JP3899545B2 - Supply water supply device to condenser - Google Patents
Supply water supply device to condenser Download PDFInfo
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- JP3899545B2 JP3899545B2 JP04893996A JP4893996A JP3899545B2 JP 3899545 B2 JP3899545 B2 JP 3899545B2 JP 04893996 A JP04893996 A JP 04893996A JP 4893996 A JP4893996 A JP 4893996A JP 3899545 B2 JP3899545 B2 JP 3899545B2
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Description
【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。
【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。
【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。
【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１０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。
【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。
【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▲１▼〜▲４▼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。
【０００７】
▲１▼ 前処理装置で除去できなかった原水由来の微細粒子
▲２▼ 純水装置やタンク内で発生した微生物
▲３▼ 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。）
▲４▼ 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▲１▼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。
【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▲４▼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、▲３▼のようにタンクにおいて混入する微細粒子及び▲２▼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。
【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。
【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タンクを経て直接膜濾過装置に通し、該膜濾過装置の透過水を直接復水器に供給する補給水供給装置であって、前記復水器の余剰水が前記タンクに返送されることを特徴とする。
【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。
【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。
【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。
【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１４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。
【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。
【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。
【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。
【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。
【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−８０００」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。
【００２０】
模擬鉄クラッド
四三酸化鉄（Ｆｅ3 Ｏ4 ）：三二酸化鉄（Ｆｅ2 Ｏ3 ）：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：６００Ｌ／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。
【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。
【００２２】
【表１】
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。
【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。
【００２５】
▲１▼ 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。
▲２▼ 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。
▲３▼ 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。
▲４▼ 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。
【図面の簡単な説明】
【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。
【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。
【図３】実施例１及び比較例１の結果を示すグラフである。
【符号の説明】
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[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a makeup water supply device to a condenser, and in particular, to prevent inflow of microorganisms, fine particles, and iron clad into the condenser, thereby stabilizing the water quality of the condenser system and improving the operation efficiency. The present invention relates to a makeup water supply device to a water vessel.
[0002]
[Prior art]
In thermal power plants, nuclear power plants and the like, pure water is heated to generate steam, thereby driving a turbine and operating a generator. Usually, since steam is supplied outside the circulation system of the condenser, the boiler, and the condenser, pure water is replenished to the circulation system from outside the system.
[0003]
FIG. 2 is a system diagram showing a conventional makeup water purification system and a condensate circulation system. Condensate in the
[0004]
Supply water (pure water) to be supplied to the
[0005]
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
[0006]
In such conventional make-up water purification system and condensate circulation system, the following (1) to (4) pollutants flow into the condensate circulation system, so that the differential pressure of the hollow
[0007]
(1) Fine particles derived from raw water that could not be removed by the pretreatment device (2) Microorganisms generated in the pure water device or tank (3) Fine particles mixed in the tank from the atmosphere (pure water tank or makeup water tank) Is not a completely sealed structure, so fine particles may be mixed in.)
(4) Iron clad generated in the condensate circulation system, mixed in surplus water and flowing into the make-up water tank is disclosed in JP-A-6-134490, in which a membrane filtration device is provided in the pure water device of the make-up water purification system. If the membrane filtration device is provided in this way, it is possible to prevent the pollutant derived from the raw water (1) from flowing into the condensate circulation system.
[0008]
[Problems to be solved by the invention]
However, when a membrane filtration device is applied to a pure water device, it is possible to remove contaminants derived from raw water. However, as described in (4) above, it is generated in the condensate circulation system and mixed with surplus water for replenishment. Remove iron clad flowing into the water tank and brought back into the condensate circulation system, fine particles mixed in the tank as in (3), and microorganisms generated in the latter stage of the deionized water device as in (2). I can't. For this reason, the differential pressure | voltage rise of the hollow fiber membrane filter of a condensate circulation system cannot fully be suppressed.
[0009]
The present invention solves the above-mentioned conventional problems, significantly reduces the inflow of contaminants from the makeup water purification system to the condensate circulation system, and suppresses an increase in the differential pressure of the hollow fiber membrane filter in the condensate circulation system, thereby An object of the present invention is to provide a makeup water supply device for a condenser that reduces the frequency of backwashing of the membrane filter and improves the operation efficiency.
[0010]
[Means for Solving the Problems]
In condensate water replenishment water supply device to the instrument, makeup water supply device to the condenser and supplies the clarified makeup water to the condenser at the purifier raw water of the present invention, the tank water from the purifying means through direct membrane filtering device through a feature that a makeup water supply device for supplying permeate to direct condenser membrane filtration device, excess water in the condenser is returned to the tank To do.
[0011]
In the makeup water supply device to the condenser of the present invention, in the membrane filtration device, not only the fine particles derived from the raw water and the microorganisms generated in the purification system and the mixed fine particles are mixed into the surplus water from the condensate circulation system. Since the iron clad flowing into the makeup water is removed and the obtained permeate is directly supplied to the condenser, it is possible to reliably prevent these contaminants from flowing into the condensate circulation system.
[0012]
DETAILED DESCRIPTION OF THE INVENTION
Embodiments of the present invention will be described below with reference to the drawings.
[0013]
FIG. 1 is a system diagram showing an embodiment of an apparatus for supplying makeup water to a condenser according to the present invention. In FIG. 1, members having the same functions as those shown in FIG.
[0014]
The supply water supply device to the condenser of the present invention shown in FIG. 1 is that the makeup water from the
[0015]
In the present invention, as the membrane filtration device, a crossflow type or a full-volume type filtration device can be used. In addition, when the water is passed through the entire amount, although the speed of the differential pressure is high, the rate of increase in the differential pressure is high, and the backwash treatment or the membrane must be replaced in a short time. In many cases, even if a backwash operation is performed, the differential pressure is not completely recovered. On the other hand, the cross flow filtration method is preferable because the concentrated water is discharged, so that contaminants such as fine particles, microorganisms, and iron clad can be discharged out of the system and reliably prevented from flowing into the condensate circulation system.
[0016]
The concentrated water of the membrane filtration device 14 is returned to the
[0017]
As the membrane of the membrane filtration device used in the present invention, an MF (microfiltration) membrane, a UF (ultrafiltration) membrane or an RO (reverse osmosis) membrane is preferable. From the viewpoint of energy efficiency, an MF membrane other than the RO membrane or UF A membrane, particularly a spiral UF membrane, is preferred.
[0018]
【Example】
Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples.
[0019]
Example 1
In the supply water supply device of the actual machine, which is treated with a 4-bed 5-tower ion exchange device and a mixed bed ion exchange device after being subjected to coagulation filtration treatment, and supplied to the condenser through the pure water tank and the make-up water tank Then, the following simulated iron clad is continuously injected into this make-up water so as to be 3 μg-Fe / L, and 4 m 3 / m is applied to a spiral type UF membrane filtration device (“NTU-3150” membrane size: 4 inches manufactured by Nitto Denko Corporation). 2 / day, and the permeate is directly supplied to the condenser. The water in the condenser is a hollow fiber membrane filter (“FPM-8000” manufactured by Sumitomo Bakelite Co., Ltd., pore size: 0.03 μm or less). The water was passed through such that the flux was 0.3 m 3 / m 2 -membrane / hr. The water temperature was adjusted to 20-25 ° C. In addition, the back washing of the hollow fiber membrane filter was performed in principle when the differential pressure increased by 0.3 kg / cm 2 .
[0020]
Simulated iron clad <br/> triiron tetroxide (Fe 3 O 4): ferric oxide (Fe 2 O 3): Ferric hydroxide (FeO (OH)) = 7 : 2: 1 (weight ratio) blend
Membrane filtration conditions Membrane effective pressure: 1.0 kg / cm < 2 >
Concentrated water outlet flow rate of vessel (membrane-filled pressure vessel): 600 L / hr
FIG. 3 shows changes with time in the differential pressure (corrected value at 30 ° C.) of the hollow fiber membrane filter. Table 1 shows the number of backwashes during the test period (about 2 months) and the range of increase in the differential pressure at the end of the test relative to the initial value.
[0021]
Comparative Example 1
In Example 1, the same procedure was performed except that the UF membrane filtration device was not used and water in which simulated iron clad was injected into makeup water was directly supplied to the hollow fiber membrane filter. FIG. 3 shows changes with time in the differential pressure of the hollow fiber membrane filter. Table 1 shows the number of backwashes and the range of increase in the differential pressure.
[0022]
[Table 1]
3 and Table 1, it can be seen that according to the present invention, an increase in the differential pressure of the condensate circulation hollow fiber membrane filter can be suppressed, and the backwash frequency can be reduced.
[0024]
【The invention's effect】
As described above in detail, the makeup water supply device to the condenser of the present invention can greatly reduce the inflow of contaminants from the makeup water purification system to the condensate circulation system, and has the following effects. Play.
[0025]
(1) The frequency of backwashing of the condensate purification hollow fiber membrane filter in the condensate circulation system can be reduced.
(2) The purification time (interval between backwashing) of the hollow fiber membrane filter is extended, and the operation efficiency is improved.
(3) The differential pressure recovery efficiency of the hollow fiber membrane after backwashing can be improved and the frequency of chemical washing can be reduced.
(4) Condensate quality in the condensate circulation system is stabilized by continuous operation of the hollow fiber membrane filter.
[Brief description of the drawings]
FIG. 1 is a system diagram showing an embodiment of a makeup water supply apparatus for a condenser according to the present invention.
FIG. 2 is a system diagram showing a conventional makeup water purification system and a condensate circulation system.
FIG. 3 is a graph showing the results of Example 1 and Comparative Example 1.
[Explanation of symbols]
DESCRIPTION OF
Claims (4)
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 JPH09239362A (en) | 1997-09-16 |
| JP3899545B2 true 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) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP5088996B2 (en) * | 2001-09-27 | 2012-12-05 | 中国電力株式会社 | 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 |
| JP6447663B2 (en) * | 2017-05-12 | 2019-01-09 | 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
Also Published As
| Publication number | Publication date |
|---|---|
| JPH09239362A (en) | 1997-09-16 |
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