JP2004279227A - Method and device for condensate demineralization - Google Patents
Method and device for condensate demineralization Download PDFInfo
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- JP2004279227A JP2004279227A JP2003071507A JP2003071507A JP2004279227A JP 2004279227 A JP2004279227 A JP 2004279227A JP 2003071507 A JP2003071507 A JP 2003071507A JP 2003071507 A JP2003071507 A JP 2003071507A JP 2004279227 A JP2004279227 A JP 2004279227A
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- 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
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- 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
Abstract
Description
【０００１】
【発明の属する技術分野】
本発明は、ＢＷＲ原子力発電プラントの復水処理に係り、特に、懸濁性腐食生成物濃度が低く且つ硫酸イオン濃度の低い、高純度な処理水質を得ることができる復水脱塩方法及び装置に関するものである。
【０００２】
【従来の技術】
【特許文献１】特開昭５５−５９８８１号公報
【特許文献２】特許第３０８７９０５号公報
ＢＷＲ原子力発電プラントでは、原子炉にて発生した蒸気で発電した後に海水にて蒸気を冷却し、その復水を、復水脱塩装置にて処理し原子炉に給水している。ＢＷＲ原子力発電プラントの概略フロー構成図を図３に示す。復水脱塩装置ではイオン交換樹脂が使用され、系統内に流入した海水成分や、プラント構成材料より生成した鉄酸化物を主体とした懸濁性腐食生成物（以下、クラッドと称す）やイオン性不純物を除去している。
ＢＷＲ原子力発電プラントの復水脱塩装置で使用しているイオン交換樹脂は、上流側より流入するＮａＣｌに代表される海水成分などのイオン成分の除去能力は高いが、クラッドの除去能力については、入口濃度に対する除去率が５０〜８０程度と低い。このため、そのままではクラッドが原子炉に給水されることとなり、放射能レベル上昇の一つの原因となる。
【０００３】
更に、カチオン樹脂から溶出する有機性不純物（以下、ＴＯＣと称す〉は、原子炉内に持ち込まれると硫酸を生成するため、原子炉水質を低下させる原因となる。
従って、原子炉水質を高純度にするためには、復水脱塩装置によるクラッド除去能力を高め、且つカチオン樹脂から溶出するＴＯＣのリーク量を少なくする必要がある。
これらを解決する方法としては、特許第３０８７９０５号公報にあるような、架橋度が６％程度で且つ表面構造が特殊なカチオン樹脂を使用してクラッドを効率的に除去する方法や、特開昭５５−５９８８１号公報にあるような、カチオン樹脂を樹脂層表層部に配してクラッドを除去する方法、などが提案されているが、クラッドの除去とカチオン樹脂溶出ＴＯＣの低減の双方を満足する復水脱塩装置は提案されていない。
【０００４】
【発明が解決しようとする課題】
本発明は、上記従来技術に鑑み、ＢＷＲ原子力発電プラントの復水脱塩装置による復水処理において、懸濁性腐食生成物濃度が低く且つ硫酸イオン濃度の低い、高純度の処理水質を得ることができる復水脱塩方法及び装置を提供することを課題とする。
【０００５】
【課題を解決するための手段】
上記課題を解決するために、本発明では、ＢＷＲ原子力発電プラントの復水をイオン交換樹脂層で処理する復水脱塩方法において、該復水を処理するイオン交換樹脂層を、表層部がカチオン樹脂、中間部がカチオン樹脂とアニオン樹脂の混床、及び、下層部がアニオン樹脂とすることを特徴とする復水脱塩方法、及び、ＢＷＲ原子力発電プラントの復水をイオン交換樹脂層で処理する復水脱塩方法において、該復水を処理するイオン交換樹脂層を、表層部がアニオン樹脂に対してカチオン樹脂の存在比率を１：２より多くした混床、中間部がアニオン樹脂とカチオン樹脂の比率が２：１から１：２の混床、及び、下層部がアニオン樹脂に対してカチオン樹脂の存在比率を２：１より少なくした混床とすることを特徴とする復水脱塩方法としたものである。
この復水脱塩方法によれば、処理水中のクラッドの低減とＴＯＣリーク量の低減の双方を満足し、高純度の処理水質を得ることができる。
【０００６】
また、本発明では、ＢＷＲ原子力発電プラントの復水を処理するイオン交換樹脂層を有する復水脱塩装置において、該イオン交換樹脂層は、表層部がカチオン樹脂、中間部がカチオン樹脂とアニオン樹脂の混床、及び、下層部がアニオン樹脂で形成されていることを特徴とする復水脱塩装置、及び、ＢＷＲ原子力発電プラントの復水を処理するイオン交換樹脂層を有する復水脱塩装置において、該イオン交換樹脂層は、表層部がアニオン樹脂に対してカチオン樹脂の存在比率を１：２より多くした混床、中間部がアニオン樹脂とカチオン樹脂の比率が２：１から１：２の混床、及び、下層部がアニオン樹脂に対してカチオン樹脂の存在比率を２：１より少なくした混床で形成されていることを特徴とする復水脱塩装置としたものである。
このように構成した復水脱塩装置によれば、処理水中のクラッドの低減とＴＯＣリーク量の低減の双方を満足し、高純度の処理水質を得ることができる。
【０００７】
【発明の実施の形態】
次に、本発明を図面を参照にして、詳細に説明する。
図１に、本発明で用いる復水脱塩装置のフロー構成図を示す。通水が完了したイオン交換樹脂は、脱塩塔１よりカチオン樹脂再生塔２に移送される。ここで逆洗分離を行いカチオン樹脂とアニオン樹脂を比重差により分離する。続いてアニオン樹脂をアニオン樹脂移送ライン５よりアニオン樹脂再生塔６に移送する。その後、分離状態となったカチオン樹脂とアニオン樹脂は単独で逆洗分離を行う。次にアニオン樹脂の一部を樹脂貯槽４に移送し、引き続き樹脂返送ライン７にて脱塩塔１に返送し、脱塩塔１の下部にアニオン樹脂層を形成する。その後、アニオン樹脂再生塔６に残留しているアニオン樹脂全量とカチオン樹脂再生塔２にあるカチオン樹脂の一部を樹脂貯槽４に移相する。ここで、空気を用いてアニオン樹脂とカチオン樹脂を混合して混床を形成し、樹脂返送ライン７にて脱塩塔１に移送してアニオン樹脂層の上に混床を形成する。引き続き、カチオン樹脂再生塔２に残留しているカチオン樹脂を樹脂貯層４に移相し、続いて樹脂返送ライン７にて脱塩塔１に移送して樹脂層表層部にカチオン樹脂を形成する。これにより、脱塩塔１内でカチオン樹脂とアニオン樹脂の混合比率の異なる３層を有する樹脂層が形成されることとなる。
【０００８】
また、上記操作において、アニオン樹脂再生塔６から樹脂貯槽４を通り、アニオン樹脂を脱塩塔１に移送する際に、アニオン樹脂の体積に対して半量以下の量のカチオン樹脂を樹脂貯層４に移送して空気を用いて混合した上で脱塩塔１へ移送して、塔内にアニオン樹脂リッチの下層を形成し、次に、アニオン樹脂とカチオン樹脂とを体積比で１対２から２対１の比率で空気を用いて混合して脱塩塔１に移送して、塔内に通常比率の混床を中間部に形成し、最後にカチオン樹脂を脱塩塔１に移送する際に、カチオン樹脂の体積に対して半量以下の量のアニオン樹脂を、樹脂貯層４に移送して空気を用いて混合した上で脱塩塔１へ移送して、塔内にカチオン樹脂リッチの上層を形成することで、脱塩塔内でカチオン樹脂とアニオン樹脂の混合比率の異なる３層を有する樹脂層を形成してもよい。
【０００９】
なお、形成する樹脂層の層高については、中間層１に対して、上下層はそれぞれ０．１〜１、特に、０．４〜１の割合で用いることができる。例えば、上下層をそれぞれ２０〜３０ｃｍとすることが望ましい。この理由は次の通りである。ＢＷＲ原子力発電プラントの復水脱塩装置の樹脂層高は、通常９０ｃｍ程度である。イオン交換樹脂に被処理水を通水して不純物を除去する場合、被処理水が樹脂層を通過するにつれて不純物イオンが除去されるため、超純水を得るには、ある程度の樹脂層高が必要である。通常の復水脱塩装置は通水線流速が１２０ｍ／ｈ程度であり、設計基準で想定されている入口負荷は、海水の主成分である食塩濃度として２ｍｇ／Ｌ若しくは２０ｍｇ／Ｌ程度である。これを処理するためには、２ｍｇ／Ｌの場合で樹脂層高として３０ｃｍ以上、２０ｍｇ／Ｌの場合で５０ｃｍ以上の樹脂層高が必要である。従って、この３０若しくは５０ｃｍの混床を樹脂層の中間部に形成し、残りの樹脂層高分を上下層に等分に配すると、２０〜３０ｃｍの上・下層を形成することが可能である。
【００１０】
【実施例】
以下、実施例により、本発明を具体的に説明する。
実施例１
ＢＷＲ原子力発電プラントの復水脱塩装置で広く使用されているイオン交換樹脂（三菱化学社製）であるカチオン樹脂ＳＫ１ＢＮと、アニオン樹脂ＳＡ１０ＢＮを用い、図２に示すケース１〜６の樹脂層を形成し、通水試験を行い、クラッド除去性能と樹脂からリークするイオン濃度の測定を行った。試験は、被処理水の水質、温度、溶存酸素濃度、樹脂層条件が実プラントと同等であり、実際のプラントと同条件を模擬したものである。
なお、図２において、ｂは混床、（カチオン樹脂：アニオン樹脂比＝１：１）、ａはアニオン樹脂層、ｃはカチオン樹脂層、ｂ＜ａはアニオン樹脂リッチ層（カチオン樹脂：アニオン樹脂比＝１：２）、ｂ＜ｃはカチオン樹脂リッチ層（カチオン樹脂：アニオン樹脂比＝２：１）であり、（ ）内は層高である。
【００１１】
内径２５ｍｍのガラスカラムに、カチオン樹脂とアニオン樹脂を充填し、十分に脱気された比抵抗値１８ＭΩ・ｃｍで４５℃、クラッド濃度２０μｇ／Ｌを含む純水を１Ｌ／ｍｉｎの流量で通水し、処理水中のクラッド濃度とイオン濃度を測定した。クラッド濃度は、処理水の一部を分岐し、１００ｍＬ／分で孔径０．４５μｍのメンブレンフィルタに約５０Ｌ通水し、フィルタ上に捕集したクラッド鉄の絶対量を原子吸光法若しくは蛍光Ｘ線分光光度法にて定量し、メンブレンフィルタへの通水量で除すことで濃度を算出した。また、イオン濃度は、処理水を紫外線照射して処理水中に含まれるＴＯＣを分解し、生成する硫酸イオン濃度をイオンクロマト法にて分析した。１日１回分析を行い、１ヶ月の通水期間の平均値の結果を、表１に示す。なお、表１によれば、ケース６より、ケース５、ケース４よりケース５の方が効果は上がっているが、上・下層の単独の層が厚い方が効果が高まることによる。表１からわかるように、従来技術（ケース１）や表層のみにカチオン樹脂層を形成したケース（ケース２）、下層のみにアニオン樹脂を形成したケース（ケース３）に比べ、本発明はクラッド除去率と硫酸濃度の両方で優れた結果であることが確認された。
【００１２】
【表１】
【発明の効果】
本発明によれば、前記した本発明のＢＷＲ原子力発電プラントの復水脱塩処理により、復水中に存在するクラッドを効果的に除去し、装置からのＴＯＣリーク量を低減でき、懸濁性腐食生成物濃度が低く且つ硫酸イオン濃度の低い、高純度な処理水質を得ることが可能となる復水脱塩方法及び装置を提供することができた。
【図面の簡単な説明】
【図１】本発明で用いる復水脱塩装置の一例を示すフロー構成図。
【図２】実施例１で用いる樹脂層の構成図。
【図３】公知のＢＷＲ原子力発電プラントの概略フロー構成図。
【符号の説明】
１：脱塩塔、２：カチオン樹脂再生塔、３：カチオン樹脂移送ライン、４：樹脂貯槽、５：アニオン樹脂移送ライン、６：アニオン樹脂再生塔、７：樹脂返送ライン、ａ：アニオン樹脂層、ｂ：混床、ｃ：カチオン樹脂層、ｂ＜ａ：アニオン樹脂リッチ層、ｂ＜ｃ：カチオン樹脂リッチ層[0001]
TECHNICAL FIELD OF THE INVENTION
The present invention relates to a condensate treatment for a BWR nuclear power plant, and more particularly to a condensate desalination method and apparatus capable of obtaining high-purity treated water having a low suspended corrosion product concentration and a low sulfate ion concentration. It is about.
[0002]
[Prior art]
[Patent Document 1] Japanese Patent Application Laid-Open No. 55-59881 [Patent Document 2] Japanese Patent No. 3087905 In a BWR nuclear power plant, after steam is generated in a nuclear reactor, the steam is cooled with seawater and then recovered. Water is treated by a condensate desalination unit and supplied to the reactor. FIG. 3 shows a schematic flow configuration diagram of the BWR nuclear power plant. The condensate desalination system uses an ion exchange resin, which contains seawater components that flow into the system, suspended corrosion products mainly composed of iron oxides generated from plant constituent materials (hereinafter referred to as cladding), and ions. Sexual impurities are removed.
The ion exchange resin used in the condensate desalination unit of the BWR nuclear power plant has a high ability to remove ionic components such as seawater components typified by NaCl flowing from the upstream side, but the ability to remove the cladding is as follows: The removal rate with respect to the inlet concentration is as low as about 50 to 80. For this reason, the cladding is supplied to the reactor as it is, which is one of the causes of an increase in the radioactivity level.
[0003]
Further, organic impurities (hereinafter, referred to as TOC) eluted from the cationic resin generate sulfuric acid when introduced into the reactor, which causes a reduction in the water quality of the reactor.
Therefore, in order to increase the water quality of the reactor, it is necessary to enhance the ability to remove the clad by the condensate desalination apparatus and to reduce the amount of TOC eluted from the cationic resin.
As a method for solving these problems, a method of efficiently removing the clad using a cationic resin having a degree of crosslinking of about 6% and a special surface structure as disclosed in Japanese Patent No. Japanese Patent Application Laid-Open No. 55-59881 proposes a method of disposing a cationic resin on the surface layer of a resin layer to remove the clad, and the like, but it satisfies both the removal of the clad and the reduction of the TOC eluted by the cationic resin. A condensate desalination unit has not been proposed.
[0004]
[Problems to be solved by the invention]
In view of the above prior art, the present invention provides a high-purity treated water having a low suspended corrosion product concentration and a low sulfate ion concentration in condensate treatment by a condensate desalination apparatus of a BWR nuclear power plant. It is an object of the present invention to provide a condensed water desalination method and apparatus that can perform the method.
[0005]
[Means for Solving the Problems]
In order to solve the above problems, the present invention provides a condensate desalination method in which condensate of a BWR nuclear power plant is treated with an ion exchange resin layer. Resin, a condensed water desalination method characterized in that the middle part is a mixed bed of a cationic resin and an anionic resin, and the lower part is an anionic resin, and the condensate of a BWR nuclear power plant is treated with an ion exchange resin layer. In the condensate desalination method, the ion-exchange resin layer for treating the condensate is mixed with an anion resin in which the ratio of the cationic resin to the anionic resin is more than 1: 2. Condensed water desalination characterized in that the mixed bed has a resin ratio of 2: 1 to 1: 2 and the mixed bed has a lower layer in which the ratio of the cationic resin to the anionic resin is less than 2: 1. Method Than it is.
According to the condensate desalination method, it is possible to satisfy both the reduction of the clad in the treated water and the reduction of the TOC leak amount, and to obtain a high-purity treated water quality.
[0006]
Further, according to the present invention, in a condensate desalination apparatus having an ion exchange resin layer for treating condensate of a BWR nuclear power plant, the ion exchange resin layer has a surface layer portion of a cationic resin, and an intermediate portion has a cationic resin and an anionic resin. And a condensate desalination apparatus characterized in that the lower layer portion is formed of an anionic resin, and a condensate desalination apparatus having an ion exchange resin layer for treating condensate of a BWR nuclear power plant In the ion-exchange resin layer, the surface layer portion has a mixed bed in which the ratio of the cationic resin to the anionic resin is more than 1: 2, and the middle portion has a ratio of the anionic resin to the cationic resin of 2: 1 to 1: 2. And a mixed bed in which the lower layer has an abundance ratio of a cationic resin to an anionic resin of less than 2: 1.
According to the condensate desalination apparatus configured as described above, both the reduction of the clad in the treated water and the reduction of the TOC leak amount can be satisfied, and the treated water with high purity can be obtained.
[0007]
BEST MODE FOR CARRYING OUT THE INVENTION
Next, the present invention will be described in detail with reference to the drawings.
FIG. 1 shows a flow configuration diagram of a condensate desalination apparatus used in the present invention. The ion-exchange resin that has passed through the water is transferred from the desalination tower 1 to the cation resin regeneration tower 2. Here, backwashing separation is performed to separate the cation resin and the anion resin by a difference in specific gravity. Subsequently, the anion resin is transferred from the anion resin transfer line 5 to the anion resin regeneration tower 6. Thereafter, the separated cationic resin and anionic resin are subjected to backwashing and separation alone. Next, a part of the anion resin is transferred to the resin storage tank 4 and then returned to the desalination tower 1 through the resin return line 7 to form an anion resin layer below the desalination tower 1. Thereafter, the entire amount of the anion resin remaining in the anion resin regeneration tower 6 and a part of the cation resin in the cation resin regeneration tower 2 are phase-shifted to the resin storage tank 4. Here, the mixed bed is formed by mixing the anionic resin and the cationic resin using air, and the mixed bed is formed on the anion resin layer by transferring to the desalting tower 1 through the resin return line 7. Subsequently, the cation resin remaining in the cation resin regeneration tower 2 is phase-shifted to the resin storage layer 4 and then transferred to the desalination tower 1 via the resin return line 7 to form the cation resin on the surface layer of the resin layer. . As a result, a resin layer having three layers having different mixing ratios of the cationic resin and the anionic resin is formed in the desalting tower 1.
[0008]
In the above operation, when transferring the anion resin from the anion resin regeneration tower 6 through the resin storage tank 4 to the desalination tower 1, the amount of the cation resin which is less than half the volume of the anion resin is reduced to the resin storage layer 4. And mixed with air, and then transferred to the desalination tower 1 to form an anion resin-rich lower layer in the tower. Then, the anion resin and the cation resin are mixed at a volume ratio of 1: 2 to 1: 2. When mixed with air at a ratio of 2: 1 and transferred to the desalination tower 1, a mixed bed of a normal ratio is formed in the middle part in the tower, and finally when the cationic resin is transferred to the desalination tower 1. Next, an anion resin in an amount equal to or less than half the volume of the cation resin is transferred to the resin reservoir 4, mixed with air, and then transferred to the desalting tower 1, where the cation resin-rich resin is introduced into the tower. By forming the upper layer, the mixing ratio of the cationic resin and the anionic resin in the desalting tower A resin layer may be formed with different three layers.
[0009]
Regarding the layer height of the resin layer to be formed, the upper and lower layers can be used at a ratio of 0.1 to 1, particularly 0.4 to 1, with respect to the intermediate layer 1. For example, each of the upper and lower layers is desirably 20 to 30 cm. The reason is as follows. The height of the resin layer of the condensate desalination unit of the BWR nuclear power plant is usually about 90 cm. When impurities are removed by passing the water to be treated through the ion exchange resin, impurity ions are removed as the water to be treated passes through the resin layer. Therefore, to obtain ultrapure water, a certain height of the resin layer is required. is necessary. A normal condensate desalination apparatus has a water flow velocity of about 120 m / h, and the inlet load assumed in the design standards is about 2 mg / L or 20 mg / L as a salt concentration as a main component of seawater. . In order to treat this, the resin layer height needs to be 30 cm or more for 2 mg / L and 50 cm or more for 20 mg / L. Therefore, if this mixed bed of 30 or 50 cm is formed in the middle of the resin layer, and the height of the remaining resin layer is equally distributed between the upper and lower layers, it is possible to form the upper and lower layers of 20 to 30 cm. .
[0010]
【Example】
Hereinafter, the present invention will be specifically described with reference to examples.
Example 1
Using a cationic resin SK1BN and an anionic resin SA10BN, which are ion exchange resins (manufactured by Mitsubishi Chemical Corporation) widely used in condensate desalination equipment of a BWR nuclear power plant, the resin layers of cases 1 to 6 shown in FIG. It was formed and subjected to a water flow test to measure the clad removal performance and the ion concentration leaked from the resin. In the test, the quality of the water to be treated, the temperature, the dissolved oxygen concentration, and the resin layer conditions were equivalent to those of an actual plant, and simulated the same conditions as those of an actual plant.
In FIG. 2, b is a mixed bed, (cation resin: anion resin ratio = 1: 1), a is an anion resin layer, c is a cation resin layer, and b <a is an anion resin rich layer (cation resin: anion resin). Ratio = 1: 2), b <c is a cationic resin rich layer (cation resin: anion resin ratio = 2: 1), and the height in parentheses is the layer height.
[0011]
A glass column having an inner diameter of 25 mm is filled with a cation resin and an anion resin, and fully deaerated at a specific resistance of 18 MΩ · cm at 45 ° C. and pure water containing a clad concentration of 20 μg / L is passed at a flow rate of 1 L / min. Then, the clad concentration and the ion concentration in the treated water were measured. The clad concentration was determined by branching a part of the treated water, passing about 50 L of water through a membrane filter having a pore size of 0.45 μm at 100 mL / min, and measuring the absolute amount of clad iron collected on the filter by atomic absorption spectrometry or fluorescent X-ray. Quantification was performed by a spectrophotometric method, and the concentration was calculated by dividing by the amount of water passing through the membrane filter. The ion concentration was determined by irradiating the treated water with ultraviolet light to decompose the TOC contained in the treated water, and analyzing the concentration of the produced sulfate ion by an ion chromatography method. The analysis was performed once a day, and the results of the average value during the one-month water passage period are shown in Table 1. According to Table 1, the effect is higher in case 5 than in case 6 and in case 5 than in case 4, but the effect is higher when the single upper and lower layers are thicker. As can be seen from Table 1, the present invention removes the cladding as compared with the prior art (Case 1), the case where the cationic resin layer is formed only on the surface layer (Case 2), and the case where the anionic resin is formed only on the lower layer (Case 3). It was confirmed that both the rate and the sulfuric acid concentration were excellent.
[0012]
[Table 1]
【The invention's effect】
According to the present invention, the condensate desalination treatment of the BWR nuclear power plant of the present invention described above can effectively remove the clad existing in the condensate water, reduce the amount of TOC leak from the apparatus, and improve the suspension corrosion. A condensate desalination method and apparatus capable of obtaining a high-purity treated water having a low product concentration and a low sulfate ion concentration can be provided.
[Brief description of the drawings]
FIG. 1 is a flow diagram showing an example of a condensate desalination apparatus used in the present invention.
FIG. 2 is a configuration diagram of a resin layer used in Example 1.
FIG. 3 is a schematic flow configuration diagram of a known BWR nuclear power plant.
[Explanation of symbols]
1: desalination tower, 2: cation resin regeneration tower, 3: cation resin transfer line, 4: resin storage tank, 5: anion resin transfer line, 6: anion resin regeneration tower, 7: resin return line, a: anion resin layer , B: mixed bed, c: cationic resin layer, b <a: anion resin rich layer, b <c: cationic resin rich layer
Claims (4)
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| JP2003071507A JP2004279227A (en) | 2003-03-17 | 2003-03-17 | Method and device for condensate demineralization |
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| JP2003071507A JP2004279227A (en) | 2003-03-17 | 2003-03-17 | Method and device for condensate demineralization |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009281875A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Method and device for condensate demineralization |
| JP2009279519A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Condensate demineralization method and condensate demineralizer |
| JP2009281873A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Method and device for condensate demineralization |
| CN103177781A (en) * | 2011-12-23 | 2013-06-26 | 江苏核电有限公司 | Method for controlling concentration of sulfate radical of pressurized water reactor nuclear power plant unit-loop |
-
2003
- 2003-03-17 JP JP2003071507A patent/JP2004279227A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2009281875A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Method and device for condensate demineralization |
| JP2009279519A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Condensate demineralization method and condensate demineralizer |
| JP2009281873A (en) * | 2008-05-22 | 2009-12-03 | Ebara Corp | Method and device for condensate demineralization |
| US8861670B2 (en) | 2008-05-22 | 2014-10-14 | Ebara Corporation | Method and apparatus for condensate demineralization |
| CN103177781A (en) * | 2011-12-23 | 2013-06-26 | 江苏核电有限公司 | Method for controlling concentration of sulfate radical of pressurized water reactor nuclear power plant unit-loop |
| CN103177781B (en) * | 2011-12-23 | 2015-08-26 | 江苏核电有限公司 | A kind of pressurized-water reactor nuclear power plant unit primary Ioops sulfate concentration control method |
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