JPS62180705A - Method for operating hollow yarn membrane filter - Google Patents
Method for operating hollow yarn membrane filterInfo
- Publication number
- JPS62180705A JPS62180705A JP2195286A JP2195286A JPS62180705A JP S62180705 A JPS62180705 A JP S62180705A JP 2195286 A JP2195286 A JP 2195286A JP 2195286 A JP2195286 A JP 2195286A JP S62180705 A JPS62180705 A JP S62180705A
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fiber membrane
- filtration
- membrane filter
- condensate
- 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 60
- 238000000034 method Methods 0.000 title claims description 11
- 238000001914 filtration Methods 0.000 claims abstract description 39
- 239000007787 solid Substances 0.000 claims abstract description 29
- 239000012510 hollow fiber Substances 0.000 claims description 55
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000004140 cleaning Methods 0.000 claims description 5
- 238000007599 discharging Methods 0.000 claims description 2
- 230000008961 swelling Effects 0.000 claims 1
- 238000011045 prefiltration Methods 0.000 abstract description 8
- 238000000746 purification Methods 0.000 abstract description 8
- 230000003247 decreasing effect Effects 0.000 abstract 2
- 238000005406 washing Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 9
- 238000010586 diagram Methods 0.000 description 6
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 239000003456 ion exchange resin Substances 0.000 description 3
- 229920003303 ion-exchange polymer Polymers 0.000 description 3
- 238000011017 operating method Methods 0.000 description 3
- 239000013535 sea water Substances 0.000 description 3
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 238000005056 compaction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000002901 radioactive waste Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 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、火力９ｇ子力発電所等において、復水及び廃
水等の浄化に使用する中空糸膜フィルタの運転方法に関
し、特に原子力発電所の水浄化に使用するに好適な中空
糸膜フィルタの運転方法に関する。[Detailed Description of the Invention] (Industrial Application Field) The present invention relates to a method of operating a hollow fiber membrane filter used for purifying condensate and wastewater in thermal 9g nuclear power plants, etc., and particularly in nuclear power plants. The present invention relates to a method of operating a hollow fiber membrane filter suitable for use in water purification.
従来の原子力発電所における復水浄化設備は、その復水
処理系のなかにプレフィルタとベッド型説塩器とを配設
するのが普通であり、このような蒸気タービン３を回転
させて発電機４で発電を行った後、復水器５に入り、海
水６により冷却され復水７となる。この復水中には配管
等の腐食による固形状やイオン状の不純物（酸化鉄が主
体である。）が含まれており１発電所の安全性、信頼性
向上のためには、これらの不純物を除去することが必要
である。そこで復水器５から復水ポンプ８を介して原子
炉１に至る流路中にプレフィルタ９及びベッド型説塩器
１０を設置し復水処理系を構□成している。Conventional condensate purification equipment in nuclear power plants usually includes a pre-filter and a bed-type salt generator in the condensate treatment system, and generates electricity by rotating such a steam turbine 3. After generating electricity in the machine 4, it enters the condenser 5, where it is cooled by seawater 6 and becomes condensate 7. This condensate water contains solid and ionic impurities (mainly iron oxide) due to corrosion of piping, etc.1 In order to improve the safety and reliability of the power plant, these impurities must be removed. It is necessary to remove it. Therefore, a pre-filter 9 and a bed-type salt analyzer 10 are installed in the flow path from the condenser 5 to the reactor 1 via the condensate pump 8 to constitute a condensate treatment system.
プレフィルタ９は、従来粉状イオン交換樹脂を濾□過助
材とするプリコート型フィルタであったが、最近、非助
材型のフィルタとして中空糸膜フィルタが採用されつつ
ある。このプレフィルタ９に復水を通水することによっ
て特に固形状の不純物の除去を行う。また、脱塩器１０
は、塔内に粒状のイオン交換樹脂を充填したもので、イ
オン状の不、、郷、物、特に復水器５から海水がリーク
した場合の・導素イオンの除去を目的としている。The prefilter 9 has conventionally been a precoat type filter that uses powdered ion exchange resin as a filtration aid, but recently, hollow fiber membrane filters are being adopted as non-aid filters. By passing condensate through this pre-filter 9, particularly solid impurities are removed. In addition, the desalination device 10
The column is filled with granular ion exchange resin, and its purpose is to remove ionic substances, especially conductive ions when seawater leaks from the condenser 5.
上記した復水処理設備は原子力発電プラントの低放射能
化に極めて大きく貢献している。しかし′：ながらプレ
フィルタ９がプリコート型フィルタの場合、プリコート
材の粉状イオン交換樹脂を使いゝ棄てにしているため、
廃樹脂による放射性廃棄物量の低減が課題であった。こ
のため助材を使用しない中空糸膜フィルタの実用化検討
が進められてきた。The above-mentioned condensate treatment equipment makes an extremely large contribution to lowering the radioactivity of nuclear power plants. However, if the pre-filter 9 is a pre-coated type filter, the powdered ion exchange resin of the pre-coated material is used and discarded.
The challenge was to reduce the amount of radioactive waste generated from waste resin. For this reason, studies have been underway to put hollow fiber membrane filters that do not use auxiliary materials into practical use.
中空糸膜フィルタは、例えば特開昭４９−９７６７ 。A hollow fiber membrane filter is disclosed in, for example, Japanese Patent Application Laid-Open No. 49-9767.
５６−７６２０８．５９−４４０３に公知例があるが、
第２図に示すように外径１＋ｍ程度の中空状の糸１４を
数千水束にし°て充填した中空糸膜モジュール１５を一
本又は複数本濾過塔１１に装着したもので、中空糸１４
の表面には０．１μｍ程度の微小な孔が多数おいており
、この面で液中の固形成分が有価物の場合分離回収し、
不要物の場合分離除去する。There is a known example in 56-76208.59-4403,
As shown in FIG. 2, one or more hollow fiber membrane modules 15 filled with several thousand water bundles of hollow fibers 14 with an outer diameter of approximately 1+ m are attached to the filtration tower 11.
There are many minute pores of about 0.1 μm on the surface, and if the solid components in the liquid are valuable, they can be separated and recovered.
Separate and remove unnecessary items.
原子力発電所の復水浄化では中空糸膜モジュール１５は
外径１００〜２００ ｍ 、長さ１〜２ｍで、復水は入
口１２から流入して中空糸膜モジユール１５内に入り、
中空糸膜モジュール１５の上部端面から膜透過水が出て
、出口１３から流出するようになっている。In condensate purification at a nuclear power plant, the hollow fiber membrane module 15 has an outer diameter of 100 to 200 m and a length of 1 to 2 m, and condensate flows in from the inlet 12 and enters the hollow fiber membrane module 15.
Membrane permeate water comes out from the upper end face of the hollow fiber membrane module 15 and flows out from the outlet 13.
ここで、中空糸膜フィルタの特長は中空糸の径が極めて
小さいため、濾過塔１１内に多数の中空糸を充填できる
ことである。従って、濾過面積が非常に大きく、同一処
理水量に対して単位膜面積当たりの処理量を小さくする
ことができるため、固形成分の捕捉に伴う濾過差圧上昇
が極めて小さくなる。しかしながら、中空糸シフィルタ
の短所は中空糸が極めて精密な膜であるため非常に高価
−二とである。従って、中空糸Ｑ使用量をできるだけ少
なくするよう、中空糸膜？イルタのコンパクト化、塔数
の削減が要望されてきた。Here, the feature of the hollow fiber membrane filter is that the diameter of the hollow fibers is extremely small, so that the filtration tower 11 can be filled with a large number of hollow fibers. Therefore, the filtration area is very large, and the amount of water to be treated per unit membrane area can be reduced for the same amount of water to be treated, so that the increase in filtration differential pressure due to the capture of solid components becomes extremely small. However, the disadvantage of hollow fiber filters is that they are very expensive because the hollow fibers are extremely precise membranes. Therefore, to minimize the amount of hollow fiber Q used, hollow fiber membranes should be used. There has been a demand for a more compact Ilter and a reduction in the number of towers.
［１１１１が解決しようとする間！Ｉａ）中空糸の使用
量の低減は濾過面積の減少につながり、単位面積当りの
固形成分負荷量が増大すること１：こなる。[While 1111 tries to solve it! Ia) Reduction in the amount of hollow fibers used leads to a decrease in the filtration area, and the amount of solid component loaded per unit area increases.1: This results.
、一般に中空糸膜フィルタは複数の塔で並列運転され、
処理水量が一定の定速濾過で運転される。Generally, hollow fiber membrane filters are operated in parallel with multiple towers.
It is operated with constant speed filtration where the amount of water to be treated is constant.
この場合、濾過差圧は固形成分９捕捉に伴い上昇するた
め、設定差圧に到達すると運転を中止し、膜の忰浄を行
う、膜の洗浄によ？固形成分をはく離し眸過差圧を低減
した後再度碍転を開始する６、この１：クイタルの時間
は運転操作上長い程良い力ｉ、＊速濾過におけるケーク
濾過理論からサイクル１Ｉ１１ｆｌＴは次式の関係が成
立すや。In this case, the filtration differential pressure increases as the solid component 9 is captured, so when the set differential pressure is reached, operation is stopped and the membrane is cleaned. After stripping off the solid components and reducing the differential pressure, the filtration starts again. 6. This 1: The longer the quill time, the better the force i. *Based on the theory of cake filtration in rapid filtration, cycle 1I11flT is calculated by the following formula: The relationship is established.
Ｔ＝Ｋ ・ ａｏ−” −Ｃ−” ・ （ＬＶ）−”こ
こでＫは定数、α０は固形成分の濾過比抵抗係数、Ｃは
固形成分濃度、ＬＶは濾過線流速である。この式から処
理する復水の水質が一定の場合。T=K ・ ao−” −C−” ・ (LV) − “Here, K is a constant, α0 is the filtration resistivity coefficient of the solid component, C is the solid component concentration, and LV is the filtration linear flow velocity. From this equation, When the quality of the condensate to be treated is constant.
サイクル時間は濾過線流速の二乗に反比例することがわ
かる。即ち、例えば中空糸の使用量を半減すると濾過線
流速は２倍になるため、サイクル時間は１／４に短縮す
ることになる。このように中空糸膜フィルタの塔のコン
パクト化や塔数削減はサイクル時間を大幅に減少させる
ため、、膜の洗浄を頻繁に行わなければならなと１問題
があった。It can be seen that the cycle time is inversely proportional to the square of the filtration line flow rate. That is, for example, if the amount of hollow fibers used is halved, the linear filtration flow rate will double, and therefore the cycle time will be shortened to 1/4. As described above, making the towers of hollow fiber membrane filters more compact and reducing the number of towers significantly reduces the cycle time, which poses a problem in that the membranes must be washed frequently.
本発明の目的は中空糸膜フざルタの線流速が高いにもか
かわらずサイクル時−ｅ短縮を極力防ぐことにある。An object of the present invention is to prevent shortening of cycle time -e as much as possible despite the high linear flow velocity of the hollow fiber membrane Fulta.
本発明の運転方法は、中空糸膜フィルタにより固形成分
を分離するに当たり５．洗浄設定差圧に到達する以前に
、運転を一旦停止するか、又は中空糸膜に付着した固成
形分が、膨諒しうる程度の濾過線流速に下げて緩慢な還
御操作を行い、、前記固形成分の膨潤後、再度定常運転
することを特徴とする。The operating method of the present invention includes 5. in separating solid components using a hollow fiber membrane filter. Before the set cleaning pressure difference is reached, either the operation is temporarily stopped, or the solid components adhering to the hollow fiber membrane are reduced to a filtration line flow rate that can swell, and a slow return operation is performed. After the solid component has swelled, steady operation is performed again.
本発明によれば、濾過差圧は停止前又は緩慢な運転前の
圧力に比べて低い状態から始まり、又、差圧上昇も遅く
なるという現象がこれ迄の濾過試験から明らかになって
いる。この現象は膜面に堆積した固形成分層の圧密状態
に関係するものと考えられ、運転停止により固形成分層
が膨潤し、固形成分層の濾過抵抗が減少するためと推察
される。According to the present invention, it has become clear from the filtration tests to date that the filtration differential pressure starts from a lower state than the pressure before stopping or slow operation, and the rise in the differential pressure is also slower. This phenomenon is thought to be related to the compaction state of the solid component layer deposited on the membrane surface, and is presumed to be because the solid component layer swells due to the stoppage of operation, and the filtration resistance of the solid component layer decreases.
又、固形成分層を膨潤させるには運転の停止の４王かに
濾過線流速を下げる方法もある。Further, in order to swell the solid component layer, there is also a method of lowering the filtration line flow rate by stopping the operation.
従って、これらを中空糸膜フィルタの運転方法に取入れ
れば、濾過差圧上昇が小さくなると考えられた。Therefore, it was thought that if these were incorporated into the operating method of the hollow fiber membrane filter, the increase in filtration differential pressure would be reduced.
本発明では中空糸膜フィルタを運転する場合、運転中に
一旦運転を停止又は濾過線流速を下げるが、その際、停
止又は濾過線流速を下げた塔の被処理水は中空糸膜フィ
ルタをバイパスさせるか。In the present invention, when operating a hollow fiber membrane filter, the operation is temporarily stopped or the filtration line flow rate is reduced, but at that time, the water to be treated in the tower that is stopped or the filtration line flow rate is reduced bypasses the hollow fiber membrane filter. Shall I let you?
又は他の塔の処理量を増加させることで対処できる。こ
の停止時間は極めて短くて良いので、処理水質や他の塔
の濾過差圧上昇に与える影響はほとんど無い。Alternatively, this can be dealt with by increasing the throughput of other towers. Since this stop time is extremely short, it has almost no effect on the quality of treated water or on the rise in filtration differential pressure in other columns.
以下、本発明の一実施例を第３図により説明する。原子
カプラントの復水浄化系のプレフィルタとして複数個の
中空糸膜フィルタ１８とバイパス管１９を並列に設置し
ている。それぞれの中空糸膜フィルタ１８とバイパスＩ
ｒ！１９は復水母管１６から分岐している。中空糸膜フ
ィルタ１８は復水母管１６の復水をそれぞれ等量、一定
流量で処理する。中空糸膜フィルタ１８の上流又は下流
側には処理流量を一定にするための流量調整弁１７が設
けられている。An embodiment of the present invention will be described below with reference to FIG. A plurality of hollow fiber membrane filters 18 and bypass pipes 19 are installed in parallel as pre-filters for the condensate purification system of the atomic couplant. Each hollow fiber membrane filter 18 and bypass I
r! 19 branches from the condensate main pipe 16. The hollow fiber membrane filter 18 processes the condensate from the condensate main pipe 16 in equal amounts and at a constant flow rate. A flow rate adjustment valve 17 is provided upstream or downstream of the hollow fiber membrane filter 18 to keep the processing flow rate constant.
この中空糸膜フイルタシステムにおいて１次のような運
転方法を考案した。即ち、各中空糸膜フィルタを一定流
量で運転するが、その内−塔のみを一旦停止する。その
際、その塔が処理していた復水はバイパス管１９でバイ
パスさせるが、又は他の塔に回して処理させる。停止さ
せた塔はすぐ運転を復起させ、運転状態を元に戻す、そ
の操作は一塔当たり、復水の場合月に１〜２回が望まし
い。又、停止時期は設定した濾過差圧で管理する。We devised the following operating method for this hollow fiber membrane filter system. That is, each hollow fiber membrane filter is operated at a constant flow rate, but only the inner column is temporarily stopped. At this time, the condensate that was being treated by that column is bypassed through the bypass pipe 19 or sent to another column for treatment. The stopped tower should be immediately restarted to return to its original operating state. This operation should preferably be done per tower, or once or twice a month in the case of condensate water. In addition, the stop timing is controlled by the set filtration differential pressure.
停止時間は１時間以内とする。このように中空糸膜フィ
ルタの濾過差圧が洗浄設定差圧に到達する迄この操作を
一回以上行うことにより各省の濾過差圧上昇を極力小さ
くすることができる。Stoppage time shall be within one hour. In this way, by performing this operation one or more times until the filtration differential pressure of the hollow fiber membrane filter reaches the cleaning set differential pressure, the increase in filtration differential pressure in each province can be minimized as much as possible.
本発明の効果を第４図に示す、中空糸膜フィルタ（ポア
サイズ０．１μｍ） を用い、濾過線流速０ 、４ ｍ
／ ｈ で試験した結果である。固形成分はＦｅ（Ｏ
Ｈ）ａを用い濃度１ｐｐｓｏａｓＦｅで純水中に分散さ
せて模擬復水とした。膜洗浄の濾過差圧上昇を０．５ｋ
ｇ／ｆｆｌに設定したが、その圧力に従来法では約６時
間で達した。それに対して本発明法では差圧上昇が０．
２ｋｇ／ｃｄに達した時期に運転を一旦停止した。５分
間の停止後再度運転を始めたところ、初期の濾過差圧は
停止直前の圧力より低く、又、差圧上昇も緩やかになっ
た。その結果、０．５ｋＩＣ／ｄの差圧上昇迄従来法の
約１．５倍の時間を要した。次に第５図に示すように停
止回数を３回にしたところ更に運転寿命が延長され。The effect of the present invention is shown in Fig. 4, using a hollow fiber membrane filter (pore size 0.1 μm) at a linear filtration flow rate of 0.4 m.
This is the result of testing at /h. The solid component is Fe(O
H) a was dispersed in pure water at a concentration of 1 ppsoasFe to provide simulated condensate. Increase in filtration differential pressure during membrane cleaning by 0.5k
g/ffl, and that pressure was reached in about 6 hours using the conventional method. On the other hand, in the method of the present invention, the differential pressure rise is 0.
Operation was temporarily stopped when it reached 2 kg/cd. When the operation was started again after stopping for 5 minutes, the initial filtration differential pressure was lower than the pressure immediately before stopping, and the rise in the differential pressure was also gradual. As a result, it took about 1.5 times as long as the conventional method until the differential pressure increased to 0.5 kIC/d. Next, as shown in Figure 5, when the number of stops was increased to three, the operating life was further extended.
約２倍となった。このように本発明が中空糸膜フィルタ
の運転寿命の延長に多大の効果のあることが確認された
。It has approximately doubled. Thus, it was confirmed that the present invention has a great effect on extending the operating life of hollow fiber membrane filters.
次に、本発明の効果を更に向上させるには、中空糸膜フ
ィルタの運転を一旦停止する場合において、停止中に中
空糸膜に捕捉された固形成分を水圧又は空気によっては
く離させる方法がある。はく離した固形成分は濾過塔外
に排出することなしに再度運転を開始する。これにより
再運転時の濾過差圧は更に低くなり、−サイクルが終了
する時間がより延長する。中空糸膜面から固形成分のは
く離を行う方法として実施例を第６図に示す。空気配管
２０から供給される空気を中空糸膜フイルタ１８内に吹
き込んで中空糸膜面に捕捉されている固形成分を空気低
木により攪拌、はく離させるものである。使用済み空気
はベント管２２から排出される。Next, in order to further improve the effects of the present invention, when the operation of the hollow fiber membrane filter is temporarily stopped, there is a method in which the solid components captured by the hollow fiber membrane are removed by water pressure or air during the stoppage. The operation is restarted without discharging the separated solid components to the outside of the filtration tower. As a result, the filtration differential pressure upon restarting becomes even lower, and the time it takes for the cycle to complete is extended. An example is shown in FIG. 6 as a method for stripping solid components from the hollow fiber membrane surface. Air supplied from the air pipe 20 is blown into the hollow fiber membrane filter 18, and the solid components captured on the hollow fiber membrane surface are agitated and peeled off by the air shrub. Spent air is exhausted through vent pipe 22.
本発明によれば、中空糸膜フィルタの濾過線流速を高く
しても膜の洗浄迄の運転時間の短縮を極力防ぐことがで
きるので、中空糸膜フィルタのコンパクト化や塔数の削
除が可能となり、中空糸膜フィルタのコストを大幅に低
減させる効果がある。According to the present invention, even if the linear filtration flow rate of the hollow fiber membrane filter is increased, it is possible to prevent shortening of the operating time until cleaning the membrane as much as possible, making it possible to downsize the hollow fiber membrane filter and eliminate the number of columns. This has the effect of significantly reducing the cost of hollow fiber membrane filters.
、、第１図は原子カプラントの概略図を示すもので、復
水浄化設備の一例を説明するための図、第２図は中空糸
膜フィルタの断面図、第３図は本発明の一実施例に用い
た復水浄化設備の概略図、第４図、は本発明の効果を示
す図、第５図は本発明の一層、の効果を示すグラフ、第
６図は他の実施例を示す復水浄化設備の概略図である。
１・・・原子炉、２・・・蒸気、３・・・蒸気タービン
、４・・・発電機、５・・・復水器、６・・・海水、７
・・・復水、８・・・復水ポンプ、９・・・プレフィル
タ、１０・・・脱塩器。
１１・・・濾過塔、１２・・・水入口、１３・・・水出
口。
↓４・・・中空糸、１５・・・中空糸膜モジュール、１
６・ｉ・復水母管、１７・・・流量調整弁、１８・・・
中空糸膜フィルタ、１９・・・バイパス管、２０・・・
空気配管、２１・・・開閉弁、２２・・・ベント！。,, Fig. 1 shows a schematic diagram of an atomic couplant and is a diagram for explaining an example of condensate purification equipment, Fig. 2 is a cross-sectional view of a hollow fiber membrane filter, and Fig. 3 shows an example of an implementation of the present invention. A schematic diagram of the condensate purification equipment used in the example, FIG. 4 is a diagram showing the effect of the present invention, FIG. 5 is a graph showing the further effect of the present invention, and FIG. 6 is a diagram showing another embodiment. It is a schematic diagram of a condensate purification facility. 1... Nuclear reactor, 2... Steam, 3... Steam turbine, 4... Generator, 5... Condenser, 6... Seawater, 7
...Condensate, 8...Condensate pump, 9...Prefilter, 10...Demineralizer. 11...Filtering tower, 12...Water inlet, 13...Water outlet. ↓4...Hollow fiber, 15...Hollow fiber membrane module, 1
6.i. Condensate main pipe, 17...Flow rate adjustment valve, 18...
Hollow fiber membrane filter, 19... bypass pipe, 20...
Air piping, 21...on/off valve, 22...vent! .
Claims (1)
り、洗浄設定差圧に到達する以前に、運転を一旦停止す
るか、又は中空糸膜に付着した固成形分が膨潤しうる程
度の濾過線流速に下げて緩慢な運転操作を行い前記固形
成分の膨潤後、再度定常運転することを特徴とする中空
糸膜フィルタの運転方法。 ２、前記操作を２回以上行うことを特徴とする特許請求
の範囲第１項記載の中空糸膜フィルタの運転方法。 ３、中空糸膜フィルタの運転を一旦停止している間、中
空糸膜に捕捉された固形成分を水又は空気ではく離させ
、固形成分を塔外に排出することなく再度運転を継続す
ることを特徴とする特許請求の範囲第１項又は第２項記
載の中空糸膜フィルタの運転方法。[Claims] 1. When separating solid components using a hollow fiber membrane filter, the operation must be temporarily stopped or the solid components attached to the hollow fiber membrane may swell before the cleaning set differential pressure is reached. 1. A method for operating a hollow fiber membrane filter, which comprises: reducing the filtration line flow velocity to a level where the flow rate is low, performing slow operation, and after swelling the solid component, performing steady operation again. 2. The method for operating a hollow fiber membrane filter according to claim 1, wherein the operation is performed twice or more. 3. While the operation of the hollow fiber membrane filter is temporarily stopped, the solid components captured by the hollow fiber membrane are removed with water or air, and the operation can be continued again without discharging the solid components outside the column. A method for operating a hollow fiber membrane filter according to claim 1 or 2, characterized in that:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2195286A JPS62180705A (en) | 1986-02-05 | 1986-02-05 | Method for operating hollow yarn membrane filter |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2195286A JPS62180705A (en) | 1986-02-05 | 1986-02-05 | Method for operating hollow yarn membrane filter |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS62180705A true JPS62180705A (en) | 1987-08-08 |
Family
ID=12069398
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2195286A Pending JPS62180705A (en) | 1986-02-05 | 1986-02-05 | Method for operating hollow yarn membrane filter |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62180705A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003275759A (en) * | 2002-03-20 | 2003-09-30 | Hitachi Plant Eng & Constr Co Ltd | Water treatment device |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4892279A (en) * | 1972-03-07 | 1973-11-30 | ||
| JPS58223416A (en) * | 1982-06-18 | 1983-12-26 | Iwai Kikai Kogyo Kk | Removing method of gel layer such as concentration polarization layer or the like sticking to surface of filter film in plane film type ultrafilter device |
-
1986
- 1986-02-05 JP JP2195286A patent/JPS62180705A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS4892279A (en) * | 1972-03-07 | 1973-11-30 | ||
| JPS58223416A (en) * | 1982-06-18 | 1983-12-26 | Iwai Kikai Kogyo Kk | Removing method of gel layer such as concentration polarization layer or the like sticking to surface of filter film in plane film type ultrafilter device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003275759A (en) * | 2002-03-20 | 2003-09-30 | Hitachi Plant Eng & Constr Co Ltd | Water treatment device |
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