JPH01143687A - Condensate purifying equipment - Google Patents
Condensate purifying equipmentInfo
- Publication number
- JPH01143687A JPH01143687A JP62303026A JP30302687A JPH01143687A JP H01143687 A JPH01143687 A JP H01143687A JP 62303026 A JP62303026 A JP 62303026A JP 30302687 A JP30302687 A JP 30302687A JP H01143687 A JPH01143687 A JP H01143687A
- Authority
- JP
- Japan
- Prior art keywords
- condensate
- hollow fiber
- fiber membrane
- membrane filter
- hollow yarn
- 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 claims abstract description 53
- 238000011144 upstream manufacturing Methods 0.000 claims abstract description 4
- 239000012510 hollow fiber Substances 0.000 claims description 43
- 238000001914 filtration Methods 0.000 claims description 27
- 229910021645 metal ion Inorganic materials 0.000 claims description 27
- 238000010612 desalination reaction Methods 0.000 claims description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000000746 purification Methods 0.000 claims description 6
- 229910044991 metal oxide Inorganic materials 0.000 abstract description 7
- 238000005253 cladding Methods 0.000 abstract description 4
- 239000011148 porous material Substances 0.000 abstract description 3
- 150000001455 metallic ions Chemical class 0.000 abstract 5
- 238000011033 desalting Methods 0.000 abstract 2
- 230000008021 deposition Effects 0.000 abstract 1
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 150000002500 ions Chemical class 0.000 description 9
- 238000011001 backwashing Methods 0.000 description 8
- 239000012535 impurity Substances 0.000 description 7
- 238000000034 method Methods 0.000 description 6
- 150000004706 metal oxides Chemical class 0.000 description 5
- 230000007423 decrease Effects 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000005115 demineralization Methods 0.000 description 1
- 230000002328 demineralizing effect Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E30/00—Energy generation of nuclear origin
- Y02E30/30—Nuclear fission reactors
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、原子カプラントの復水浄化装置に係り、特に
復水中の金属イオン濃度に着目した復水浄化装置に関す
る。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a condensate purification device for an atomic couplant, and particularly to a condensate purification device that focuses on metal ion concentration in condensate.
、〔従来の技術〕
従来、原子カプラント、特に沸騰水型原子炉は、第３図
に示すような構成からなり、復水器１で凝縮された復水
を、低圧復水ポンプ２によりまず中空糸膜フィルタ型復
水ろ過装置３に導き、復水中のクラッドを除去する。中
空糸膜フィルタ型復水ろ過装置３を出た復水は、復水脱
塩装置４に導かれ、ここでイオン状不純物を除去して、
高圧復水ポンプ５に送られる。高圧復水ポンプ５を出た
復水は、低圧給水加熱器６で加熱され、給水ポンプ７の
吸込側へ導かれる。この給水ポンプ７を出たのち、給水
は高圧給水加熱器８を経て、原子炉給水配管９を通って
原子炉圧力容器１０に送られ原子炉内で蒸気となり、主
蒸気配管１１を通ってタービン１２へ導かれ、再び復水
器１で凝縮されて復水となる。１３は発電器を示す。, [Prior Art] Conventionally, a nuclear coupler plant, especially a boiling water reactor, has a configuration as shown in FIG. The condensate is introduced into a thread membrane filter type condensate filtration device 3 to remove crud in the condensate. The condensate that has exited the hollow fiber membrane filter type condensate filtration device 3 is led to a condensate desalination device 4, where ionic impurities are removed.
It is sent to the high pressure condensate pump 5. Condensate exiting the high-pressure condensate pump 5 is heated by a low-pressure feed water heater 6 and guided to the suction side of the feed water pump 7. After leaving this feedwater pump 7, the feedwater passes through a high-pressure feedwater heater 8, passes through a reactor feedwater pipe 9, is sent to a reactor pressure vessel 10, becomes steam in the reactor, and passes through a main steam pipe 11 to a turbine. 12 and condensed again in the condenser 1 to become condensate. 13 indicates a generator.
上記の原子カプラント復水給水系における中空糸膜フィ
ルタ型復水ろ過装置３は、中空糸膜でクラッド状不純物
を除去することを主目的としている。ここで、中空糸膜
は、中空の糸で膜面に小口径の孔がおいており、復水が
膜の外側から孔を通り内側の中空部に入る際、孔部で不
純物を物理的に除去する。したがって、クラッド状不純
物は除去されるが、イオン状不純物の除去は目的として
いない。このイオン状不純物は、復水脱塩装置４により
除去される。The hollow fiber membrane filter type condensate filtration device 3 in the above-mentioned atomic couplant condensate water supply system has the main purpose of removing clad-like impurities with the hollow fiber membrane. Here, hollow fiber membranes are hollow fibers with small diameter holes on the membrane surface, and when condensate passes from the outside of the membrane into the hollow inside, the holes physically remove impurities. Remove. Therefore, although cladding impurities are removed, ionic impurities are not removed. This ionic impurity is removed by the condensate desalination device 4.
塔の監視は、規定量の不純物を捕捉したことを差圧等で
検知し、ろ過器を逆洗する。この逆洗を行うことにより
、中空糸膜フィルタに付着したクラッドを除去し、ろ過
装置入口と出口差圧を回復させて、長時間にわたって使
用することができる。The tower is monitored by detecting whether a specified amount of impurities has been captured using differential pressure, etc., and backwashing the filter. By performing this backwashing, the crud attached to the hollow fiber membrane filter is removed, the pressure difference between the inlet and the outlet of the filter is restored, and the filter can be used for a long period of time.
この中空糸膜フィルタの逆洗方法についての従来技術は
、以下のとおりである。A conventional technique for backwashing a hollow fiber membrane filter is as follows.
まず１つは、スクラビングと呼ばれる方法で、ろ過器に
逆洗用水を供給したのちに、ろ過器に連通された空気導
入ラインを経て空気を導入し、気泡を通過させることに
より中空糸膜フィルタを振動させて、中空糸膜外面に付
着したクラッドを除去するものである。The first is a method called scrubbing. After supplying water for backwashing to the filter, air is introduced through the air introduction line connected to the filter, and air bubbles are passed through the hollow fiber membrane filter. It vibrates to remove crud attached to the outer surface of the hollow fiber membrane.
もう一つは、エアサージと呼ばれる方法で、ろ過器に逆
洗用水を供給したのちに、ろ過器の復水出口側に圧縮空
気を導入して、逆洗用水を中空糸膜内側から外側に透過
させて、中空糸膜に付着したクラッドを除去するもので
ある。The other method is called air surge, which supplies backwash water to the filter and then introduces compressed air to the condensate outlet side of the filter, allowing the backwash water to permeate from the inside of the hollow fiber membrane to the outside. This removes the cladding attached to the hollow fiber membrane.
なお、この種の中空糸膜フィルタ型復水ろ過器の逆洗方
法に関連するものとしては、特開昭６０−１９００２号
「中空糸膜フィルタの逆洗方法Ｊが挙げられる。Incidentally, a method related to the backwashing method of this kind of hollow fiber membrane filter type condensate filter includes JP-A No. 60-19002 "Backwashing method J of hollow fiber membrane filter."
しかしながら、復水が中空糸膜フィルタを通過する際に
、復水中の金属イオンが金属酸化物として中空糸膜内側
に付着析出し、フィルタ差圧が除徐に上昇すること、お
よび逆洗を行っても金属酸化物が除去しきれず、差圧回
復率が低下する事実を発見した。この事実は、中空糸膜
フィルタの寿命を短かくする問題を有する。However, when condensate passes through a hollow fiber membrane filter, metal ions in the condensate adhere to and precipitate on the inside of the hollow fiber membrane as metal oxides, causing a gradual increase in the filter differential pressure and the need for backwashing. It was discovered that the metal oxides could not be completely removed even when the pressure was removed, resulting in a decrease in the differential pressure recovery rate. This fact has the problem of shortening the life of the hollow fiber membrane filter.
本発明の目的は、中空糸膜内側に金属イオンが付着酸化
物として析出することを防止するために、中空糸膜フィ
ルタ型復水ろ過装置で処理される前に、復水中の金属イ
オンを復水脱塩装置により処理し、ろ過装置へ流入する
金属イオンの量を低減することにある。The purpose of the present invention is to remove metal ions from condensate before being processed by a hollow fiber membrane filter type condensate filtration device, in order to prevent metal ions from depositing as attached oxides on the inside of the hollow fiber membrane. The purpose is to reduce the amount of metal ions that are processed by a water desalination device and flow into the filtration device.
本発明は、プラントの給復水系に含まれているイオン量
はプラント配管系の表面に酸化皮膜が形成される前が多
く、特に新規プラントおよび給復水系の配管工事等を行
ったのちにはイオン量が多くなり、その後酸化皮膜が形
成されるとイオン量が減少してくるという事実の発見を
前提とする。In the present invention, the amount of ions contained in the water supply and condensate system of a plant is large before an oxide film is formed on the surface of the plant piping system, and especially after the piping work of the water supply and condensate system has been carried out in a new plant. The premise is the discovery of the fact that when the amount of ions increases and then an oxide film is formed, the amount of ions decreases.
すなわち、本発明は、中空糸膜フィルタ型ろ過装置およ
び復水脱塩装置を有する復水系を備えた復水浄化装置に
おいて、復水脱塩装置を復水流れに対して中空糸膜フィ
ルタ型ろ過装置の上流に配設したものである。That is, the present invention provides a condensate purification device equipped with a condensate system having a hollow fiber membrane filter type filtration device and a condensate desalination device, in which the condensate desalination device is connected to the hollow fiber membrane filter type filtration device for the condensate flow. It is placed upstream of the device.
復水ろ過装置へ供給される復水中の金属イオンは、中空
糸膜フィルタの外側から内側への孔の大きさ（直径約０
．１μｍ）よりも小さいために、内側に流入していき、
金属イオンが金属酸化物として付着する可能性がある。Metal ions in the condensate water supplied to the condensate filtration device are absorbed by the pore size (approximately 0 diameter) from the outside to the inside of the hollow fiber membrane filter.
．． 1μm), so it flows inward,
Metal ions may be deposited as metal oxides.
したがって、中空糸膜フィルタに流入する復水中の金属
イオンを、予め復水脱塩装置で処理することにより、膜
内側へ流入する金属イオンの量を低減し、膜内側への金
属酸化物の析出を低減することができる。Therefore, by treating the metal ions in the condensate flowing into the hollow fiber membrane filter in advance with a condensate desalination device, the amount of metal ions flowing into the inside of the membrane can be reduced and metal oxides can be precipitated inside the membrane. can be reduced.
なお、プラントの給復水系に含まれているイオン量は、
プラント配管系の表面に酸化皮膜が形成される前が多く
、特に新規プラントおよび給復水系の配管工事等を行っ
たのちにはイオン量が多くなり、その後酸化皮膜が形成
されるとイオン量が減少してくる。したがって、イオン
量に応じて、復水脱塩装置と復水ろ過装置の運転順序を
切り換え可能としておき、イオン量が多くなったときに
は、復水脱塩装置で金属イオンを処理し、復水ろ過装置
に復水を供給することにより、金属イオンの中空糸膜フ
ィルタへの流入量を減少させることができる。The amount of ions contained in the water supply and condensation system of the plant is
In most cases, an oxide film is not formed on the surface of a plant piping system, and the amount of ions increases especially after piping work is performed in a new plant or water supply and condensate system. It will decrease. Therefore, the operating order of the condensate desalination equipment and the condensate filtration equipment can be changed according to the amount of ions, and when the amount of ions increases, the metal ions are processed in the condensate demineralization equipment, and the condensate filtration equipment is processed. By supplying condensate to the device, the amount of metal ions flowing into the hollow fiber membrane filter can be reduced.
以下、本発明の一実施例を、第１図により説明する。同
図は、復水脱塩装置４を中空糸膜フィルタ型ろ過装置３
の上流側に設置した原子カプラントの復水給水系の全体
構成を示す。低圧復水ポンプ２を出た復水は、まず復水
脱塩装置４へ供給される。ここで金属イオンを除去され
たのち、中空糸膜フィルタ型ろ過装置３に供給されてク
ラッドを除去され、高圧復水ポンプ５へ導かれる。An embodiment of the present invention will be described below with reference to FIG. The figure shows a condensate desalination device 4 and a hollow fiber membrane filter type filtration device 3.
The overall configuration of the condensate water supply system for the atomic coupler installed upstream of the plant is shown. Condensate that has exited the low-pressure condensate pump 2 is first supplied to a condensate desalination device 4. After removing metal ions, the water is supplied to a hollow fiber membrane filter type filtration device 3 to remove crud, and then led to a high-pressure condensate pump 5.
以上の方法により、復水中の多量の金属イオンが中空糸
膜フィルタに流入することを防止し、中空糸膜フィルタ
内側に金属イオンが付着析出することを抑制する。The above method prevents a large amount of metal ions in the condensate from flowing into the hollow fiber membrane filter, and suppresses attachment and precipitation of metal ions inside the hollow fiber membrane filter.
第２図は本発明の他の実施例を示し、復水脱塩装置４と
中空糸膜フィルタ型ろ過装置３の運用を復水脱塩装置４
で復水を処理したのち、中空糸膜フィルタ型ろ過装置３
で処理する場合と、該ろ過装置３で処理した復水を復水
脱塩装置４で処理する場合のいずれの運用も可能とした
復水給水系の全体構成図である。FIG. 2 shows another embodiment of the present invention, in which the operation of the condensate desalination device 4 and the hollow fiber membrane filter type filtration device 3 is explained.
After treating the condensate, the hollow fiber membrane filter type filtration device 3
FIG. 2 is an overall configuration diagram of a condensate water supply system that can be operated in both cases of processing the condensate with the filtration device 3 and processing the condensate treated with the condensate desalination device 4.
中空糸膜フィルタへの金属イオンの付着量は、復水中の
イオン量が多いほど多い。したがって、復水中の金属イ
オンが多いときは、まず復水脱塩装置４に復水を通して
、金属イオンを該復水脱塩装置４にて処理したのち、中
空糸膜フィルタ型ろ過装置３に通水し処理するようにし
たものである。The amount of metal ions attached to the hollow fiber membrane filter increases as the amount of ions in the condensate increases. Therefore, when there are many metal ions in the condensate, the condensate is first passed through the condensate desalination device 4, the metal ions are treated in the condensate desalination device 4, and then the condensate is passed through the hollow fiber membrane filter type filtration device 3. It is made to be treated with water.
第２図は、金属イオン量の多い状態の運転を示している
。すなわち、弁１６，２０．２１は開であり、弁１７，
１８．１９は閉の状態である。このときはまず、金属イ
オン測定装置１４により金属イオン量を測定し、その信
号を弁開閉状態指示装置１５へ送り、この弁開閉状態指
示装置１５から復水脱塩装置４．中空糸膜フィルタ型ろ
過装置３周りの多弁１６〜２１へ開閉指示信号を伝達し
、所定の弁開閉状態とする。FIG. 2 shows operation with a large amount of metal ions. That is, valves 16, 20, 21 are open and valves 17, 20, 21 are open.
18.19 is in the closed state. At this time, first, the amount of metal ions is measured by the metal ion measuring device 14, and the signal is sent to the valve opening/closing state indicating device 15. An opening/closing instruction signal is transmitted to the multiple valves 16 to 21 around the hollow fiber membrane filter type filtration device 3 to set the valves in a predetermined opening/closing state.
次に、配管系の表面に酸化皮膜が形成され、金属イオン
量が減少し所定のイオン濃度に達すると。Next, an oxide film is formed on the surface of the piping system, and the amount of metal ions decreases until a predetermined ion concentration is reached.
金属イオン測定装置１４より弁開閉状態指示装置１５に
信号を送り、復水脱塩装置４．中空糸膜フィルタ型ろ過
装置３周りの多弁１６〜２１へ、弁開閉状態指示装置１
５から弁開閉状態の切り換え信号を送り、ろ過装置入口
弁１９．流路切替弁１８、復水脱塩装置出口弁１７を開
とし、復水脱塩装置人口弁１６．流路切替弁２１．ろ過
装置出口弁２０を開とし、復水の流れを中空糸膜フィル
タ型ろ過装置３から復水脱塩装置４とし、該ろ過装置３
でクラッドを処理したあとで、復水脱塩装置４で金属イ
オンを処理する運転とする。The metal ion measuring device 14 sends a signal to the valve opening/closing state indicating device 15, and the condensate desalination device 4. Valve open/close status indicating device 1 to multiple valves 16 to 21 around hollow fiber membrane filter type filtration device 3
A switching signal for valve open/close state is sent from filtration device inlet valve 19. Open the flow path switching valve 18 and the condensate desalination device outlet valve 17, and open the condensate desalination device artificial valve 16. Flow path switching valve 21. The filtration device outlet valve 20 is opened, and the condensate flows from the hollow fiber membrane filter type filtration device 3 to the condensate desalination device 4, and the filtration device 3
After treating the cladding, the condensate desalination device 4 is operated to treat metal ions.
本発明によれば、中空糸膜フィルタ型ろ過装置３へ流入
する復水中の金属イオン濃度を低減することにより、中
空糸膜内側への金属イオン付着。According to the present invention, by reducing the concentration of metal ions in the condensate flowing into the hollow fiber membrane filter type filtration device 3, metal ions are prevented from adhering to the inside of the hollow fiber membrane.
金属酸化物の析出を抑制し、中空糸膜の孔の閉塞を防止
することができるので、中空糸膜フィルタ逆洗時の差圧
回復率を向上させ、中空糸膜フィルタの寿命を長期化で
きる効果がある。It can suppress the precipitation of metal oxides and prevent the pores of hollow fiber membranes from being blocked, improving the differential pressure recovery rate during backwashing of hollow fiber membrane filters and extending the life of hollow fiber membrane filters. effective.
【図面の簡単な説明】
第１図は本発明の一実施例の構成図、第２図は本発明の
他実施例の構成図、第３図は従来の原子カプラント復水
給水系の全体構成図を示す。
１・・・復水器、３・・・中空糸膜フィルタ型ろ過装置
、４・・・復水脱塩装置、６・・・低圧給水加熱器、８
・・・高圧給水加熱器、１０・・・原子炉圧力容器、１
１・・・主蒸気配管、１２・・・タービン、１３・・・
発電機、１４・・・金属イオン測定装置、１５・・・弁
開閉状態指示装置。[Brief Description of the Drawings] Fig. 1 is a block diagram of one embodiment of the present invention, Fig. 2 is a block diagram of another embodiment of the present invention, and Fig. 3 is the overall structure of a conventional atomic coupler condensate water supply system. Show the diagram. 1... Condenser, 3... Hollow fiber membrane filter type filtration device, 4... Condensate desalination device, 6... Low pressure feed water heater, 8
... High pressure feed water heater, 10 ... Reactor pressure vessel, 1
1... Main steam piping, 12... Turbine, 13...
Generator, 14... Metal ion measuring device, 15... Valve opening/closing state indicating device.
Claims (1)
有する復水系を備えた復水浄化装置において、復水脱塩
装置を復水流れに対して中空糸膜フィルタ型ろ過装置の
上流に配設したことを特徴とする復水浄化装置。 ２、特許請求の範囲第１項において、復水脱塩装置と中
空糸膜フィルタ型ろ過装置への通水順序を復水中の金属
イオン濃度により切り換え可能とした復水浄化装置。[Claims] 1. In a condensate purification device equipped with a condensate system having a hollow fiber membrane filter type filtration device and a condensate desalination device, the condensate desalination device is connected to the hollow fiber membrane filter for the condensate flow. A condensate purification device characterized by being installed upstream of a type filtration device. 2. A condensate purification device according to claim 1, in which the order of water flow to the condensate desalination device and the hollow fiber membrane filter type filtration device can be switched depending on the metal ion concentration in the condensate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62303026A JPH01143687A (en) | 1987-11-30 | 1987-11-30 | Condensate purifying equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62303026A JPH01143687A (en) | 1987-11-30 | 1987-11-30 | Condensate purifying equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH01143687A true JPH01143687A (en) | 1989-06-06 |
Family
ID=17916038
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62303026A Pending JPH01143687A (en) | 1987-11-30 | 1987-11-30 | Condensate purifying equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01143687A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001318188A (en) * | 2000-05-10 | 2001-11-16 | Japan Organo Co Ltd | Condensate purification system and its operation method |
| JP2002004810A (en) * | 2000-06-19 | 2002-01-09 | Japan Organo Co Ltd | Method of treating condensate |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6283003A (en) * | 1985-10-09 | 1987-04-16 | Hitachi Ltd | Filter desalting device |
-
1987
- 1987-11-30 JP JP62303026A patent/JPH01143687A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS6283003A (en) * | 1985-10-09 | 1987-04-16 | Hitachi Ltd | Filter desalting device |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2001318188A (en) * | 2000-05-10 | 2001-11-16 | Japan Organo Co Ltd | Condensate purification system and its operation method |
| JP2002004810A (en) * | 2000-06-19 | 2002-01-09 | Japan Organo Co Ltd | Method of treating condensate |
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