JPH09239362A - Device for supplying makeup water to condenser - Google Patents
Device for supplying makeup water to condenserInfo
- Publication number
- JPH09239362A JPH09239362A JP4893996A JP4893996A JPH09239362A JP H09239362 A JPH09239362 A JP H09239362A JP 4893996 A JP4893996 A JP 4893996A JP 4893996 A JP4893996 A JP 4893996A JP H09239362 A JPH09239362 A JP H09239362A
- Authority
- JP
- Japan
- Prior art keywords
- water
- condenser
- makeup water
- membrane filter
- makeup
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は復水器への補給水供
給装置に係り、特に復水器への微生物や微細粒子、鉄ク
ラッドの流入を防止して、復水系の水質の安定化及び運
転効率の向上を図る復水器への補給水供給装置に関す
る。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a make-up water supply device for a condenser, and more particularly, to prevent the inflow of microorganisms, fine particles and iron clad into the condenser to stabilize the water quality of the condenser system. The present invention relates to a makeup water supply device for a condenser, which improves operation efficiency.
【０００２】[0002]
【従来の技術】火力発電所や原子力発電所等において
は、純水を加熱して蒸気を発生させ、これによりタービ
ンを駆動し、発電機を運転している。通常の場合、復水
器〜ボイラ〜復水器の循環系外へ蒸気を供給しているた
め、この循環系に対し系外から純水を補給する。2. Description of the Related Art In a thermal power plant, a nuclear power plant, etc., pure water is heated to generate steam, which drives a turbine and operates a generator. In the normal case, steam is supplied to the outside of the circulation system of the condenser-boiler-condenser, so pure water is supplied to the circulation system from outside the system.
【０００３】図２は、従来の補給水浄化系統及び復水循
環系統を示す系統図であり、タービン１から戻された復
水器２内の復水は、循環系内で復水中に混入した鉄クラ
ッド（酸化鉄粒子の混合物）が中空糸膜フィルター３で
除去された後、混床型イオン交換装置４でイオン交換処
理される。そして、低圧加熱器５、脱気器６、高圧加熱
器７及びボイラ８を経て発生した蒸気がタービン１に供
給され、復水が復水器２に循環される。FIG. 2 is a system diagram showing a conventional makeup water purification system and a condensate circulation system. Condensed water in the condenser 2 returned from the turbine 1 is iron mixed in condensate in the circulation system. After the clad (mixture of iron oxide particles) is removed by the hollow fiber membrane filter 3, an ion exchange treatment is performed by the mixed bed type ion exchange device 4. Then, the steam generated through the low-pressure heater 5, the deaerator 6, the high-pressure heater 7, and the boiler 8 is supplied to the turbine 1, and the condensate is circulated to the condenser 2.
【０００４】復水器２に補給される補給水（純水）は、
工水又は市水等の原水が、原水槽９を経て前処理装置１
０及び純水装置１１で処理され、純水タンク１２及び補
給水タンク１３を経て供給される。前処理装置１０は、
一般に、原水が工水の場合は凝集・加圧浮上濾過装置で
あり、原水が市水の場合は濾過装置である。また、純水
装置１１は、４床５塔式イオン交換装置、或いは、４床
５塔式イオン交換装置と混床式イオン交換装置とで構成
される。Make-up water (pure water) supplied to the condenser 2 is
Raw water such as industrial water or city water passes through the raw water tank 9 and the pretreatment device 1
0 and the pure water device 11, and is supplied through the pure water tank 12 and the makeup water tank 13. The pretreatment device 10 is
Generally, when raw water is industrial water, it is a flocculation / pressure floating filter, and when raw water is city water, it is a filter. The deionized water device 11 is composed of a 4-bed, 5-tower type ion exchange device, or a 4-bed, 5-tower type ion exchange device and a mixed-bed type ion exchange device.
【０００５】なお、復水循環系においては、発電量の変
動により復水循環量が変動して、復水器２の下部水槽が
上昇する場合があるため、復水器２内の復水を補給水タ
ンク１３に返送する配管が設けられている。In the condensate circulation system, the condensate circulation amount may fluctuate due to fluctuations in the amount of power generation, and the lower water tank of the condenser 2 may rise. Piping for returning to the tank 13 is provided.
【０００６】このような従来の補給水浄化系統及び復水
循環系統においては、復水循環系に下記〜の汚染物
質が流入するため、復水循環系の中空糸膜フィルター３
の差圧が上昇し易く、逆洗頻度が高い。なお、この差圧
上昇は、通水流束を高く設定した場合ほど起こり易い。In the conventional makeup water purification system and condensate circulation system as described above, the following pollutants in the condensate circulation system flow into the condensate circulation system.
The differential pressure of is easy to rise and the backwash frequency is high. It should be noted that this increase in differential pressure is more likely to occur when the water flow flux is set higher.
【０００７】 前処理装置で除去できなかった原水由
来の微細粒子 純水装置やタンク内で発生した微生物 大気中からタンク内に混入した微細粒子（純水タン
クや補給水タンクは完全な密閉構造ではないため、微細
粒子が混入する可能性がある。） 復水循環系内で発生し、余剰水中に混入して補給水
タンクに流入した鉄クラッド 特開平６−１３４４９０号公報には、補給水浄化系統の
純水装置に膜濾過装置を設けることが提案されており、
このように膜濾過装置を設けたものであれば、上記の
原水由来の汚染物質の復水循環系統への流入を防止する
ことができる。Fine particles derived from raw water that could not be removed by the pretreatment device Microorganisms generated in the pure water device or the tank Fine particles mixed in the tank from the atmosphere (The pure water tank and the makeup water tank have a completely closed structure. Therefore, fine particles may be mixed in.) Iron clad generated in the condensate circulation system, mixed in excess water and flowing into the makeup water tank JP-A-6-134490 discloses a makeup water purification system. It has been proposed to install a membrane filtration device in the pure water device of
If the membrane filtration device is provided in this way, it is possible to prevent the above-mentioned pollutants derived from raw water from flowing into the condensate circulation system.
【０００８】[0008]
【発明が解決しようとする課題】しかしながら、純水装
置に膜濾過装置を適用したものでは、原水由来の汚染物
質の除去は可能であるが、前記のように復水循環系内
で発生し、余剰水中に混入して補給水タンクに流入し、
再度復水循環系内に持ち込まれる鉄クラッドや、のよ
うにタンクにおいて混入する微細粒子及びのように純
水装置の後段で発生する微生物を除去することはできな
い。このため、復水循環系の中空糸膜フィルターの差圧
上昇を十分に抑制することができない。However, in the case where the membrane filtration device is applied to the deionized water device, it is possible to remove the pollutants derived from the raw water, but as described above, the pollutants generated in the condensate circulation system are excessive. It mixes in the water and flows into the makeup water tank,
It is not possible to remove iron clad that is brought into the condensate circulation system again, fine particles that are mixed in the tank such as, and microorganisms that occur in the latter stage of the pure water device, such as fine particles. Therefore, it is not possible to sufficiently suppress an increase in the differential pressure of the hollow fiber membrane filter of the condensate circulation system.
【０００９】本発明は上記従来の問題点を解決し、補給
水浄化系統から復水循環系統への汚染物質の流入を大幅
に低減して復水循環系の中空糸膜フィルターの差圧上昇
を抑え、これにより中空糸膜フィルターの逆洗頻度の低
減及び運転効率の向上を図る復水器への補給水供給装置
を提供することを目的とする。The present invention solves the above-mentioned conventional problems, greatly reduces the inflow of pollutants from the makeup water purification system to the condensate circulation system, and suppresses the differential pressure rise of the hollow fiber membrane filter of the condensate circulation system, Thus, it is an object of the present invention to provide a makeup water supply device for a condenser that reduces the frequency of backwashing hollow fiber membrane filters and improves operating efficiency.
【００１０】[0010]
【課題を解決するための手段】本発明の復水器への補給
水供給装置は、原水を浄化手段にて浄化した補給水を復
水器に供給する復水器への補給水供給装置において、該
浄化手段からの水を膜濾過装置に通し、該膜濾過装置の
透過水を直接復水器に供給することを特徴とする。A makeup water supply apparatus for a condenser according to the present invention is a makeup water supply apparatus for a condenser for supplying makeup water purified by raw water to a condenser. The water from the purification means is passed through a membrane filtration device, and the permeated water of the membrane filtration device is directly supplied to the condenser.
【００１１】本発明の復水器への補給水供給装置では、
膜濾過装置において、原水由来の微細粒子及び浄化系内
で発生する微生物や混入する微細粒子はもとより、復水
循環系から余剰水中に混入して補給水中に流入する鉄ク
ラッドを除去し、得られた透過水を直接復水器に供給す
るため、これらの汚染物質が復水循環系に流入するのを
確実に防止することができる。In the makeup water supply device for the condenser of the present invention,
In the membrane filtration device, not only the fine particles derived from raw water and the microbes and fine particles generated in the purification system, but also the iron clad that was mixed into the excess water from the condensate circulation system and flowed into the makeup water were removed and obtained. Since the permeated water is directly supplied to the condenser, it is possible to reliably prevent these pollutants from flowing into the condensate circulation system.
【００１２】[0012]
【発明の実施の形態】以下、図面を参照して本発明の実
施の形態を説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１３】図１は本発明の復水器への補給水供給装置
の一実施例を示す系統図である。図１において、図２に
示す部材と同一機能を奏する部材には同一符号を付して
ある。FIG. 1 is a system diagram showing an embodiment of a makeup water supply device for a condenser of the present invention. In FIG. 1, members having the same functions as those shown in FIG. 2 are designated by the same reference numerals.
【００１４】図１に示す本発明の復水器への補給水供給
装置は、補給水タンク１３からの補給水を膜濾過装置１
４に通水し、透過水を復水器２に供給する点が、図２の
従来装置とは異なり、その他は同様の構成とされてい
る。The make-up water supply device for the condenser of the present invention shown in FIG.
4 is different from the conventional device of FIG. 2 in that permeate water is supplied to the condenser 2, and other configurations are the same.
【００１５】本発明において、膜濾過装置としてはクロ
スフロー型や全量型濾過装置を用いることができる。な
お、全量濾過にて通水した場合、濾過する膜の目の細か
さにも左右されるものの、差圧上昇速度は速く、短期で
逆洗処理ないし膜の交換をせざるを得なくなる。また、
仮りに逆洗操作をしても完全に差圧が回復しないことが
多い。一方、クロスフロー濾過方式では濃縮水を排出す
ることにより、微細粒子や微生物、鉄クラッド等の汚染
物質を系外へ排出して復水循環系への流入を確実に防止
することができるので好ましい。In the present invention, as the membrane filtration device, a cross-flow type or a full-volume type filtration device can be used. In addition, when water is passed by full-scale filtration, the differential pressure increase rate is fast, although it depends on the fineness of the membrane to be filtered, and it is unavoidable to perform backwashing or membrane replacement in a short period of time. Also,
Even if backwashing is performed, the differential pressure is often not completely recovered. On the other hand, in the cross-flow filtration method, it is preferable to discharge the concentrated water so that contaminants such as fine particles, microorganisms, and iron clad can be discharged to the outside of the system and reliably prevented from flowing into the condensate circulation system.
【００１６】この膜濾過装置１４の濃縮水は、原水槽９
に返送して水回収率を高め、一方で濃縮水中の微細粒子
等は前処理装置１０の濾過装置や純水装置１１のイオン
交換装置等で捕捉し、これを汚泥引き抜き又は逆洗等で
系外へ排出するようにするのが好ましい。濃縮水はまた
発電所設備内の冷却水等として利用しても良い。The concentrated water of the membrane filtration device 14 is used as the raw water tank 9
To increase the water recovery rate, while fine particles in the concentrated water are captured by the filtration device of the pretreatment device 10 or the ion exchange device of the deionized water device 11 and the like, which is then removed by sludge extraction or backwashing. It is preferable to discharge it to the outside. The concentrated water may also be used as cooling water in power plant equipment.
【００１７】本発明で用いる膜濾過装置の膜としては、
ＭＦ（精密濾過）膜、ＵＦ（限外濾過）膜又はＲＯ（逆
浸透）膜が好ましく、エネルギー効率の面からはＲＯ膜
以外のＭＦ膜又はＵＦ膜、特にスパイラル型ＵＦ膜が好
適である。As the membrane of the membrane filtration device used in the present invention,
MF (microfiltration) membranes, UF (ultrafiltration) membranes or RO (reverse osmosis) membranes are preferable, and from the viewpoint of energy efficiency, MF membranes or UF membranes other than RO membranes, particularly spiral type UF membranes are preferable.
【００１８】[0018]
【実施例】以下に実施例及び比較例を挙げて本発明をよ
り具体的に説明する。The present invention will be described more specifically below with reference to examples and comparative examples.
【００１９】実施例１ 工水を凝集濾過処理した後、４床５塔式イオン交換装置
及び混床式イオン交換装置で処理し、純水タンク及び補
給水タンクを経て復水器に供給する実機の補給水供給装
置において、この補給水に下記模擬鉄クラッドを３μｇ
−Ｆｅ／Ｌとなるように連続注入し、スパイラル型ＵＦ
膜濾過装置（日東電工社製「ＮＴＵ−３１５０」膜サイ
ズ：４インチ）に４ｍ3 ／ｍ2 ／日で通水し、この透過
水を直接に復水器に供給し、この復水器内の水を中空糸
膜フィルター（住友ベークライト社製「ＦＰＭ−８００
０」孔径：０．０３μｍ以下）に流束０．３ｍ3 ／ｍ2
−膜／ｈｒとなるように通水した。なお、水温は２０〜
２５℃に調整した。また、中空糸膜フィルターの逆洗
は、原則として差圧が０．３ｋｇ／ｃｍ2 上昇した時点
で行うこととした。Example 1 An actual machine in which industrial water is subjected to coagulation filtration treatment, treated with a 4-bed 5-tower type ion exchange device and a mixed-bed type ion exchange device, and then supplied to a condenser via a pure water tank and a makeup water tank. In this makeup water supply device, 3 μg of the following simulated iron clad is added to this makeup water.
-Fe / L is continuously injected to obtain spiral type UF
Water is passed through a membrane filtration device (“NTU-3150” manufactured by Nitto Denko Corporation, membrane size: 4 inches) at 4 m 3 / m 2 / day, and this permeated water is directly supplied to the condenser, and inside the condenser. The water of the hollow fiber membrane filter ("FPM-800" manufactured by Sumitomo Bakelite Co., Ltd.
0 "hole diameter: 0.03 μm or less), flux 0.3 m 3 / m 2
-Water was passed so that it would be a membrane / hr. The water temperature is 20-
The temperature was adjusted to 25 ° C. In principle, backwashing of the hollow fiber membrane filter was performed when the differential pressure increased by 0.3 kg / cm 2 .
【００２０】模擬鉄クラッド 四三酸化鉄（Ｆｅ3 Ｏ4 ）：三二酸化鉄（Ｆｅ2 Ｏ
3 ）：水酸化第二鉄（ＦｅＯ（ＯＨ））＝７：２：１
（重量比）の混合物膜濾過条件 膜有効圧力：１．０ｋｇ／ｃｍ2 ベッセル（膜充填圧力容器）の濃縮水出口流量：６００
Ｌ／ｈｒ 中空糸膜フィルターの差圧（３０℃補正値）の経時変化
を図３に示す。また、試験期間（約２ケ月）中の逆洗回
数及び試験終了時の差圧の初期値に対する上昇幅を表１
に示す。 Simulated iron clad ferrosoferric oxide (Fe 3 O 4 ): iron sesquioxide (Fe 2 O)
3 ): ferric hydroxide (FeO (OH)) = 7: 2: 1
(Weight ratio) mixture Membrane filtration conditions Membrane effective pressure: 1.0 kg / cm 2 Vessel (membrane filling pressure vessel) concentrated water outlet flow rate: 600
FIG. 3 shows changes with time of the differential pressure (corrected value at 30 ° C.) of the L / hr hollow fiber membrane filter. Table 1 shows the number of backwashes during the test period (about 2 months) and the increase in the differential pressure at the end of the test with respect to the initial value.
Shown in
【００２１】比較例１ 実施例１において、ＵＦ膜濾過装置を用いず、補給水に
模擬鉄クラッドを注入した水を直接中空糸膜フィルター
に供給したこと以外は同様に行った。中空糸膜フィルタ
ーの差圧の経時変化を図３に示す。また、逆洗回数及び
差圧の上昇幅を表１に示す。Comparative Example 1 The same procedure as in Example 1 was carried out, except that the UF membrane filtration device was not used and the water in which the simulated iron clad was injected into the makeup water was directly supplied to the hollow fiber membrane filter. The time-dependent change in the differential pressure of the hollow fiber membrane filter is shown in FIG. Table 1 shows the number of times of backwashing and the range of increase in differential pressure.
【００２２】[0022]
【表１】 [Table 1]
【００２３】図３及び表１より、本発明によれば、復水
循環系の中空糸膜フィルターの差圧の上昇を抑えること
ができ、逆洗頻度を低減することができることがわか
る。From FIG. 3 and Table 1, it is understood that according to the present invention, it is possible to suppress an increase in the differential pressure of the hollow fiber membrane filter of the condensate circulation system and to reduce the frequency of backwashing.
【００２４】[0024]
【発明の効果】以上詳述した通り、本発明の復水器への
補給水供給装置は、補給水浄化系統から復水循環系統へ
の汚染物質の流入を大幅に低減することができるもので
あり、次の効果を奏する。As described in detail above, the makeup water supply device for a condenser of the present invention can greatly reduce the inflow of pollutants from the makeup water purification system to the condensate circulation system. , Has the following effects.
【００２５】 復水循環系の復水浄化用中空糸膜フィ
ルターの逆洗頻度を低減することができる。 中空糸膜フィルターの浄化時間（逆洗と逆洗の間
隔）が延長され、運転効率が向上する。 逆洗後の中空糸膜の差圧回復効率も向上し、薬品洗
浄頻度を低減することができる。 中空糸膜フィルターの連続運転により復水循環系の
復水水質が安定する。It is possible to reduce the frequency of backwashing the hollow fiber membrane filter for condensate purification of the condensate circulation system. The cleaning time of the hollow fiber membrane filter (the interval between backwashing and backwashing) is extended, and the operating efficiency is improved. The differential pressure recovery efficiency of the hollow fiber membrane after backwashing is also improved, and the frequency of chemical cleaning can be reduced. The continuous operation of the hollow fiber membrane filter stabilizes the condensate quality of the condensate circulation system.
【図１】本発明の復水器への補給水供給装置の一実施例
を示す系統図である。FIG. 1 is a system diagram showing an embodiment of a makeup water supply device for a condenser of the present invention.
【図２】従来の補給水浄化系統及び復水循環系統を示す
系統図である。FIG. 2 is a system diagram showing a conventional makeup water purification system and a condensate circulation system.
【図３】実施例１及び比較例１の結果を示すグラフであ
る。FIG. 3 is a graph showing the results of Example 1 and Comparative Example 1.
１ タービン ２ 復水器 ３ 中空糸膜フィルター ４ 混床型イオン交換装置 ５ 低圧加熱器 ６ 脱気器 ７ 高圧加熱器 ８ ボイラ ９ 原水槽 １０ 前処理装置 １１ 純水装置 １２ 純水タンク １３ 補給水タンク １４ 膜濾過装置 1 Turbine 2 Condenser 3 Hollow Fiber Membrane Filter 4 Mixed Bed Ion Exchanger 5 Low Pressure Heater 6 Deaerator 7 High Pressure Heater 8 Boiler 9 Raw Water Tank 10 Pretreatment Device 11 Pure Water Device 12 Pure Water Tank 13 Makeup Water Tank 14 membrane filtration device
Claims (1)
水器に供給する復水器への補給水供給装置において、該
浄化手段からの水を膜濾過装置に通し、該膜濾過装置の
透過水を直接復水器に供給することを特徴とする復水器
への補給水供給装置。1. A make-up water supply device for a condenser for supplying make-up water obtained by purifying raw water by a purifying means to a condenser, wherein the water from the purifying means is passed through a membrane filtration device to obtain the membrane filtration device. A makeup water supply device for a condenser, which directly supplies the permeated water of the condenser to the condenser.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04893996A JP3899545B2 (en) | 1996-03-06 | 1996-03-06 | Supply water supply device to condenser |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP04893996A JP3899545B2 (en) | 1996-03-06 | 1996-03-06 | Supply water supply device to condenser |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09239362A true JPH09239362A (en) | 1997-09-16 |
| JP3899545B2 JP3899545B2 (en) | 2007-03-28 |
Family
ID=12817250
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP04893996A Expired - Fee Related JP3899545B2 (en) | 1996-03-06 | 1996-03-06 | Supply water supply device to condenser |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3899545B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003100312A (en) * | 2001-09-27 | 2003-04-04 | Chugoku Electric Power Co Inc:The | Reversible cogeneration system |
| JP2013169530A (en) * | 2012-02-22 | 2013-09-02 | Mitsubishi Heavy Ind Ltd | Water treatment system for power plant and water treatment method |
| WO2018207492A1 (en) * | 2017-05-12 | 2018-11-15 | 栗田工業株式会社 | Boiler water treatment apparatus and treatment method |
-
1996
- 1996-03-06 JP JP04893996A patent/JP3899545B2/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003100312A (en) * | 2001-09-27 | 2003-04-04 | Chugoku Electric Power Co Inc:The | Reversible cogeneration system |
| JP2013169530A (en) * | 2012-02-22 | 2013-09-02 | Mitsubishi Heavy Ind Ltd | Water treatment system for power plant and water treatment method |
| WO2018207492A1 (en) * | 2017-05-12 | 2018-11-15 | 栗田工業株式会社 | Boiler water treatment apparatus and treatment method |
| JP2018192385A (en) * | 2017-05-12 | 2018-12-06 | 栗田工業株式会社 | Boiler water treatment apparatus and treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3899545B2 (en) | 2007-03-28 |
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