JPH06277455A - Operation of ultrafiltration membrane module - Google Patents
Operation of ultrafiltration membrane moduleInfo
- Publication number
- JPH06277455A JPH06277455A JP7006693A JP7006693A JPH06277455A JP H06277455 A JPH06277455 A JP H06277455A JP 7006693 A JP7006693 A JP 7006693A JP 7006693 A JP7006693 A JP 7006693A JP H06277455 A JPH06277455 A JP H06277455A
- Authority
- JP
- Japan
- Prior art keywords
- ultrafiltration
- soln
- pressure
- membrane module
- permeate
- 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.)
- Withdrawn
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明はＰＷＲ原子力プラント等
の廃液処理設備として用いられる廃液ほう酸処理装置も
しくは洗浄排水処理装置で使用する限外ろ過膜モジュー
ルの運転方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for operating an ultrafiltration membrane module used in a waste liquid boric acid treatment device or a cleaning waste water treatment device used as a waste liquid treatment facility of a PWR nuclear power plant or the like.
【０００２】[0002]
【従来の技術】従来技術として廃液ほう酸処理装置を例
にあげ、これを図３によって説明する。図３において、
処理廃液１は限外ろ過循環タンク２に供給され、限外ろ
過循環ポンプ３により限外ろ過供給液５として限外ろ過
膜モジュール４に供給され、廃液中の粒子状不純物を取
り除いた後、限外ろ過透過液７となって逆浸透タンク８
に送られ、一方、限外ろ過濃縮液６は前記限外ろ過循環
タンク２へ返送される。この限外ろ過透過液７を逆浸透
高圧ポンプ９により逆浸透供給液１１として逆浸透膜モ
ジュール１０に送り、ＳｉＯ2 等の不純物を取り除いた
逆浸透透過液１３が回収ほう酸として再使用される。な
お、図中、１２は逆浸透濃縮液である。2. Description of the Related Art As a prior art, a waste liquid boric acid processing apparatus will be taken as an example and described with reference to FIG. In FIG.
The treatment waste liquid 1 is supplied to the ultrafiltration circulation tank 2, supplied to the ultrafiltration membrane module 4 as the ultrafiltration supply liquid 5 by the ultrafiltration circulation pump 3, and after removing particulate impurities in the waste liquid, Outer filtration permeate 7 becomes reverse osmosis tank 8
On the other hand, the ultrafiltration concentrate 6 is returned to the ultrafiltration circulation tank 2. This ultrafiltration permeate 7 is sent to the reverse osmosis membrane module 10 as the reverse osmosis feed liquid 11 by the reverse osmosis high pressure pump 9, and the reverse osmosis permeate 13 from which impurities such as SiO 2 have been removed is reused as recovered boric acid. In the figure, 12 is a reverse osmosis concentrate.
【０００３】[0003]
【発明が解決しようとする課題】従来、限外ろ過膜モジ
ュールの運転は限外ろ過膜モジュール供給液側と透過液
側との圧力差を約２kg／cm2 G と一定にして行われてき
た。図４に限外ろ過透過流束の時間変化を示すが、初期
約３００リットル／ｍ2 ・ ｈ得られていた透過流束が約
５００時間後には必要流束である約７０リットル／ｍ2
・ ｈを下まわるまで急激に低下しており、限外ろ過膜は
約５００時間で交換を余儀なくされていた。この透過流
束の低下は膜面にスケールが堆積することにより起こっ
ているもので、膜面のスケーリングは限外ろ過膜モジュ
ールの供給液側と透過液側との圧力差が大きいことによ
り起因している。従って、この圧力差を小さくする必要
がある。Conventionally, the operation of the ultrafiltration membrane module has been performed with the pressure difference between the supply side and the permeate side of the ultrafiltration membrane module being kept constant at about 2 kg / cm 2 G. . Fig. 4 shows the time variation of the permeation flux of ultrafiltration. The permeation flux that was initially about 300 liters / m 2 · h was about 500 liters / m 2 which was the required flux after about 500 hours.
-It dropped sharply until it fell below h, and the ultrafiltration membrane had to be replaced in about 500 hours. This decrease in permeation flux is caused by the accumulation of scale on the membrane surface, and scaling of the membrane surface is caused by the large pressure difference between the feed liquid side and the permeate side of the ultrafiltration membrane module. ing. Therefore, it is necessary to reduce this pressure difference.
【０００４】本発明は上記技術水準に鑑み、限外ろ過膜
モジュールの運転寿命を延ばすことが可能な限外ろ過膜
モジュールの運転方法を提供しようとするものである。In view of the above-mentioned state of the art, the present invention is to provide an operating method of an ultrafiltration membrane module which can extend the operating life of the ultrafiltration membrane module.
【０００５】[0005]
【課題を解決するための手段】本発明は限外ろ過膜モジ
ュールの透過液側に背圧をかけて供給液側と透過液側の
圧力差を小さくすることにより膜面へのスケーリングを
低減し、長期にわたり安定した透過流束を得る限外ろ過
膜モジュールの運転方法において、透過液側に流量計及
び圧力制御弁を設け、運転初期には該圧力制御弁を制御
して透過液側の圧力を濃縮液側の圧力よりも高く設定す
ることにより、ろ過運転中においても膜モジュールの一
部で逆洗作用を生起させ、ろ過運転中流量計により透過
流の流量を監視しながら透過液流量がほゞ一定となるよ
うに圧力制御弁を徐々に開くことを特徴とする限外ろ過
膜モジュールの運転方法である。The present invention reduces the scaling to the membrane surface by applying a back pressure to the permeate side of the ultrafiltration membrane module to reduce the pressure difference between the feed and permeate sides. In a method of operating an ultrafiltration membrane module that obtains a stable permeation flux for a long period of time, a flow meter and a pressure control valve are provided on the permeate side, and the pressure control valve is controlled at the initial stage of operation to control the pressure on the permeate side. Is set higher than the pressure on the concentrate side, a backwash action occurs in a part of the membrane module even during filtration operation, and the permeate flow rate is monitored while monitoring the permeate flow rate with a flow meter during filtration operation. This is a method of operating an ultrafiltration membrane module, which is characterized by gradually opening a pressure control valve so that the pressure control valve becomes almost constant.
【０００６】[0006]
【作用】限外ろ過透過液側に圧力制御弁を設置すること
により、透過液側に背圧をかけ、供給液側との差圧を小
さくし、膜面へのスケールの堆積を減らす。また、透過
液側の圧力を濃縮液側よりも若干高くしておくことによ
り、膜の一部に透過液の濃縮側への逆洗を施し、スケー
リングの防止を図る。ただし、膜面にスケールが付着し
てくると透過液流量が落ちてくるので、透過液側に設け
た圧力制御弁を徐々に開いていくことにより、透過液側
の圧力も落ちることになる。従って逆洗の効果は運転終
了（膜寿命）までは続くものではない。[Function] By installing a pressure control valve on the ultrafiltration permeate side, a back pressure is applied to the permeate side to reduce the differential pressure between the permeate side and the feed liquid side and reduce the accumulation of scale on the membrane surface. Further, by making the pressure on the permeate side slightly higher than that on the concentrate side, a part of the membrane is backwashed to the concentrate side to prevent scaling. However, since the permeate flow rate decreases when scale adheres to the membrane surface, the pressure on the permeate side also drops by gradually opening the pressure control valve provided on the permeate side. Therefore, the effect of backwashing does not continue until the end of operation (membrane life).
【０００７】[0007]
【実施例】本発明の一実施例を図１によって説明する。
処理廃液１は限外ろ過循環タンク２に供給され、限外ろ
過循環ポンプ３により限外ろ過供給液５となって限外ろ
過モジュール４に供給され、廃液中の粒子状不純物を除
去する。この時、限外ろ過透過液７流量を流量計１５に
より検知し、所定流量となるように圧力制御弁１４をコ
ントロールする。限外ろ過濃縮液６は前記限外ろ過循環
タンク２に返送され、限外ろ過透過液７は逆浸透タンク
８に受けられ、逆浸透高圧ポンプ９により逆浸透供給液
１１となって逆浸透膜モジュール１０に供給され、Ｓｉ
Ｏ2 等の不純物を取り除いた逆浸透透過液１３が回収ほ
う酸として再使用される。なお、１２は逆浸透濃縮液で
ある。DESCRIPTION OF THE PREFERRED EMBODIMENTS An embodiment of the present invention will be described with reference to FIG.
The treatment waste liquid 1 is supplied to the ultrafiltration circulation tank 2, becomes the ultrafiltration supply liquid 5 by the ultrafiltration circulation pump 3, and is supplied to the ultrafiltration module 4 to remove particulate impurities in the waste liquid. At this time, the flow rate of the ultrafiltration permeate 7 is detected by the flow meter 15, and the pressure control valve 14 is controlled so that the flow rate becomes a predetermined value. The ultrafiltration concentrate 6 is returned to the ultrafiltration circulation tank 2, the ultrafiltration permeate 7 is received by the reverse osmosis tank 8, and the reverse osmosis high pressure pump 9 becomes the reverse osmosis feed liquid 11 to form the reverse osmosis membrane. Supplied to module 10, Si
The reverse osmosis permeate 13 from which impurities such as O 2 have been removed is reused as recovered boric acid. In addition, 12 is a reverse osmosis concentrate.
【０００８】図２に限外ろ過膜モジュール４の透過流束
を約７５リットル／ｍ2 ・ｈとなるように制御した時の
圧力の時間変化を示す。最初、透過液側圧力を濃縮液側
圧力よりも若干高く設定しておき、膜の一部透過液の濃
縮液側への逆洗を施す。膜の有効圧力差を図中のΔＰで
定義すると、ΔＰは運転初期０．４kg／cm2 G と従来の
運転圧力約２kg／cm2 G よりも１／５低い圧力差で運転
可能となっている。膜のスケーリングが進むと、透過液
流量が低下するので圧力制御弁１４が開いて、透過液流
量を確保する。従って透過液側の圧力は徐々に低下し、
併せて有効差圧ΔＰが大きくなる。１６００時間後に透
過液側と濃縮液側の圧力が同じになっており、透過液の
濃縮液側への逆洗の効果がこれ以降なくなるが、２４０
０時間後においても透過流束の低下は見られず、従来の
限外ろ過膜の運転寿命約５００時間よりも約５倍以上延
びている。FIG. 2 shows the time variation of the pressure when the permeation flux of the ultrafiltration membrane module 4 is controlled to be about 75 liter / m 2 · h. Initially, the pressure on the permeate side is set to be slightly higher than the pressure on the concentrate side, and a partial permeate of the membrane is backwashed to the concentrate side. If the effective pressure difference of the membrane is defined by ΔP in the figure, ΔP can be operated at a pressure difference of 0.4 kg / cm 2 G at the initial stage of operation and 1/5 lower than the conventional operating pressure of about 2 kg / cm 2 G. There is. As the membrane scaling proceeds, the permeate flow rate decreases and the pressure control valve 14 opens to ensure the permeate flow rate. Therefore, the pressure on the permeate side gradually decreases,
At the same time, the effective differential pressure ΔP increases. After 1600 hours, the pressures on the permeate side and the concentrate side were the same, and the effect of backwashing the permeate on the concentrate side disappeared thereafter.
No decrease in permeation flux was observed even after 0 hour, which is about 5 times longer than the operating life of the conventional ultrafiltration membrane of about 500 hours.
【０００９】なお、図２のデータは廃液として水道水に
酸化鉄（７ppm ）、界面活性剤（５ppm ）、油（１ppm
）を混合させた模擬廃水を使用し、限外ろ過膜として
は膜材質：ポリアクリロニトリル、分画分子量：１３０
０C.M.W のものを使用した場合の例である。The data in FIG. 2 shows that iron oxide (7 ppm), surfactant (5 ppm), oil (1 ppm) were added to tap water as waste liquid.
) Is used as the simulated waste water, and the ultrafiltration membrane is made of a membrane material: polyacrylonitrile, molecular weight cutoff: 130
This is an example of using 0C.MW.
【００１０】[0010]
【発明の効果】限外ろ過膜モジュールの供給液側と透過
液側の圧力差を小さくすること、及びその時の透過液側
の圧力は濃縮液側の圧力よりも高く設定する運転方法を
採用する本発明方法により、限外ろ過膜モジュールの運
転寿命を延ばすことが可能となる。The pressure difference between the supply side and the permeate side of the ultrafiltration membrane module is reduced, and the operating method is set so that the pressure on the permeate side at that time is set higher than the pressure on the concentrate side. The method of the present invention makes it possible to extend the operating life of the ultrafiltration membrane module.
【図１】本発明の一実施例の限外ろ過膜運転方法の説明
図。FIG. 1 is an explanatory diagram of an ultrafiltration membrane operating method according to an embodiment of the present invention.
【図２】本発明の一実施例の限外ろ過膜モジュールの透
過流束及び圧力の時間変化を示す図表。FIG. 2 is a chart showing changes with time of permeation flux and pressure of the ultrafiltration membrane module of one embodiment of the present invention.
【図３】従来の一態様の限外ろ過膜運転方法の説明図。FIG. 3 is an explanatory view of a conventional ultrafiltration membrane operation method.
【図４】従来の一態様の限外ろ過膜モジュールの透過流
束の時間変化を示す図表。FIG. 4 is a chart showing a change over time in permeation flux of an ultrafiltration membrane module according to a conventional aspect.
Claims (1)
をかけて供給液側と透過液側の圧力差を小さくすること
により膜面へのスケーリングを低減し、長期にわたり安
定した透過流束を得る限外ろ過膜モジュールの運転方法
において、透過液側に流量計及び圧力制御弁を設け、運
転初期には該圧力制御弁を制御して透過液側の圧力を濃
縮液側の圧力よりも高く設定することにより、ろ過運転
中においても膜モジュールの一部で逆洗作用を生起さ
せ、ろ過運転中流量計により透過流の流量を監視しなが
ら透過液流量がほゞ一定となるように圧力制御弁を徐々
に開くことを特徴とする限外ろ過膜モジュールの運転方
法。1. A back pressure is applied to the permeate side of the ultrafiltration membrane module to reduce the pressure difference between the feed liquid side and the permeate side, thereby reducing the scaling to the membrane surface and achieving stable permeation flow over a long period of time. In the method of operating the ultrafiltration membrane module for obtaining a bundle, a flow meter and a pressure control valve are provided on the permeate side, and the pressure control valve is controlled at the initial stage of operation so that the pressure on the permeate side is higher than the pressure on the concentrate side. By setting a high value, the backwashing action will occur in a part of the membrane module even during the filtration operation, and the permeate flow rate will be almost constant while monitoring the flow rate of the permeate flow during the filtration operation. A method of operating an ultrafiltration membrane module, characterized by gradually opening a pressure control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7006693A JPH06277455A (en) | 1993-03-29 | 1993-03-29 | Operation of ultrafiltration membrane module |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7006693A JPH06277455A (en) | 1993-03-29 | 1993-03-29 | Operation of ultrafiltration membrane module |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06277455A true JPH06277455A (en) | 1994-10-04 |
Family
ID=13420797
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7006693A Withdrawn JPH06277455A (en) | 1993-03-29 | 1993-03-29 | Operation of ultrafiltration membrane module |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06277455A (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005147788A (en) * | 2003-11-13 | 2005-06-09 | Inst Nuclear Energy Research Rocaec | Boric acid purification and reutilization system, and method, using reverse osmosis separation method |
| KR100687768B1 (en) * | 2005-04-12 | 2007-03-02 | 가부시키가이샤 웰시 | Water feed and distribution system and apparatus thereof |
| WO2010103679A1 (en) * | 2009-03-11 | 2010-09-16 | 三菱重工業株式会社 | Water desalination equipment and cleaning method for water desalination equipment |
| JP2014504879A (en) * | 2011-01-27 | 2014-02-27 | ジーイーエー メカニカル エクイップメント ゲーエムベーハー | Method for treating low-concentration distillation waste liquor and apparatus for producing protein-containing products |
| WO2015083773A1 (en) * | 2013-12-05 | 2015-06-11 | 三菱重工業株式会社 | Membrane separation device, circulated water utilization system |
| CN106448788A (en) * | 2016-12-02 | 2017-02-22 | 北京科泰兴达高新技术有限公司 | Deep purifying system of water quality polluted by radioactive substances |
| US9611161B2 (en) | 2013-12-05 | 2017-04-04 | Mitsubishi Hitachi Power Systems, Ltd. | Circulating water utilization system |
| US9783963B2 (en) | 2013-12-05 | 2017-10-10 | Mitsubishi Hitachi Power Systems, Ltd. | Safety device for circulating water utilization system and circulating-water utilization system |
| KR101870598B1 (en) * | 2017-05-18 | 2018-06-22 | 미츠비시 쥬코 칸쿄 카가쿠 엔지니어링 가부시키가이샤 | Biological treatment apparatus, biological treatment method, and program |
| US10315930B2 (en) | 2013-12-05 | 2019-06-11 | Mitsubishi Hitachi Power Systems, Ltd. | Method and system for remotely monitoring a group of circulating-water utilization systems |
| US10997673B2 (en) | 2013-12-05 | 2021-05-04 | Wota Group Llc | Charging device of circulating water utilization system and circulating-water utilization system |
-
1993
- 1993-03-29 JP JP7006693A patent/JPH06277455A/en not_active Withdrawn
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005147788A (en) * | 2003-11-13 | 2005-06-09 | Inst Nuclear Energy Research Rocaec | Boric acid purification and reutilization system, and method, using reverse osmosis separation method |
| KR100687768B1 (en) * | 2005-04-12 | 2007-03-02 | 가부시키가이샤 웰시 | Water feed and distribution system and apparatus thereof |
| WO2010103679A1 (en) * | 2009-03-11 | 2010-09-16 | 三菱重工業株式会社 | Water desalination equipment and cleaning method for water desalination equipment |
| JP2010207748A (en) * | 2009-03-11 | 2010-09-24 | Mitsubishi Heavy Ind Ltd | Desalination apparatus and method of washing the same |
| US9714267B2 (en) | 2011-01-27 | 2017-07-25 | Gea Mechanical Equipment Gmbh | Method for processing thin stillage and apparatus for producing a protein containing product |
| JP2014504879A (en) * | 2011-01-27 | 2014-02-27 | ジーイーエー メカニカル エクイップメント ゲーエムベーハー | Method for treating low-concentration distillation waste liquor and apparatus for producing protein-containing products |
| US9783963B2 (en) | 2013-12-05 | 2017-10-10 | Mitsubishi Hitachi Power Systems, Ltd. | Safety device for circulating water utilization system and circulating-water utilization system |
| US9611161B2 (en) | 2013-12-05 | 2017-04-04 | Mitsubishi Hitachi Power Systems, Ltd. | Circulating water utilization system |
| WO2015083773A1 (en) * | 2013-12-05 | 2015-06-11 | 三菱重工業株式会社 | Membrane separation device, circulated water utilization system |
| US10315930B2 (en) | 2013-12-05 | 2019-06-11 | Mitsubishi Hitachi Power Systems, Ltd. | Method and system for remotely monitoring a group of circulating-water utilization systems |
| US10997673B2 (en) | 2013-12-05 | 2021-05-04 | Wota Group Llc | Charging device of circulating water utilization system and circulating-water utilization system |
| CN106448788A (en) * | 2016-12-02 | 2017-02-22 | 北京科泰兴达高新技术有限公司 | Deep purifying system of water quality polluted by radioactive substances |
| KR101870598B1 (en) * | 2017-05-18 | 2018-06-22 | 미츠비시 쥬코 칸쿄 카가쿠 엔지니어링 가부시키가이샤 | Biological treatment apparatus, biological treatment method, and program |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A300 | Withdrawal of application because of no request for examination |
Free format text: JAPANESE INTERMEDIATE CODE: A300 Effective date: 20000530 |