detected by the pressure gauge 28 indirectly means the filtration resistance of the membrane element 16 when the membrane permeate is operated so that the flow rate of the membrane permeate becomes a predetermined constant value.
Needless to say, the above suction pressure is a relative index, and changes significantly depending on the flow rate of the membrane permeate.
【００１１】図２は本実施形態における間欠運転の一例
をモデル化して示した説明図であり、横軸は経過時間を
示し、縦軸は吸引圧力を示す。運転開始のＴ0時は間欠
運転のサイクル時間がなるべく長くなるように設定され
る。例えばサイクル時間を３０分とし、この時の１サイ
クルにおける濾過操作の時間を２７分、濾過停止の時間
を３分に設定する。この時の１サイクルにおける濾過操
作と濾過停止の時間比は９：１である。このようなサイ
クルで運転すると濾過開始時にＳ1であった吸引圧力が
濾過操作の過程で徐々に上昇し、２７分後の濾過停止直
前時にはＳ2になる。次に、３分間の濾過停止によって
膜エレメント１６が洗浄され、濾過抵抗が回復して低下
する。すなわち、この濾過停止の間でも散気管１８から
の散気が継続されるので、膜エレメント１６の濾過膜面
に付着、堆積した付着物が膜面から剥離し、効果的な洗
浄が行われる。したがって、次の濾過開始時での吸引圧
力Ｓ1は１サイクル前の濾過開始時での吸引圧力Ｓ1と同
程度の値に低下する。しかしながら、濾過停止によって
は濾過抵抗を完全に回復させることは困難である。この
ため、吸引圧力Ｓ1はサイクルを繰り返すごとに徐々に
上昇する。また、濾過停止直前時の吸引圧力Ｓ2も吸引
圧力Ｓ1に追随してサイクルを繰り返すごとに徐々に上
昇する。吸引圧力が大きくなればなるほど、濾過膜の閉
塞をもたらすファウリング物質が濾過膜内に浸透し易く
なり、濾過抵抗の上昇が加速する。FIG. 2 is an explanatory view showing a modeled example of the intermittent operation in the present embodiment. The horizontal axis shows the elapsed time and the vertical axis shows the suction pressure. At the time T 0 of the operation start, the cycle time of the intermittent operation is set to be as long as possible. For example, the cycle time is set to 30 minutes, the filtration operation time in one cycle is set to 27 minutes, and the filtration stop time is set to 3 minutes. At this time, the time ratio between the filtration operation and the filtration stop in one cycle is 9: 1. When operated in such a cycle, the suction pressure, which was S 1 at the start of filtration, gradually increases in the course of the filtration operation, and becomes S 2 just after stopping filtration after 27 minutes. Then, the membrane element 16 is washed by stopping the filtration for 3 minutes, and the filtration resistance is recovered and lowered. That is, since the air diffusion from the air diffuser 18 is continued even during the stop of the filtration, the adhered substances deposited and accumulated on the filtration membrane surface of the membrane element 16 are separated from the membrane surface, and effective cleaning is performed. Therefore, the suction pressure S 1 at the start of the next filtration is reduced to a value similar to the suction pressure S 1 at the start of the filtration one cycle before. However, it is difficult to completely recover the filtration resistance by stopping the filtration. Therefore, the suction pressure S 1 gradually rises each time the cycle is repeated. The suction pressure S 2 immediately before the stop of the filtration also follows the suction pressure S 1 and gradually increases each time the cycle is repeated. The higher the suction pressure, the easier the fouling substance that causes the clogging of the filtration membrane to permeate into the filtration membrane, and the increase in filtration resistance is accelerated.
【００１２】したがって、本実施の形態では濾過抵抗の
上昇が加速しにくいレベルの吸引圧力の許容値Ｘを設定
しておき、前記濾過停止直前時の吸引圧力Ｓ2がこの許
容値Ｘを超えたＴ1時に、間欠運転のサイクル時間を短
縮するように制御する。すなわち、次回のサイクルから
はサイクル時間を２０分とし、この時の１サイクルにお
ける濾過操作の時間を１８分、濾過停止の時間を２分に
設定する。この時の１サイクルにおける濾過操作と濾過
停止の時間比は今までのサイクルと同様に９：１であ
る。したがって、サイクル時間を短縮しても膜透過液の
流量を今までのサイクルと同様に所定の一定値に維持す
ることができ、処理装置としての安定性を確保できる。
また、サイクル時間の短縮によって濾過停止直前時の吸
引圧力Ｓ2が許容値Ｘを十分に下回る低い値で運転する
ことができる。このため、濾過開始時の吸引圧力Ｓ1の
上昇も低く抑えることができる。Therefore, in the present embodiment, the suction pressure allowable value X is set to a level at which the increase of the filtration resistance is hard to accelerate, and the suction pressure S 2 immediately before the stop of the filtration exceeds the allowable value X. At time T 1 , control is performed so as to shorten the cycle time of intermittent operation. That is, the cycle time is set to 20 minutes from the next cycle, the filtration operation time in one cycle at this time is set to 18 minutes, and the filtration stop time is set to 2 minutes. At this time, the time ratio between the filtration operation and the filtration stop in one cycle is 9: 1 as in the previous cycles. Therefore, even if the cycle time is shortened, the flow rate of the membrane permeate can be maintained at a predetermined constant value as in the conventional cycles, and the stability as a processing apparatus can be secured.
Further, by shortening the cycle time, the suction pressure S 2 immediately before the stop of filtration can be operated at a low value sufficiently lower than the allowable value X. Therefore, the rise in suction pressure S 1 at the start of filtration can be suppressed to a low level.
【００１３】しかしながら、上記のサイクル時間の短縮
を実行してもサイクル数を重ねると、濾過開始時の吸引
圧力Ｓ1と濾過停止直前時の吸引圧力Ｓ2の双方が徐々に
上昇する。したがって、濾過停止直前時の吸引圧力Ｓ2
が許容値Ｘを超えたＴ2時に、間欠運転のサイクル時間
を再度、短縮するように制御する。すなわち、次回のサ
イクルからはサイクル時間を１０分とし、この時の１サ
イクルにおける濾過操作の時間を９分、濾過停止の時間
を１分に設定する。この時の１サイクルにおける濾過操
作と濾過停止の時間比は今までのサイクルと同様に９：
１である。この再度のサイクル時間の短縮によって、再
び、吸引圧力が許容値Ｘを超えない範囲内での安定な間
欠運転が可能となる。However, even if the cycle time is shortened as described above, when the number of cycles is increased, both the suction pressure S 1 at the start of filtration and the suction pressure S 2 immediately before the stop of filtration gradually increase. Therefore, the suction pressure S 2 just before the filtration is stopped
When T 2 exceeds the allowable value X, the intermittent operation cycle time is controlled to be shortened again. That is, the cycle time is set to 10 minutes from the next cycle, the filtration operation time in one cycle at this time is set to 9 minutes, and the filtration stop time is set to 1 minute. At this time, the time ratio between the filtration operation and the filtration stop in one cycle was 9: as in the previous cycles.
It is 1. By shortening the cycle time again, stable intermittent operation can be performed again within the range where the suction pressure does not exceed the allowable value X.
【００１４】濾過停止直前時の吸引圧力Ｓ2が許容値Ｘ
を超えたＴ3時では、最早、間欠運転のみでは濾過抵抗
の回復が困難と判断できるので、制御器４２は間欠運転
を停止し、膜エレメント１６の薬液洗浄に切り替える。
すなわち、図１において切替弁３０を閉とし、吸引ポン
プ３２を停止させた濾過停止の状態から、切替弁３６を
開とする。すると薬液タンク４０内の薬液がその水頭差
によって薬液供給ライン３８、切替弁３６を介して透過
液排出ライン２６に逆流し、薬液が膜エレメント１６の
二次側２４に流入する。この薬液の流入によって膜エレ
メント１６が薬液洗浄され、濾過抵抗がほぼ運転初期の
低い状態にまで回復する。薬液洗浄が終了すると、切替
弁３６を閉とした後、図２に示した間欠運転の開始時Ｔ
0に戻る。The suction pressure S 2 immediately before the filtration is stopped is the allowable value X.
At time T 3 that exceeds T3, it can be determined that it is difficult to recover the filtration resistance only by the intermittent operation. Therefore, the controller 42 stops the intermittent operation and switches to the chemical solution cleaning of the membrane element 16.
That is, in FIG. 1, the switching valve 30 is closed, and the switching valve 36 is opened from the filtration stopped state in which the suction pump 32 is stopped. Then, the chemical liquid in the chemical liquid tank 40 flows back to the permeated liquid discharge line 26 via the chemical liquid supply line 38 and the switching valve 36 due to the difference in water head, and the chemical liquid flows into the secondary side 24 of the membrane element 16. The inflow of the chemical liquid causes the membrane element 16 to be cleaned with the chemical liquid, and the filtration resistance is restored to a low state at the beginning of operation. When the chemical cleaning is completed, the switching valve 36 is closed, and then the intermittent operation start time T shown in FIG.
Return to 0 .
【００１５】このように本実施形態によれば、時間経過
がＴ0〜Ｔ1のＡ期間ではサイクル時間が最も長い間欠運
転、Ｔ1〜Ｔ2のＢ期間ではサイクル時間が中程度の間欠
運転、Ｔ2〜Ｔ3のＣ期間ではサイクル時間が最も短い間
欠運転、Ｔ3以降に薬液洗浄をするように制御を繰り返
すので、吸引圧力が許容値Ｘを大幅に越えない範囲内で
比較的長期間にわたり安定した運転が可能となる。ま
た、各間欠運転の１サイクルにおける濾過操作と濾過停
止の時間比を一定に維持するようにしたので、サイクル
時間を短縮しても膜透過液の流量を所定の一定値に維持
することができ、処理装置としての安定性を確保でき
る。なお、図２において破線で示した操作線は吸引圧力
が許容値Ｘを超えても引き続き、サイクル時間が最も長
い間欠運転を継続した場合を例示したものである。この
ような場合には吸引圧力が急激に上昇し、比較的早い時
期に上限値Ｙに達する。上限値Ｙの状態では、薬液洗浄
を実施しても濾過抵抗を運転初期の低い状態にまで回復
させることは困難であり、大きな不利をもたらす。ま
た、サイクル時間が最も短い間欠運転を運転開始の当初
から実施した場合には運転操作が煩雑化し、装置構成品
に対する機械的なショックが頻繁になる。このため、装
置寿命を縮めたり、運転トラブルの頻度が多くなるとい
う不利を招く。As described above, according to this embodiment, the intermittent operation having the longest cycle time is performed in the period A of T 0 to T 1 , and the intermittent operation of the medium cycle time is performed in the period B of T 1 to T 2. , The control is repeated so that the cycle time is the shortest in the period C from T 2 to T 3 and the chemical cleaning is performed after T 3 , so that the suction pressure is relatively long within a range that does not significantly exceed the allowable value X. Stable operation is possible over a period of time. Further, since the time ratio between the filtration operation and the filtration stop in one cycle of each intermittent operation is maintained constant, the flow rate of the membrane permeate can be maintained at a predetermined constant value even if the cycle time is shortened. The stability of the processing device can be secured. The operation line shown by the broken line in FIG. 2 illustrates the case where the intermittent operation continues for the longest cycle time even if the suction pressure exceeds the allowable value X. In such a case, the suction pressure rises rapidly and reaches the upper limit value Y at a relatively early time. In the state of the upper limit value Y, it is difficult to recover the filtration resistance to the low state at the initial stage of operation even if the chemical cleaning is performed, which brings a great disadvantage. In addition, when the intermittent operation with the shortest cycle time is performed from the beginning of the operation, the operation becomes complicated, and mechanical shocks to the components of the apparatus become frequent. Therefore, there are disadvantages that the life of the device is shortened and the frequency of operating troubles increases.
【００１６】前記実施形態では制御器４２では膜透過液
の流量を一定に維持する条件で濾過停止直前時の吸引圧
力Ｓ2に基づいて間欠運転のサイクルを制御するように
した。しかしながら、本発明はこれに限らず、濾過開始
時の吸引圧力Ｓ1の上昇程度に応じて間欠運転のサイク
ルを制御するようにしてもよい。また、膜分離装置の用
途によっては膜エレメントへの吸引圧力や押出圧力を一
定に維持して運転する場合があり、膜エレメントの濾過
抵抗に変化に応じて膜透過液の流量が変化する運転とな
る。このような場合には膜エレメントの濾過抵抗を検出
する検出手段として膜透過液の流量計を用いればよい。
すなわち、濾過操作時に流量計で検出される膜透過液の
流量が設定値以下となった時に、膜エレメントの濾過抵
抗が許容上限値に達したとみなして、間欠運転のサイク
ル時間を短縮するように制御することになる。また、図
１に示したように制御器４２に被処理液１４の性状を把
握するための計器４４の検出値を入力し、制御器４２で
は被処理液１４の性状を加味して間欠運転のサイクルを
制御するようにしてもよい。たとえば、膜エレメントの
膜透過性能は被処理液の粘性に大きく関係する。また、
被処理液の粘性は組成が同一であっても液温によって変
化する。したがって、計器４４では液温を検出し、制御
器４２では液温との相関で被処理液の粘性を推定する。
そして、被処理液の粘性が低い時には間欠運転のサイク
ル時間を比較的長くし、粘性が高い時には間欠運転のサ
イクル時間を比較的短く設定する考え方を、前記膜エレ
メントの濾過抵抗に応じて間欠運転のサイクルを制御す
る際に加味する。このような、きめの細かな制御をすれ
ば、間欠運転をより一層実状に即した内容で実行でき
る。In the above embodiment, the controller 42 controls the intermittent operation cycle based on the suction pressure S 2 immediately before the filtration is stopped under the condition that the flow rate of the membrane permeate is kept constant. However, the present invention is not limited to this, and the cycle of intermittent operation may be controlled according to the degree of increase in suction pressure S 1 at the start of filtration. In addition, depending on the application of the membrane separation device, there may be a case where the suction pressure and the extrusion pressure to the membrane element are kept constant, and the operation is such that the flow rate of the membrane permeate changes according to the change in the filtration resistance of the membrane element. Become. In such a case, a flow meter of the membrane permeate may be used as the detection means for detecting the filtration resistance of the membrane element.
That is, when the flow rate of the membrane permeate detected by the flow meter during the filtration operation becomes equal to or less than the set value, it is considered that the filtration resistance of the membrane element has reached the allowable upper limit value, and the cycle time of the intermittent operation is shortened. Will be controlled. Further, as shown in FIG. 1, the detection value of the meter 44 for grasping the property of the liquid to be treated 14 is input to the controller 42, and the controller 42 takes the property of the liquid to be treated 14 into consideration to perform the intermittent operation. The cycle may be controlled. For example, the membrane permeation performance of the membrane element is greatly related to the viscosity of the liquid to be treated. Also,
The viscosity of the liquid to be treated varies depending on the liquid temperature even if the composition is the same. Therefore, the meter 44 detects the liquid temperature, and the controller 42 estimates the viscosity of the liquid to be treated in correlation with the liquid temperature.
Then, when the viscosity of the liquid to be treated is low, the cycle time of the intermittent operation is set to be relatively long, and when the viscosity is high, the cycle time of the intermittent operation is set to be relatively short, according to the filtration resistance of the membrane element. Take into account when controlling the cycle of. By performing such fine control, the intermittent operation can be executed with a more realistic content.
【００１７】[0017]
【発明の効果】本発明の膜分離装置によれば、膜エレメ
ントの濾過操作時における濾過抵抗に応じて間欠運転の
サイクルを適正に制御するようにした。このため、間欠
運転を長期間継続しても運転操作が比較的安定し、装置
構成品に対する機械的なショックが比較的小さく、か
つ、濾過抵抗の上昇傾向が比較的小さい。According to the membrane separation apparatus of the present invention, the cycle of intermittent operation is properly controlled according to the filtration resistance during the filtration operation of the membrane element. Therefore, even if the intermittent operation is continued for a long period of time, the driving operation is relatively stable, the mechanical shock to the device components is relatively small, and the increase tendency of the filtration resistance is relatively small.
【図１】本発明に係る膜分離装置の実施形態を示す装置
系統図である。FIG. 1 is a device system diagram showing an embodiment of a membrane separation device according to the present invention.
【図２】本実施形態における間欠運転の一例をモデル化
して示した説明図である。FIG. 2 is an explanatory view showing a modeled example of the intermittent operation in the present embodiment.
１０……液槽 １４……被処理液 １６……膜エレメント ２４……（膜エレメントの）二次側 ２６……透過液排出ライン ２８……圧力計 ３０……切替弁 ３２……吸引ポンプ ３４……流量計 ４２……制御器 10 ... Liquid tank 14 ... Liquid to be treated 16: Membrane element 24 ... Secondary side (of membrane element) 26 ... Permeate discharge line 28 ... pressure gauge 30 ... Switching valve 32 ... Suction pump 34 ... Flowmeter 42 ... Controller
Claims (4)
浸漬し、この膜エレメントにおける濾過操作と濾過停止
とを繰り返す間欠運転を行うようにした膜分離装置にお
いて、前記膜エレメントの濾過操作時における濾過抵抗
を検出する検出手段と、この検出手段の検出結果に応じ
て前記間欠運転のサイクルを変化させる制御手段とを具
備したことを特徴とする膜分離装置。1. A membrane separation apparatus in which a membrane element is immersed in a liquid tank filled with a liquid to be treated, and an intermittent operation in which the filtration operation and the filtration stoppage of the membrane element are repeated is performed. A membrane separation device comprising: a detection unit that detects the filtration resistance at the time, and a control unit that changes the cycle of the intermittent operation according to the detection result of the detection unit.
作時における膜透過液の流量が一定となるように吸引し
た際の吸引圧力を検出する手段であることを特徴とする
請求項１に記載の膜分離装置。2. The method according to claim 1, wherein the detection means is means for detecting a suction pressure at the time of suction so that the flow rate of the membrane permeated liquid during the filtration operation of the membrane element becomes constant. Membrane separator.
設定値を超えた時に、１サイクルにおける濾過操作と濾
過停止の時間比を一定に維持しつつ、間欠運転のサイク
ル時間を短縮するように制御することを特徴とする請求
項１又は請求項２に記載の膜分離装置。3. The control means shortens the cycle time of the intermittent operation while maintaining a constant time ratio between the filtration operation and the filtration stop in one cycle when the filtration resistance of the membrane element exceeds a set value. It controls, The membrane separation apparatus of Claim 1 or Claim 2 characterized by the above-mentioned.
して前記サイクルを制御することを特徴とする請求項１
乃至請求項３のいずれかに記載の膜分離装置。4. The control means controls the cycle in consideration of the properties of the liquid to be treated.
The membrane separation device according to claim 3.
Priority Applications (1)
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|---|---|---|---|
| JP2002077898A JP3744447B2 (en) | 2002-03-20 | 2002-03-20 | Membrane separator |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002077898A JP3744447B2 (en) | 2002-03-20 | 2002-03-20 | Membrane separator |
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| Publication Number | Publication Date |
|---|---|
| JP2003275548A true JP2003275548A (en) | 2003-09-30 |
| JP3744447B2 JP3744447B2 (en) | 2006-02-08 |
Family
ID=29205868
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|---|---|---|---|
| JP2002077898A Expired - Fee Related JP3744447B2 (en) | 2002-03-20 | 2002-03-20 | Membrane separator |
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