JP3506493B2 - Sterilization method of membrane separation device - Google Patents
Sterilization method of membrane separation deviceInfo
- Publication number
- JP3506493B2 JP3506493B2 JP17407994A JP17407994A JP3506493B2 JP 3506493 B2 JP3506493 B2 JP 3506493B2 JP 17407994 A JP17407994 A JP 17407994A JP 17407994 A JP17407994 A JP 17407994A JP 3506493 B2 JP3506493 B2 JP 3506493B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- membrane separation
- separation device
- chamber
- raw water
- 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.)
- Expired - Fee Related
Links
- 239000012528 membrane Substances 0.000 title claims description 96
- 238000000926 separation method Methods 0.000 title claims description 72
- 230000001954 sterilising effect Effects 0.000 title claims description 44
- 238000000034 method Methods 0.000 title claims description 17
- 238000004659 sterilization and disinfection Methods 0.000 title description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 169
- 239000012466 permeate Substances 0.000 claims description 11
- 239000008236 heating water Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 3
- 238000000605 extraction Methods 0.000 claims description 2
- 238000011282 treatment Methods 0.000 description 17
- FYGDTMLNYKFZSV-URKRLVJHSA-N (2s,3r,4s,5s,6r)-2-[(2r,4r,5r,6s)-4,5-dihydroxy-2-(hydroxymethyl)-6-[(2r,4r,5r,6s)-4,5,6-trihydroxy-2-(hydroxymethyl)oxan-3-yl]oxyoxan-3-yl]oxy-6-(hydroxymethyl)oxane-3,4,5-triol Chemical compound O[C@@H]1[C@@H](O)[C@H](O)[C@@H](CO)O[C@H]1OC1[C@@H](CO)O[C@@H](OC2[C@H](O[C@H](O)[C@H](O)[C@H]2O)CO)[C@H](O)[C@H]1O FYGDTMLNYKFZSV-URKRLVJHSA-N 0.000 description 7
- 229920002498 Beta-glucan Polymers 0.000 description 7
- 239000000126 substance Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- 239000000356 contaminant Substances 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 241000894006 Bacteria Species 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000002158 endotoxin Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 229920002492 poly(sulfone) Polymers 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 238000003809 water extraction Methods 0.000 description 2
- 241000195493 Cryptophyta Species 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 230000000249 desinfective effect Effects 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 230000002542 deteriorative effect Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000008238 pharmaceutical water Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 239000002510 pyrogen Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000008400 supply water Substances 0.000 description 1
- -1 that is Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Description
【発明の詳細な説明】
【０００１】
【産業上の利用分野】本発明は膜分離装置の殺菌方法に
係り、特に、膜分離装置を加熱水により簡単な操作で効
果的に殺菌する方法に関する。
【０００２】
【従来の技術】原水中のパイロジエン及び菌を除去して
医薬用精製水、即ち、医薬品の製造工程で用いられる用
水を製造するために、従来、ＵＦ（限外濾過）膜又はＲ
Ｏ（逆浸透）膜等を用いた膜分離処理が適用されてい
る。特に、ＵＦ膜は熱水殺菌が可能な材質（例えばポリ
スルホン）が用いられており、加熱水による無菌化が容
易であることから医薬用精製水製造工程に多用されてい
る。
【０００３】即ち、原水の脱パイロ（パイロジエン除
去）及び除菌を継続して行うことにより、膜分離装置の
膜を含む系内が汚染されてくる。このため、定期的（標
準的には１週間に１回）に加熱水を通水して膜分離装置
系内の殺菌を行う必要があるが、ＵＦ膜は一般にこの加
熱水による殺菌処理にも十分に耐える耐熱性を有する。
【０００４】従来の膜分離装置における膜分離処理及び
殺菌方法を図１を参照して説明する。図１において、１
は原水タンク、２はポンプ、３は熱交換器、４はＵＦ膜
分離装置本体、５は処理水タンクであり、１１〜２０の
各符号は配管、Ｖ1 ，Ｖ2 ，Ｖ3 ，Ｖ4 はバルブを示
す。
【０００５】原水の膜分離処理に際しては、バルブＶ
1 ，Ｖ4 を閉、バルブＶ2 ，Ｖ3 を開として原水タンク
１内の原水をポンプ２を備える配管１１、熱交換器３、
配管１２を経てＵＦ膜分離装置本体４の原水室４Ａに供
給し、膜透過水を透過水室４Ｂから配管１３、配管１４
を経て抜き出し、処理水タンク５に受ける。一方、膜濃
縮水は、原水室４Ａより配管１６，１７を経て抜き出
し、原水タンク１に循環させる。なお、バルブＶ4 を開
として、膜濃縮水の一部を配管１８より系外へ排出する
場合もある。
【０００６】このような膜分離処理による脱パイロ及び
除菌を継続することにより、系内が汚染されるため、加
熱水を通水して系内の殺菌を行う。殺菌処理に当って
は、バルブＶ1 ，Ｖ4 を開、バルブＶ2 ，Ｖ3 を閉とす
るとともに、配管１９より熱交換器３に加熱蒸気を供給
してＵＦ膜分離装置本体４に給水される原水を加熱し、
加熱した原水をＵＦ膜分離装置本体４の原水室４Ａから
透過水室４Ｂに透過させ、配管１３，１５を経て系外へ
排出させる。なお、加熱水の一部は原水室４Ａから、配
管１６，１８を経て系外へ排出される。
【０００７】
【発明が解決しようとする課題】最近になって、上記従
来の膜分離装置の殺菌処理を行うと、殺菌処理後の膜分
離処理の運転再開時において、透過水のパイロジエン濃
度が殺菌処理前よりも上昇することが判明した。
【０００８】そこで、上記従来の膜分離装置の殺菌処理
において、殺菌処理前、処理中、処理後の透過水のパイ
ロジエン濃度と原水室内の水温との関係を調べたところ
（ただし、原水のパイロジエン濃度は２０〜４０ＥＵ
（エンドトキシンユニット）／ｍｌ）、図３に示す如
く、水温が約６０℃以上になるとパイロジエン濃度が大
きく上昇し、その後水温を低下させて、膜分離処理を再
開した際には、透過水のパイロジエン濃度が殺菌処理前
よりも高くなることが確認された。なお、この実験で用
いたＵＦ膜は水温９０℃であってもパイロジエンを透過
しないことが予め確認されているものである。
【０００９】本発明者らは、このパイロジエン濃度の上
昇について検討するに当り、パイロジエン以外のパイロ
ジエン類似物質、例えばβ−グルカン等が透過水側に移
行し、擬似パイロジエンとして検出されることを仮定し
た。そして、β−グルカンを原水側に投入して透過実験
を行ったところ、約６０℃以上の温度では、β−グルカ
ンの膜透過が認められた。
【００１０】このことから、本発明者らは、パイロジエ
ン以外の、パイロジエン分析（エンドトキシン試験）に
感知するβ−グルカン等の物質（これらは原水中の藻類
から発生すると推定される。）が加熱水による殺菌時に
ＵＦ膜を透過し、透過水側を汚染させ、これが膜分離処
理の通水時に少しずつ溶解し、処理水質を悪化させてい
るものと判断した。
【００１１】従って、この水質悪化を防止するために
は、原水中のβ−グルカン等の擬似パイロジエン物質を
ＲＯ膜等により予め除去することが考えられるが、本発
明者らは、この擬似パイロジエン物質を効果的に除去し
得る簡便な殺菌方法を見出し、本発明をなすに到った。
【００１２】本発明は、特に脱パイロ及び除菌を行う膜
分離装置を簡便な方法で効果的に殺菌する方法であっ
て、殺菌処理後において、高水質透過水を得ることがで
きる膜分離装置の殺菌方法を提供することを目的とす
る。
【００１３】
【課題を解決するための手段】本発明の膜分離装置の殺
菌方法は、内部に膜を備え、該膜により原水室と透過水
室とが画成されている膜分離装置本体と、該膜分離装置
本体の原水室に原水を導入する給水手段と、該膜分離装
置本体の透過水室から透過水を抜き出す透過水取出手段
と、該膜分離装置本体の原水室から濃縮水を抜き出して
前記給水手段に循環する循環手段とを備えた膜分離装置
を加熱水で殺菌する方法において、前記透過水取出手段
を閉とした状態で６０℃以上の加熱水を給水手段、膜分
離装置本体の原水室及び循環手段に流通させ、且つ該原
水室を通過した加熱水の一部を膜分離装置外に排出させ
ながら上記の流通を行うことにより該給水手段、原水室
及び循環手段を殺菌した後、前記透過水取出手段を開と
した状態で膜分離装置本体の原水室に６０℃以上の加熱
水を供給して膜分離装置本体の透過水室及び透過水取出
手段に該加熱水を流通させ、該透過水室及び透過水取出
手段を通過した加熱水を膜分離装置外に排出することに
より該透過水室及び透過水取出手段を殺菌することを特
徴とする。
【００１４】以下、一般的なＵＦ膜分離装置の系統図で
ある図１を参照して、本発明の膜分離装置の殺菌方法の
一実施例方法を詳細に説明する。
【００１５】なお、以下において、膜分離装置の殺菌の
ために系内に加熱水を供給した後、膜分離装置本体の原
水室内の水温が上昇する工程を昇温工程、原水室内の水
温が一定の加熱水温に保たれる工程を保持工程、加熱水
の供給を停止し、原水室内の水温が常温まで低下する工
程を冷却工程と称す。また、保持工程のうち、透過水取
出手段を閉として給水手段、膜分離装置本体の原水室及
び循環手段を殺菌する工程を第１保持工程と称し、透過
水取出手段を開として膜分離装置本体の透過水室及び透
過水取出手段を殺菌する工程を第２保持工程と称す。
【００１６】図１に示すＵＦ膜分離装置において、本発
明の殺菌方法を実施するには、まず、バルブＶ1 ，Ｖ2
を閉、バルブＶ3 ，Ｖ4 を開とすると共に、配管１９よ
り蒸気を供給し、配管１１より送給される原水タンク１
からの原水を加熱し、加熱した原水を配管１２よりＵＦ
膜分離装置本体４に供給する。これにより、膜分離装置
本体４の原水室４Ａ内の水温は上昇し（昇温工程）、そ
の後一定に保持される（第１保持工程）。この加熱水
は、配管１２、ＵＦ膜分離装置本体４の原水室４Ａ、配
管１６を経て、一部は配管１８より系外に排出され、残
部は配管１７より原水タンク１に返送される。
【００１７】これにより、給水手段（配管１２）、膜分
離装置本体４の原水室４Ａ及び循環手段（配管１６）が
加熱水により効果的に殺菌され、パイロジエンやβ−グ
ルカン等の擬似パイロジエン物質は系外へ排出される。
【００１８】本発明において、昇温工程及び第１保持工
程においては透過水取出手段が閉とされ、加熱水の膜透
過が起こらない。
【００１９】昇温工程及び第１保持工程のバルブ開閉は
例えば次のように設定することができる。
【００２０】昇温工程及び第１保持工程において、配管
１６内の水の５０〜１０％を配管１７より循環し、残部
５０〜９０％を系外へ排出するようにし、第１保持工程
終了直前に、一旦全量を膜分離装置外へ排出する。
【００２１】
【００２２】
【００２３】第１保持工程終了後、バルブＶ1 ，Ｖ4 を
開、バルブＶ2 ，Ｖ3 を閉として、引き続き加熱水を膜
分離装置本体４に供給し、加熱水を原水室４Ａから透過
水室４Ｂに透過させ、配管１３，１５を経て膜分離装置
外へ排出する。また、加熱水の一部（通常の場合、供給
される加熱水の５〜２０％程度）は配管１６，１８を経
て膜分離装置外へ排出する（第２保持工程）。その後、
この状態で蒸気の供給を停止することにより原水の加熱
を止める。これにより膜分離装置本体４の原水室４Ａ内
の水温は常温まで低下する（冷却工程）。
【００２４】この第２保持工程及び冷却工程により、膜
分離装置本体４の透過水室４Ｂ及び透過水取出手段（配
管１３）内は加熱水により効果的に殺菌される。
【００２５】この際、原水側のパイロジエンやβ−グル
カン等の擬似パイロジエン物質は、昇温工程及び第１保
持工程において、この透過水側へ移行することなく膜分
離装置外へ排出されているため、これらの物質により透
過水側が汚染されることはない。
【００２６】従って、一連の殺菌処理後においては、膜
分離装置内は十分に殺菌され、汚染物質が除去されたも
のとなる。
【００２７】殺菌処理後は、バルブＶ1 を閉、バルブＶ
2 ，Ｖ3 を開、バルブＶ4 を閉又は開として、原水を通
水して、膜分離処理を再開し、透過水を配管１３，１４
を経て処理水タンク５に受ける。
【００２８】本発明において、昇温工程、第１保持工
程、第２保持工程及び冷却工程の各工程の処理時間は、
例えば、次のような範囲とするのが好ましい。
【００２９】昇温工程：５〜６０分、より好ましくは１
０〜３０分
第１保持工程：１５〜６０分、より好ましくは３０〜６
０分
第２保持工程：１５〜６０分、より好ましくは１５〜３
０分
冷却工程：５〜６０分、より好ましくは１０〜３０分
また、殺菌に用いる加熱水の温度（即ち、保持工程にお
ける膜分離装置本体の原水室の水温）は、６０℃以上、
好ましくは６０〜９５℃とする。
【００３０】本発明において、殺菌に用いる加熱水は、
図１に示す如く、原水を熱交換器等で加熱したものに限
らず、別途加熱水タンクを設け、系外から加熱水を供給
するようにしても良い。
【００３１】また、本発明の膜分離装置の殺菌方法は、
ポリスルホンＵＦ膜等の耐熱性に優れた膜を備えるＵＦ
膜分離装置に好適に適用されるが、これに限らず、ＲＯ
膜分離装置やその他の膜分離装置にも適用可能である。
【００３２】
【作用】本発明においては、透過水取出手段を閉とした
状態で、加熱水を供給して給水手段、膜分離装置本体の
原水室、循環手段を殺菌処理した後、加熱水を膜分離装
置外へ排出するため、この殺菌処理に当り、給水側の汚
染物質を透過水側へ移行させることなく、確実に系外へ
排出することができる。そして、この給水側の殺菌及び
汚染物質排出後、透過水取出手段を開として透過水側の
殺菌を行うため、透過水側が給水側の汚染物質により再
汚染されることはなく、効果的な殺菌を行うことができ
る。
【００３３】
【実施例】以下に実施例を挙げて本発明をより具体的に
説明する。
【００３４】実施例１
図１に示す膜分離装置において、表１に示すバルブ操作
及び熱交換器の蒸気供給により膜分離処理及び殺菌処理
を行った。このときの膜分離装置本体の原水室水温及び
透過水（ただし、昇温工程と第１保持工程では透過水は
得られない。）のパイロジエン濃度を調べ、結果を図２
に示した。
【００３５】なお、昇温工程及び第１保持工程において
は、バルブＶ3 の通水量を９０％、バルブＶ4 の通水量
を１０％とし、第１保持工程終了直前の１０分間は、１
００％系外に排出した。
【００３６】
【表１】
【００３７】図２より、透過水側の水のパイロジエン濃
度は、殺菌処理時においても殺菌処理後の通水時におい
ても常にパイロジエン分析下限値の０．０３ＥＵ／ｍｌ
以下となり、殺菌処理により、パイロジエン濃度が上昇
することはなく、良好な殺菌効果が得られることが明ら
かである。
【００３８】
【発明の効果】以上詳述した通り、本発明の膜分離装置
の殺菌方法によれば、バルブ操作という簡便な操作によ
り、膜分離装置を効果的に殺菌処理することができる。
【００３９】本発明の膜分離装置の殺菌方法は、原水の
脱パイロ及び除菌を行って医薬用精製水を製造する膜分
離装置の加熱水殺菌に特に有効であり、擬似パイロジエ
ン物質の系内残留を防止して、良好な殺菌効果を得るこ
とができる。Description: BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for sterilizing a membrane separation apparatus, and more particularly to a method for effectively sterilizing a membrane separation apparatus by a simple operation using heated water. 2. Description of the Related Art Conventionally, UF (ultrafiltration) membranes or R (Ultrafiltration) membranes have been used for producing purified pharmaceutical water, that is, water for use in the production of pharmaceuticals by removing pyrodiene and bacteria from raw water.
A membrane separation process using an O (reverse osmosis) membrane or the like is applied. In particular, the UF membrane is made of a material (for example, polysulfone) that can be sterilized with hot water, and is easily used for sterilization with heated water. [0003] That is, by continuously performing depyrrolysis (removal of pyridiene) and sterilization of raw water, the inside of the system including the membrane of the membrane separation device is contaminated. For this reason, it is necessary to sterilize the membrane separator system by passing heated water periodically (typically once a week), and UF membranes are generally used for sterilization by this heated water. It has sufficient heat resistance. [0004] A membrane separation treatment and a sterilization method in a conventional membrane separation apparatus will be described with reference to FIG. In FIG. 1, 1
Is a raw water tank, 2 is a pump, 3 is a heat exchanger, 4 is a UF membrane separation device main body, 5 is a treated water tank, and reference numerals 11 to 20 are piping, V 1 , V 2 , V 3 , V 4. Indicates a valve. [0005] In the membrane separation treatment of raw water, the valve V
1, V 4 and closed, the valve V 2, a pipe 11 provided with a pump 2 raw water of the raw water tank 1 V 3 is opened, the heat exchanger 3,
The water is supplied to the raw water chamber 4A of the UF membrane separation device main body 4 via the pipe 12, and the membrane permeated water is supplied from the permeated water chamber 4B to the pipes 13 and 14,
And received in the treated water tank 5. On the other hand, the membrane concentrated water is withdrawn from the raw water chamber 4A via the pipes 16 and 17 and circulated to the raw water tank 1. Incidentally, the valve V 4 is opened, there is a case to discharge a portion of the membrane concentrated water to the outside of the system from the pipe 18. [0006] Since the inside of the system is contaminated by continuing the depyrrolysis and sterilization by the membrane separation treatment, the system is sterilized by passing heated water. In the sterilization process, the valves V 1 and V 4 are opened, the valves V 2 and V 3 are closed, and heating steam is supplied from the pipe 19 to the heat exchanger 3 to supply water to the UF membrane separation device main body 4. Heated raw water,
The heated raw water is transmitted from the raw water chamber 4A of the UF membrane separation device main body 4 to the permeated water chamber 4B, and discharged out of the system via the pipes 13 and 15. A part of the heating water is discharged from the raw water chamber 4A to the outside of the system via the pipes 16 and 18. [0007] Recently, when the sterilization treatment of the above-mentioned conventional membrane separation apparatus is performed, when the operation of the membrane separation treatment is restarted after the sterilization treatment, the concentration of the pyridiene in the permeated water becomes sterile. It was found to be higher than before the treatment. Therefore, in the sterilization treatment of the above-mentioned conventional membrane separation apparatus, the relationship between the pyridiene concentration of the permeated water before, during, and after the sterilization treatment and the water temperature in the raw water chamber was examined (however, the concentration of the pyridiene concentration in the raw water). Is 20 to 40 EU
(Endotoxin unit) / ml), as shown in FIG. 3, when the water temperature rises to about 60 ° C. or higher, the concentration of pyridiene increases greatly. It was confirmed that the concentration was higher than before the sterilization treatment. Note that it has been previously confirmed that the UF membrane used in this experiment does not permeate pyrodiene even at a water temperature of 90 ° C. In examining the increase in the concentration of pyridiene, the present inventors hypothesized that a pyrodiene-like substance other than pyridiene, for example, β-glucan, would migrate to the permeate and be detected as pseudopyrogien. . Then, when β-glucan was introduced into the raw water side and a permeation experiment was carried out, at a temperature of about 60 ° C. or higher, permeation of β-glucan through the membrane was observed. [0010] From this, the present inventors have found that substances other than pyridiene, such as β-glucan, which are detected in pyridiene analysis (endotoxin test) and the like (these are presumed to be generated from algae in raw water) are heated water. It was determined that the water permeated through the UF membrane during the sterilization and contaminated the permeated water side, and this was gradually dissolved when the water passed through the membrane separation treatment, thereby deteriorating the quality of the treated water. [0011] Therefore, in order to prevent the deterioration of water quality, it is conceivable to remove in advance the pseudo-pylogiene substance such as β-glucan in the raw water by using an RO membrane or the like. The present inventors have found a simple sterilization method capable of effectively removing, and have accomplished the present invention. The present invention is a method for effectively disinfecting a membrane separation apparatus for depyrogenating and removing bacteria in a simple and effective manner. The membrane separation apparatus is capable of obtaining permeated water of high quality after sterilization. It is an object of the present invention to provide a sterilization method. According to the present invention, there is provided a method for sterilizing a membrane separation apparatus according to the present invention, wherein a membrane is internally provided, and a raw water chamber and a permeated water chamber are defined by the membrane. A water supply means for introducing raw water into a raw water chamber of the membrane separation device main body; a permeate extraction means for extracting permeated water from a permeate water chamber of the membrane separation device main body; and a concentrated water from the raw water chamber of the membrane separation device main body. A method for sterilizing a membrane separation device provided with a circulation means for extracting and circulating the extracted water with the water supply means, wherein the permeated water take-out means is closed and heated water of 60 ° C. or more is supplied to the water supply means and the membrane separation device. The water supply means, the raw water chamber and the circulation means are sterilized by circulating the raw water chamber and the circulation means of the main body and performing the above-mentioned flow while discharging a part of the heated water passing through the raw water chamber to the outside of the membrane separation device. After that, the permeated water extracting means was opened. In this state, heated water of 60 ° C. or more is supplied to the raw water chamber of the membrane separation device main body to flow the heated water to the permeated water chamber and the permeated water extracting means of the membrane separation device main body, and the permeated water chamber and the permeated water extraction are performed.
The permeated water chamber and the permeated water extracting means are sterilized by discharging the heated water passing through the means to the outside of the membrane separation device . Referring now to FIG. 1, which is a system diagram of a general UF membrane separation apparatus, a method for sterilizing a membrane separation apparatus according to an embodiment of the present invention will be described in detail. In the following, after heating water is supplied into the system for sterilization of the membrane separation device, the process of raising the water temperature in the raw water chamber of the main body of the membrane separation device is referred to as a temperature raising step. The step of maintaining the temperature of the heated water is referred to as a holding step, and the step of stopping the supply of the heated water and reducing the temperature of the water in the raw water chamber to room temperature is referred to as a cooling step. In the holding step, the step of closing the permeated water extracting means and sterilizing the water supply means, the raw water chamber and the circulation means of the membrane separation device main body is referred to as a first holding step, and opening the permeated water extracting means and opening the membrane separation device main body. The step of sterilizing the permeated water chamber and the permeated water extracting means is referred to as a second holding step. In the UF membrane separation apparatus shown in FIG. 1, in order to carry out the sterilization method of the present invention, first, the valves V 1 , V 2
Is closed, valves V 3 and V 4 are opened, steam is supplied from pipe 19, and raw water tank 1 is supplied from pipe 11.
From the raw water, and heat the raw water from the pipe 12 to the UF
It is supplied to the membrane separation device main body 4. Thereby, the water temperature in the raw water chamber 4A of the membrane separation device main body 4 rises (temperature raising step), and is thereafter kept constant (first holding step). A part of the heated water is discharged to the outside of the system through a pipe 18 via a pipe 12, a raw water chamber 4A of the UF membrane separation device main body 4 and a pipe 16, and the rest is returned to the raw water tank 1 through a pipe 17. As a result, the water supply means (piping 12), the raw water chamber 4A of the membrane separation device main body 4 and the circulation means (piping 16) are effectively sterilized by the heated water, and pseudo-pyrodiene substances such as pyrodiene and β-glucan are removed. It is discharged out of the system. [0018] In the present invention, Oite the heating step and the first holding step is the permeate removal means closed, have such occur membrane permeability of heated water. The valve opening and closing of the heating step and the first holding step can be set as follows, for example. [0020] In the temperature raising step and the first holding step, the 50 to 10% of water in the pipe 16 circulates from the piping 17, so as to discharge 50-90% remainder out of the system, the first holding step is completed just before Then, the entire amount is once discharged out of the membrane separation device. After the completion of the first holding step, the valves V 1 and V 4 are opened and the valves V 2 and V 3 are closed. From the raw water chamber 4A to the permeated water chamber 4B, and is discharged to the outside of the membrane separation device via the pipes 13 and 15. In addition, a part of the heating water (generally, about 5 to 20% of the supplied heating water) is discharged to the outside of the membrane separation device via the pipes 16 and 18 (second holding step). afterwards,
In this state, heating of the raw water is stopped by stopping the supply of steam. As a result, the water temperature in the raw water chamber 4A of the membrane separation device main body 4 drops to room temperature (cooling step). By the second holding step and the cooling step, the permeated water chamber 4B and the permeated water extracting means (pipe 13) of the membrane separation device main body 4 are effectively sterilized by the heated water. At this time, pseudo-pyrdiene substances such as pyridiene and β-glucan on the raw water side are discharged outside the membrane separation apparatus without being transferred to the permeated water side in the temperature raising step and the first holding step. However, these substances do not contaminate the permeated water side. Therefore, after a series of sterilization treatments, the inside of the membrane separation apparatus is sufficiently sterilized and contaminants are removed. After the sterilization treatment, the valve V 1 is closed and the valve V
2, the V 3 opened, the closed or the valve V 4 opened, and passed through the raw water, resumes membrane separation process, the permeate piping 13
Through the treated water tank 5. In the present invention, the processing time of each of the temperature raising step, the first holding step, the second holding step, and the cooling step is as follows:
For example, the following ranges are preferable. Temperature raising step: 5 to 60 minutes, more preferably 1
0 to 30 minutes first holding step: 15 to 60 minutes, more preferably 30 to 6 minutes
0 minute second holding step: 15 to 60 minutes, more preferably 15 to 3 minutes
0 minute cooling step: 5 to 60 minutes, more preferably 10 to 30 minutes Further, the temperature of the heating water used for sterilization (that is, the water temperature of the raw water chamber of the membrane separation device main body in the holding step) is 60 ° C. or more.
Preferably, it shall be the 60~95 ℃. In the present invention, the heated water used for sterilization is
As shown in FIG. 1, the raw water is not limited to the raw water heated by a heat exchanger or the like. A separate heated water tank may be provided to supply heated water from outside the system. Further, the method for sterilizing a membrane separation device of the present invention comprises:
UF with a membrane with excellent heat resistance such as polysulfone UF membrane
It is preferably applied to a membrane separation device, but is not limited thereto.
The present invention is also applicable to a membrane separation device and other membrane separation devices. In the present invention, after the permeated water extracting means is closed, heated water is supplied to sterilize the water supply means, the raw water chamber of the membrane separation device main body, and the circulating means. Since the water is discharged to the outside of the membrane separation device, the contaminants on the water supply side can be reliably discharged to the outside of the system without transferring the contaminants on the water supply side to the permeated water side. After the sterilization and discharge of contaminants on the water supply side, the permeated water extraction means is opened to sterilize the permeated water side. It can be performed. The present invention will be described more specifically with reference to the following examples. Example 1 In the membrane separation apparatus shown in FIG. 1, the membrane separation treatment and the sterilization treatment were performed by operating the valves shown in Table 1 and supplying steam from the heat exchanger. At this time, the temperature of the raw water chamber and the temperature of the permeated water in the main body of the membrane separation apparatus (the permeated water was not obtained in the temperature raising step and the first holding step) were examined.
It was shown to. [0035] In the Atsushi Nobori step and the first holding step, the passing water amount of the valve V 3 90% of the passing water amount of the valve V 4 and 10%, the first holding step is completed just before the 10 minute, 1
00% was discharged out of the system. [Table 1] From FIG. 2, it can be seen that the concentration of pyridiene in the permeated water is always 0.03 EU / ml, which is the lower limit of the pyrogen analysis, both during sterilization and when passing water after sterilization.
As shown below, it is clear that the sterilization treatment does not increase the concentration of pyrodiene, and that a good sterilizing effect can be obtained. As described above in detail, according to the method for sterilizing a membrane separation apparatus of the present invention, the membrane separation apparatus can be effectively sterilized by a simple operation such as a valve operation. The method for sterilizing a membrane separation device of the present invention is particularly effective for sterilization of heated water in a membrane separation device for producing purified water for medical use by removing pyrolysis and removing bacteria from raw water. The residual can be prevented, and a good bactericidal effect can be obtained.
【図面の簡単な説明】
【図１】本発明を適用する膜分離装置の一実施例を示す
系統図である。
【図２】実施例１の結果を示す、水温及び透過水パイロ
ジエン濃度のグラフである。
【図３】従来の殺菌処理における水温及び透過水パイロ
ジエン濃度のグラフである。
【符号の説明】
１ 原水タンク
２ ポンプ
３ 熱交換器
４ ＵＦ膜分離装置本体
４Ａ 原水室
４Ｂ 透過水室
５ 処理水タンクBRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a system diagram showing one embodiment of a membrane separation apparatus to which the present invention is applied. FIG. 2 is a graph showing water temperature and permeated water pyrodiene concentration, showing the results of Example 1. FIG. 3 is a graph of water temperature and permeated water pyrodiene concentration in a conventional sterilization treatment. [Description of Signs] 1 Raw water tank 2 Pump 3 Heat exchanger 4 UF membrane separator main unit 4A Raw water chamber 4B Permeated water chamber 5 Treated water tank
Claims (1)
過水室とが画成されている膜分離装置本体と、該膜分離
装置本体の原水室に原水を導入する給水手段と、該膜分
離装置本体の透過水室から透過水を抜き出す透過水取出
手段と、該膜分離装置本体の原水室から濃縮水を抜き出
して前記給水手段に循環する循環手段とを備えた膜分離
装置を加熱水で殺菌する方法において、 前記透過水取出手段を閉とした状態で６０℃以上の加熱
水を給水手段、膜分離装置本体の原水室及び循環手段に
流通させ、且つ該原水室を通過した加熱水の一部を膜分
離装置外に排出させながら上記の流通を行うことにより
該給水手段、原水室及び循環手段を殺菌した後、 前記透過水取出手段を開とした状態で膜分離装置本体の
原水室に６０℃以上の加熱水を供給して膜分離装置本体
の透過水室及び透過水取出手段に該加熱水を流通させ、
該透過水室及び透過水取出手段を通過した加熱水を膜分
離装置外に排出することにより該透過水室及び透過水取
出手段を殺菌することを特徴とする膜分離装置の殺菌方
法。(57) [Claims 1] A membrane separation device main body having a membrane therein and defining a raw water chamber and a permeate water chamber by the membrane, and a raw water chamber of the membrane separation device main body. A water supply means for introducing raw water into the membrane separator; a permeate extraction means for extracting permeated water from a permeate chamber of the membrane separation device main body; Means for sterilizing the membrane separation apparatus provided with the means with heated water, wherein the permeated water extracting means is closed, and the heated water of 60 ° C. or higher is supplied to the water supply means, the raw water chamber of the membrane separation apparatus main body, and the circulation means. And sterilizing the water supply means, the raw water chamber and the circulation means by performing the above-mentioned circulation while discharging a part of the heated water passing through the raw water chamber to the outside of the membrane separation device, 60 ° C in the raw water chamber of the membrane separation device in the open state The heating water in the permeate chamber and permeate removal means of the membrane separation apparatus main body by supplying heated water above is circulated,
The heated water passing through the permeated water chamber and the permeated water extracting means is separated into membranes.
The permeated water chamber and permeated water
A method for sterilizing a membrane separation device, comprising sterilizing an outlet means .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17407994A JP3506493B2 (en) | 1994-07-26 | 1994-07-26 | Sterilization method of membrane separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP17407994A JP3506493B2 (en) | 1994-07-26 | 1994-07-26 | Sterilization method of membrane separation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0833833A JPH0833833A (en) | 1996-02-06 |
| JP3506493B2 true JP3506493B2 (en) | 2004-03-15 |
Family
ID=15972288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP17407994A Expired - Fee Related JP3506493B2 (en) | 1994-07-26 | 1994-07-26 | Sterilization method of membrane separation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3506493B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW393777B (en) | 1997-09-02 | 2000-06-11 | Nikon Corp | Photoelectric conversion devices and photoelectric conversion apparatus employing the same |
| CN117582824B (en) * | 2023-11-28 | 2024-07-23 | 武汉启诚生物技术有限公司 | Water purification equipment heat sterilization method and water purification equipment heat sterilization system |
-
1994
- 1994-07-26 JP JP17407994A patent/JP3506493B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0833833A (en) | 1996-02-06 |
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