JPS63315189A - Condensate treatment method - Google Patents
Condensate treatment methodInfo
- Publication number
- JPS63315189A JPS63315189A JP13569288A JP13569288A JPS63315189A JP S63315189 A JPS63315189 A JP S63315189A JP 13569288 A JP13569288 A JP 13569288A JP 13569288 A JP13569288 A JP 13569288A JP S63315189 A JPS63315189 A JP S63315189A
- Authority
- JP
- Japan
- Prior art keywords
- resin layer
- condensate
- water
- exchange resin
- ion exchange
- 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
- 238000000034 method Methods 0.000 title claims abstract description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 69
- 239000011347 resin Substances 0.000 claims abstract description 54
- 229920005989 resin Polymers 0.000 claims abstract description 54
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 41
- 239000013535 sea water Substances 0.000 claims abstract description 35
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 26
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 26
- 239000003729 cation exchange resin Substances 0.000 claims abstract description 15
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 13
- 238000011033 desalting Methods 0.000 claims abstract 3
- 238000010612 desalination reaction Methods 0.000 claims description 27
- 238000001514 detection method Methods 0.000 claims description 6
- 238000003672 processing method Methods 0.000 claims 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 abstract description 86
- 229910021529 ammonia Inorganic materials 0.000 abstract description 43
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract 4
- 238000011069 regeneration method Methods 0.000 description 12
- 238000005115 demineralization Methods 0.000 description 10
- 230000002328 demineralizing effect Effects 0.000 description 10
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 239000012535 impurity Substances 0.000 description 8
- 230000008929 regeneration Effects 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 238000007796 conventional method Methods 0.000 description 7
- 150000002500 ions Chemical class 0.000 description 5
- 229920001467 poly(styrenesulfonates) Polymers 0.000 description 4
- 230000002411 adverse Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 235000010755 mineral Nutrition 0.000 description 2
- 239000011707 mineral Substances 0.000 description 2
- 150000003839 salts Chemical group 0.000 description 2
- 238000005070 sampling Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 101100424709 Danio rerio tbxta gene Proteins 0.000 description 1
- 241000623377 Terminalia elliptica Species 0.000 description 1
- 238000003321 atomic absorption spectrophotometry Methods 0.000 description 1
- 238000001479 atomic absorption spectroscopy Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 235000010216 calcium carbonate Nutrition 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000013256 coordination polymer Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003292 glue Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Landscapes
- 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〕
本発明はボイラ、タービンなどのスケール生成および腐
食を防止するために、温床式イオン交換樹脂層を用いて
復水中に存在する不純物質を除去する復水脱塩処理方法
に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention removes impurities present in condensate using a hotbed type ion exchange resin layer in order to prevent scale formation and corrosion in boilers, turbines, etc. This invention relates to a condensate desalination treatment method.
一般にボイラ運転条件の高温高圧化にしたがい、復水処
理の重要性が広く認められるようになり、通常は温床式
イオン交換樹脂を充填した復水脱塩塔に通水することに
より良好な処理結果が得られている。この復水脱塩装置
には、強酸性陽イオン交換樹脂を形陰に再生したものき
、強塩基性陰イオン交換樹脂を０１１形に再生したもの
を混合して充填するのが普通であるが、温床式イオン交
換樹脂層はイオン交換能力により溶解性の不純物イオン
を除去するだけでなく、懸濁微粒子の大部分をも除去す
ることができる。In general, as boiler operating conditions become higher in temperature and pressure, the importance of condensate treatment has become widely recognized, and good treatment results are usually obtained by passing water through a condensate demineralization tower filled with a hotbed type ion exchange resin. is obtained. This condensate desalination equipment is usually filled with a mixture of a strongly acidic cation exchange resin regenerated into form 011 and a strongly basic anion exchange resin regenerated into form 011. Due to its ion exchange ability, the hot bed type ion exchange resin layer can not only remove soluble impurity ions but also remove most of the suspended particles.
従来この温床式イオン交換樹脂を充填した脱塩塔の運転
には、陽イオン交換樹脂が復水中のアンモニアと交換し
、アンモニアが破過した時点で樹脂の再生を行なうＨサ
イクル復水処理方法と、いま一つはアンモニアが破過し
た後も引き続きＮｔｌａ形樹脂を利用して処理を継続す
るアンモニアサイクル復水処理方法がある。最近では復
水脱塩装置の再生薬剤の節約、再生排液量の減少、運転
管理の面から、再生頻度の少ないアンモニアサイクル復
水脱塩を採用するところが多い。Conventionally, this hotbed type desalination tower filled with ion exchange resin has been operated using an H-cycle condensate treatment method in which the cation exchange resin exchanges ammonia in the condensate, and the resin is regenerated once the ammonia has broken through. Another method is an ammonia cycle condensate treatment method in which treatment continues using Ntla resin even after ammonia has broken through. Recently, many companies have adopted ammonia cycle condensate desalination, which requires less regeneration, in order to save regeneration chemicals in condensate desalination equipment, reduce the amount of regenerated effluent, and improve operational management.
しかしながら、アンモニアサイクルの運転においては１
１サイクルとは異なった種々の制限を受けるため、装置
が複雑となったり、樹脂の再生に長時間を要するなどの
問題点もあって、必ずしも完成された技術とは言えない
のが現状である。However, in the operation of the ammonia cycle, 1
Because it is subject to various limitations different from that of a single cycle, there are problems such as the equipment being complicated and the time it takes to regenerate the resin, so it cannot necessarily be said that it is a perfected technology. .
温床式イオン交換樹脂層をアンモニアサイクルで運転す
る場合の問題点の一つは、温床式イオン交換樹脂層中に
若干量存在する塩形樹脂がアンモニアブレーク時に不純
物リークの原因となる点である。これらの塩形樹脂は主
に樹脂の再生時に生成されるものである。One of the problems when operating a hot bed type ion exchange resin layer in an ammonia cycle is that a small amount of salt form resin present in the hot bed type ion exchange resin layer causes impurity leakage during ammonia break. These salt-form resins are mainly produced during resin regeneration.
一方温床式イオン交換樹脂層の再生は、逆洗により陽イ
オン交換樹脂と陰イオン交換樹脂とを分離した後、陽イ
オン交換樹脂層には鉱酸を、陰イオン交換樹脂層には苛
性ソーダを通薬することにより行なわれるが、陽イオン
交換樹脂と陰イオン交換樹脂とを完全に分離することは
困難であるので、陽イオン交換樹脂層中に混入した陰イ
オン交換樹脂は鉱酸と接触することによりＣｆｆ形、Ｓ
Ｏ。On the other hand, in hotbed type ion exchange resin layer regeneration, after separating the cation exchange resin and anion exchange resin by backwashing, mineral acid is applied to the cation exchange resin layer and caustic soda is passed to the anion exchange resin layer. However, it is difficult to completely separate the cation exchange resin and anion exchange resin, so the anion exchange resin mixed in the cation exchange resin layer must come into contact with the mineral acid. According to Cff type, S
O.
形となり、陰イオン交換樹脂層中に混入した陽イオン交
換樹脂は苛性ソーダと接触することによりＮａ形となる
。The cation exchange resin mixed into the anion exchange resin layer becomes Na form by contacting with caustic soda.
このＮａ形樹脂はアンモニアブレーク時にＮ１１４”と
イオン交換を行ないＮａ“を放出し、ｃｐ形、Ｓ０４形
樹脂もアンモニアブレーク時に０１１−とイオン交換を
行ないＣｎ−、ｓｏ、”−を放出するものである。This Na type resin performs ion exchange with N114'' during an ammonia break and releases Na'', and the CP type and S04 type resins also perform ion exchange with 011- during an ammonia break and release Cn-, so, and ``-. be.
したがって、アンモニアサイクルで運転する場合には塩
形樹脂の生成を極めて低く押さえることができるような
樹脂の再生方法をとる必要がある。Therefore, when operating on an ammonia cycle, it is necessary to use a resin regeneration method that can keep the production of salt-type resin to an extremely low level.
いま一つの問題点は、アンモニアサイクル時においては
Ｈサイクル時より不純物イオンの除去能力がやや劣るた
め、アンモニアサイクル時において海水リーク（復水の
純度悪化）が生じた場合には不純物イオンがリークし易
く、また不純物イオンが破過に至る時間もＨサイクル時
よりも短いなど、海水リーク時の処理性能に若干の問題
が残ることである。Another problem is that the ability to remove impurity ions during the ammonia cycle is slightly inferior to that during the H cycle, so if seawater leaks (deterioration of condensate purity) during the ammonia cycle, impurity ions will leak. However, the time required for impurity ions to break through is shorter than that during the H cycle, which leaves some problems with the treatment performance when seawater leaks.
このため現時点では、アンモニアサイクル時に海水リー
クの発生が検知されたならば、直ちに樹脂の再生を開始
し、脱塩塔の運転を順次Ｈサイクルへ切り換えるのが安
全と考えられている。しかしながら樹脂の再生には、あ
る程度の時間を要するため、海水リークの規模によって
は樹脂の再生が間に合わず、電力の安定供給に支障をき
たしたりあるいはボイラ、タービンに悪影響を及ぼすこ
とも考えられる。For this reason, at present, if seawater leakage is detected during the ammonia cycle, it is considered safe to immediately start regenerating the resin and sequentially switch the operation of the desalination tower to the H cycle. However, it takes a certain amount of time to regenerate the resin, so depending on the scale of the seawater leak, the resin may not be regenerated in time, which may impede the stable supply of electricity or adversely affect the boiler and turbine.
本発明は、従来技術の上記問題点に鑑み、アンモニアサ
イクル時に万一海水リークが発生しても、電力供給ある
いはボイラ、タービンに何ら悪影響を及ばずことなく極
めて迅速、適確かつ安全に対処できる復水脱塩処理方法
を提供することを目的としたものである。In view of the above-mentioned problems of the prior art, the present invention makes it possible to deal with the occurrence of a seawater leak extremely quickly, appropriately, and safely without any adverse effect on the power supply, boiler, or turbine in the event that a seawater leak occurs during the ammonia cycle. The purpose of this invention is to provide a condensate desalination treatment method.
本発明は、形陰陽イオン交換樹脂と０１１形陰イオン交
換樹脂を混合した温床式イオン交換樹脂層に下向流で通
水する復水脱塩処理方法において、同一の脱塩塔に前記
温床式イオン交換樹脂層を、前段の上層樹脂層と後段の
下層樹脂層として充填すると共に、流入する復水中の海
水リーク検知機構を設け、平常時においては前記前段の
上層樹脂層のみに通水して処理し、アンモニアサイクル
で復水脱塩を続行し、復水中に海水リークが検知された
ときには、自動弁の開閉操作により直ちに前記前段の上
層樹脂層からの流出水を前記後段の下層樹脂層にも通水
を開始し、引き続いて処理水を得ることを特徴とする復
水処理方法である。The present invention provides a condensate desalination treatment method in which water is passed in a downward flow through a hot bed type ion exchange resin layer in which a type anion exchange resin and a 011 type anion exchange resin are mixed, and the hot bed type ion exchange resin is added to the same desalination tower. The ion exchange resin layer is filled as an upper resin layer in the former stage and a lower resin layer in the latter stage, and a seawater leak detection mechanism in the inflowing condensate is provided, and under normal conditions, water is passed only to the upper resin layer in the former stage. When a seawater leak is detected in the condensate, the water flowing out from the upper resin layer of the previous stage is immediately transferred to the lower resin layer of the latter stage by opening and closing an automatic valve. This is a condensate treatment method characterized by starting water flow and subsequently obtaining treated water.
すなわち本発明の復水処理方法は、アンモニアサイクル
用に再生された形陰陽イオン交換樹脂とＯＨ形陰陽イオ
ン交換樹脂混合した温床式イオン交換樹脂層に下向流で
復水を通水し復水中の不純物を除去する復水脱塩処理方
法において、同一の脱塩浴に、再生された温床式イオン
交換樹脂層を前段の上層樹脂層と後段の下層樹脂層とに
分割して充填すると共に、流入する復水中に海水リーク
が発生したことを検知するための検知機構を設け、平常
時においては復水を前記前段の上層樹脂層のみに通水し
、アンモニアブレーク後も処理をｍ続して１１サイクル
からアンモニアサイクルへと移行するのであるが、アン
モニアサイクル復水脱塩を行なっている間に海水リーク
が検知されたならば、自動弁の開閉状態を切り換えるこ
とによって、直ちに前段の上層樹脂層の後段側にＨ−０
）１形のまま待機させていた後段の下層樹脂層に対して
、前段の上層樹脂層からの流出水の通水を開始すること
により、瞬時にアンモニアサイクルからＨサイクルに切
り換え、引き続いて高純度の処理水を得ることを特徴と
するものである。That is, in the condensate treatment method of the present invention, condensate is passed in a downward flow through a hot bed type ion exchange resin layer in which an anion and cation exchange resin regenerated for the ammonia cycle and an OH anion and cation exchange resin are mixed. In a condensate desalination treatment method for removing impurities, the same desalination bath is filled with a regenerated hotbed ion exchange resin layer divided into an upper resin layer in the former stage and a lower resin layer in the latter stage, and A detection mechanism is provided to detect the occurrence of a seawater leak in the inflowing condensate, and under normal conditions, the condensate is passed only through the upper resin layer of the previous stage, and treatment continues for m even after the ammonia break. The 11th cycle shifts to the ammonia cycle, but if a seawater leak is detected during ammonia cycle condensate desalination, the upper resin layer of the previous stage is immediately removed by switching the open/close state of the automatic valve. H-0 on the rear side of
) By starting to flow water from the upper resin layer of the previous stage to the lower resin layer of the latter stage, which had been kept in standby as type 1, the ammonia cycle was instantly switched to the H cycle, and the high purity This method is characterized by obtaining treated water.
本発明の実施態様を図面を参照しつつ説明すれば、第１
図は中間集水管を設けた脱塩塔及び関連設備を示すもの
であって、脱塩塔１は、その上部にば復水散水機構とし
ての復水流人管２を、塔中央部には処理水集水機構とし
ての第１処理水流出管３ （中間集水管）を、塔底部に
はやはり処理水集水機構としての第２処理水流出管４を
それぞれ備えている。第１処理水流出管３と第２処理水
流出管４は、それぞれ処理水取り出し位置（集水位Ｗ）
を切り換えるための自動弁５．６を介して合流し、合流
部の下流側には処理の終点を検知するだめの処理水水質
計７が設けてあり、復水流人管２の上流側には、前記自
動弁５．６へ信号を送ってこれらの開閉を自動的に切り
換え処理水取り出し位置を制御するための海水リーク検
知機構としての復水水質計８が設けである。脱塩塔１の
内部にはアンモニアサイクル用に再生した塩形樹脂含有
率の低い温床式イオン交換樹脂Ｎ９が充填しである。The embodiments of the present invention will be described with reference to the drawings.
The figure shows a desalination tower equipped with an intermediate water collection pipe and related equipment.The desalination tower 1 has a condensate flow pipe 2 as a condensate water sprinkling mechanism in the upper part of the demineralization tower 1, and a water treatment pipe in the center of the tower. A first treated water outflow pipe 3 (intermediate water collection pipe) is provided as a water collection mechanism, and a second treated water outflow pipe 4 is provided at the bottom of the tower as a treated water collection mechanism. The first treated water outflow pipe 3 and the second treated water outflow pipe 4 are located at respective treated water takeout positions (water collection level W).
A treated water quality meter 7 is installed on the downstream side of the merging point to detect the end point of the treatment, and on the upstream side of the condensate flow pipe 2. A condensate water quality meter 8 is provided as a seawater leak detection mechanism for sending signals to the automatic valves 5 and 6 to automatically switch the opening and closing of these valves to control the treated water take-out position. The inside of the demineralization tower 1 is filled with a hot bed type ion exchange resin N9 having a low content of salt form resin, which has been regenerated for the ammonia cycle.
アンモニアサイクル用の樹脂再生方法は種々あるが、本
発明では樹脂の再生方法には特に限定はなく、高純度の
処理水が得られるものであればいずれの再生方法を用い
てもかまわない。There are various resin regeneration methods for the ammonia cycle, but in the present invention, the resin regeneration method is not particularly limited, and any regeneration method may be used as long as highly purified treated water can be obtained.
このような復水処理装置では、平常時においては復水流
人管２より復水を流入せしめ、自動弁６を閉じ、自動弁
５を開けることにより、第１処理水流出管３より処理水
を取り出す。すなわち平常時においては復水水質が良好
なので樹脂の全量を使用する必要はなく、温床式イオン
交換樹脂層９の内、上部のｈｌに相当する前段の上層樹
脂層のみを用いて処理を行なう。この状態で処理を継続
すると、ｈｌの部分の陽イオン交換樹脂はしだいにＮＨ
イ形に変換されるため、脱塩塔１の運転はＨサイクルか
らアンモニアサイクルへと移行するが、温床式イオン交
換樹脂層９の下部のｈ２に相当する後段の下層樹脂層に
は復水が流れないので、この部分の樹脂は再生直後と同
様にＩＪ形、Ｏ形陰を保っている。In such a condensate treatment device, in normal times, condensate is allowed to flow in through the condensate flow pipe 2, and treated water is discharged from the first treated water outflow pipe 3 by closing the automatic valve 6 and opening the automatic valve 5. Take it out. That is, in normal times, since the quality of condensate water is good, it is not necessary to use the entire amount of resin, and only the upper resin layer of the hot bed type ion exchange resin layer 9 corresponding to the upper hl is used for the treatment. If the treatment is continued in this state, the cation exchange resin in the hl portion will gradually become NH
Since the demineralization column 1 is converted to the A type, the operation of the demineralization tower 1 shifts from the H cycle to the ammonia cycle, but condensate is present in the lower resin layer of the latter stage corresponding to h2 at the bottom of the hot bed type ion exchange resin layer 9. Since it does not flow, the resin in this area maintains the IJ-shape and O-shape as it did immediately after regeneration.
このように脱塩塔の運転がアンモニアサイクルに移行し
た後に、万一復水水質計８により海水リークが検知され
たならば、この検知信号により直ちに自動弁５を閉じ、
自動弁６を開は処理水の取り出しを第１処理水流出管３
から第２処理水流出管４へ切り換える。この操作により
、温床式イオン交換樹脂層９の内、上部のり、のみを使
用した処理から全樹脂層を使用する処理に切り換わる。If a seawater leak is detected by the condensate water quality meter 8 after the operation of the desalination tower has shifted to the ammonia cycle in this way, the automatic valve 5 is immediately closed based on this detection signal.
Open the automatic valve 6 to take out the treated water through the first treated water outflow pipe 3.
and then switch to the second treated water outflow pipe 4. By this operation, the process is switched from the process using only the upper part of the hot bed type ion exchange resin layer 9 to the process using the entire resin layer.
温床式イオン交換樹脂層９の下部ｈ２の部分は形陰、Ｏ
形陰であるので自動弁５．６の開閉操作のみで脱塩塔の
運転をアンモニアサイクルからＨサイクルへ切り換える
ことが可能となるわけである。The lower part h2 of the hot bed type ion exchange resin layer 9 has a shape of 0.
Since it is a closed-loop system, it is possible to switch the operation of the demineralization tower from the ammonia cycle to the H cycle simply by opening and closing the automatic valves 5 and 6.
この１うに、復水水質計８と自動弁５．６を連動させる
ことで、海水リークの検知と同時に自動的にアンモニア
サイクルからＩ］サイクルへ切り換えることができる。By interlocking the condensate water quality meter 8 and the automatic valve 5.6 in this manner, it is possible to automatically switch from the ammonia cycle to the I cycle at the same time as seawater leak is detected.
この場合、海水成分の大部分は上部のり、に相当する樹
脂層により除去できるので、下部のｈ２に相当する樹脂
層の必要量は少なくてすむ。このように、本発明ではア
ンモニアサイクル、Ｈ−ＯＨサイクルの利点を最大限に
生かすようにした結果、樹脂の総量は従来法と同等であ
りながら、海水リークに充分対応できる温床式イオン交
換樹脂塔を構成することが可能となったものである。In this case, most of the seawater components can be removed by the resin layer corresponding to the upper glue, so that the required amount of the lower resin layer corresponding to h2 is small. In this way, the present invention takes full advantage of the advantages of the ammonia cycle and the H-OH cycle, and as a result, the hot bed type ion exchange resin tower is able to fully cope with seawater leakage, while the total amount of resin is the same as that of the conventional method. This makes it possible to configure the following.
なお、アンモニアサイクルからＨサイクルへの切り換え
に際しては、第２処理水流出管４からの処理水純度を上
げるために、あらかじめｈ２の部分の樹脂層に短時間の
循環通水を行なうか、若干量のブローを行なうことが好
ましいが、これらの準備操作をも自動化しておけば、海
水リークという非常時においてもスイッチ操作一つで対
処できるため、現場の運転員の負担を著しく軽減するこ
とができる。In addition, when switching from the ammonia cycle to the H cycle, in order to increase the purity of the treated water from the second treated water outflow pipe 4, first circulate water through the resin layer at h2 for a short period of time, or add a small amount of water. It is preferable to carry out a blow-off process, but if these preparatory operations are also automated, even in the event of an emergency such as a seawater leak, it can be handled with a single switch operation, significantly reducing the burden on on-site operators. .
第２図は脱塩塔を４塔備え常時３塔の脱塩塔で復水を処
理し、１塔は予備とする復水処理装置に本発明を適用し
た場合（第２図（■））と従来法（第２図（Ｉ））の場
合についての、アンモニアサイクルの間に海水リークが
発生した時の運転要領及び処理能力を比較したものであ
る。Figure 2 shows a case in which the present invention is applied to a condensate treatment equipment equipped with four demineralization towers, in which condensate is always treated in three demineralization towers, and one tower is kept as a standby (Fig. 2 (■)) This figure compares the operating procedures and treatment capacity when a seawater leak occurs during the ammonia cycle between the conventional method (FIG. 2 (I)) and the conventional method (FIG. 2 (I)).
すなわち海水リーク発生前はＡ、Ｂ、Ｃの３塔をアンモ
ニアサイクルで運転しているとすると、従来法の場合に
は海水リークの検知とともに予備の脱塩塔りへの通水を
開始し、かわりに脱塩塔Ａへの通水を停止し、樹脂を再
生塔へ移送し樹脂の再生を行なうのであるが、脱塩塔Ｂ
、脱塩塔Ｃはアンモニアサイクルのまま処理をｍｍする
ことになり不純物イオンがリークし易く、ボイラ、ター
ビンに悪影響を及ぼすことになり、電力の安定供給にも
影響を及ぼすことにもなる。In other words, assuming that the three towers A, B, and C were operating on an ammonia cycle before a seawater leak occurred, in the case of the conventional method, water flow to the standby desalination tower would start as soon as a seawater leak was detected. Instead, the water flow to demineralization tower A is stopped and the resin is transferred to the regeneration tower to regenerate the resin.
Since the demineralization tower C continues to process in the ammonia cycle, impurity ions are likely to leak, which will have an adverse effect on the boiler and turbine, and will also affect the stable supply of electric power.
これに対し本発明では、海水リークの検知とともに脱塩
塔りへの通水を開始するが、同時に脱塩塔Ｂ、脱塩塔Ｃ
の処理水出口を切り換えることにより脱塩塔りだけでな
く３塔ともにＨサイクルの運転が可能となるため、引き
続き高純度の水をボイラへ供給することができる。In contrast, in the present invention, water flow to the desalination tower is started upon detection of seawater leak, but at the same time, the water flow to the desalination tower B and C
By switching the treated water outlet, not only the desalination tower but also all three towers can be operated in the H cycle, making it possible to continue supplying high-purity water to the boiler.
上記実施態様では、海水リークを検知するまでは復水を
第１の温床式イオン交換樹脂層のみに通水し、海水リー
クの検知時板後においては第１及び第２の温床式イオン
交換樹脂層に（直列的に）通水された分のみを処理水と
して取り出す。In the above embodiment, until a seawater leak is detected, condensate is passed only through the first hotbed type ion exchange resin layer, and after the seawater leak is detected, the condensate is passed through the first and second hotbed type ion exchange resin layer. Only the amount of water that has passed through the layers (in series) is taken out as treated water.
以下に、本発明による実施例及び従来法による比較例を
示す。Examples according to the present invention and comparative examples according to the conventional method are shown below.
大部分がＮＨ，形となっている強酸性陽イオン交換樹脂
Ｄｏｉｙｅｘ ＨＣＲ−ＷＺを再生レベル１０ｅｑ／
７！−Ｒの塩酸でＩ（形に再生したものと、大部分がＯ
形陰となっている強塩基性陰イオン交換樹脂Ｄｏｗｅｘ
５ＢＲ−Ｐを再生レベル１０ｅｑ／ ｊ！−Ｒの苛性
ソーダでＯ１ｌ形に再生したものを準備し、内径５０酊
のアクリル製カラムにＤｏｗｅｘ ＨＣＲ−ＷＺとＤｏ
ｗｅｘ ５ＢＲ−Ｐとを７：５に混合したものを１２０
０ｆｌ充填し、その上部にはＤｏｗｅｘ１１ＣＩ？−Ｗ
Ｚを単独で３００ｆｌ充填した。カラム全体ではＤｏｗ
ｅｘ ＩＩｃＲ−ＷＺとＤｏｗｅｘ ５ＢＲ−Ｐとの混
合比は２：１である。Recycle the strongly acidic cation exchange resin Doiyex HCR-WZ, which is mostly in the form of NH, at a regeneration level of 10eq/
7! - I with hydrochloric acid of R (regenerated into form and mostly O
Strongly basic anion exchange resin Dowex
5BR-P playback level 10eq/j! -R regenerated into O1L form with caustic soda, prepared, and placed in an acrylic column with an inner diameter of 50mm and Dowex HCR-WZ and Dowex HCR-WZ.
120 mixed with wex 5BR-P at a ratio of 7:5
Filled with 0fl and Dowex11CI? -W
300 fl of Z was filled alone. Dow for the whole column
The mixing ratio of ex IIcR-WZ and Dowex 5BR-P is 2:1.
このカラムの上部より、純水にアンモニアを５ｍｇ／
ｌａｓ ＣａＣＯ３添加した人工復水をＬ ＶＩＩＯｍ
／ｈで通水し、カラム底部から６００＋＋ｎ上方の中間
サンプリングコックより処理水を取り出した。アンモニ
アブレーク時の処理水中のＮａ“をフレームレス原子吸
光光度法で測定したところ０．５〜１．０μｇ／／！ａ
ｓＮａであり、酸導電率は０．Ｉ Ｉｔｓ ／ｃｒｎ以
下であった。中間サンプリングコックより上方の陽イオ
ン交換樹脂がアンモニアで飽和した後に、人工復水にＮ
ａ（ｌを３３ ｍｇ／ Ｒａｓ ＣａＣ０＋添加して海
水リークを模し、処理水の取り出しをカラム底部に切り
換えて処理水中のＮａ”を測定したところ０．１ μｇ
／βａｓ Ｎａ以下となり酸導電率は０．１μ５７ｃｍ
以下であった。また、海水リークの状態で処理を継続し
ても５時間以内は処理水中のＮａ“は１μｇ／ｊ！ａｓ
Ｎａ以下であり、酸導電率は０．１μ３７ｃｍ以下であ
った。From the top of this column, add 5mg/ammonia to the pure water.
las CaCO3 added artificial condensate to L VIIOm
Water was passed through the column at a rate of 1/h, and treated water was taken out from an intermediate sampling cock located 600++n above the bottom of the column. The amount of Na in the treated water during the ammonia break was measured using flameless atomic absorption spectrometry and was 0.5 to 1.0 μg//!a
sNa, and the acid conductivity is 0. I Its /crn or less. After the cation exchange resin above the intermediate sampling cock is saturated with ammonia, N is added to the artificial condensate.
33 mg/Ras CaC0+ was added to simulate a seawater leak, the treated water was taken out to the bottom of the column, and Na'' in the treated water was measured and found to be 0.1 μg.
/βas Na or less, acid conductivity is 0.1μ57cm
It was below. In addition, even if the treatment is continued in the state of seawater leak, the Na” in the treated water will be 1 μg/j!as within 5 hours.
Na or less, and acid conductivity was 0.1μ37cm or less.
上記実施例に用いたのと同じ樹脂を同一の再生条件及び
樹脂層構成（したがって、各樹脂の充填量は実施例と同
じ）で内径５０酊のアクリル製カラムに充填し、純水に
アンモニアを５ｍｇ／７！ａｓＣａＣＯｚ添加した人工
復水をＬＶ１１０ｍ／ｈでカラム上部より通水し、カラ
ム底部より処理水を取り出した。アンモニアブレーク時
の処理水中のＮａ′″をフレームレス原子吸光光度法で
測定したところ０・５〜１・０μｇ／７！ａｓＮａであ
り、酸導電率番よ０．１μｓ／ｃｍ以下であった。カラ
ム内の陽イオン交換樹脂がアンモニアで飽和した後に、
海水リークを模して人工復水にＮａＣρを３３ｍｇ／β
ａｓＣａＣＯ３添加して処理水中のＮａ”を測定したと
ころ、ＮａＣ７！添加と同時に１μｇ／ｆｆａｓＮａを
超え、酸導電率もＯ，１μ５７０ｍを超えた。The same resin used in the above example was packed into an acrylic column with an inner diameter of 50 mm under the same regeneration conditions and resin layer configuration (therefore, the amount of each resin packed was the same as in the example), and ammonia was added to pure water. 5mg/7! Artificial condensate added with asCaCOz was passed through the top of the column at a LV of 110 m/h, and treated water was taken out from the bottom of the column. When Na''' in the treated water during the ammonia break was measured by flameless atomic absorption spectrophotometry, it was 0.5 to 1.0 μg/7!asNa, and the acid conductivity was less than 0.1 μs/cm. After the cation exchange resin in the column is saturated with ammonia,
Add 33mg/β of NaCρ to artificial condensate to simulate a seawater leak.
When asCaCO3 was added and Na'' in the treated water was measured, it exceeded 1 μg/ffasNa at the same time as NaC7!, and the acid conductivity also exceeded O,1μ570m.
〔発明の効果］
以上のように、同一の脱塩塔に温床式イオン交換樹脂層
を前段と後段に分割して充填して処理する本発明方法に
よれば、従来法と同等量の樹脂を使用するにも拘らず、
アンモニアサイクルの間に万一海水リークが発生しても
、弁の開閉操作のみで全脱塩塔を直ちにアンモニアサイ
クルからＨサイクルに切り換えることができるので、海
水リークが発生しても、しばらくの間は出力を落すこと
なく安全に発電を継続することができ、この間に予備の
ユニットを起動するなどにより安定した電力供給が確保
され、またボイラ、タービンにも何らの悪影響を及ぼす
こともなく、さらに、アンモニアサイクルからＨサイク
ルへの切り換えを自動的に行なうことができるので、操
作が極めて簡便となるばかりでなく海水リークへの対処
が著しく迅速・適確なものとなり、アンモニアサイクル
復水脱塩の持つ長所を十分に発揮することが可能となる
とともに、海水リークに対しても安全に対処することが
できるなどの利点があり、復水器冷却水の塩分濃度が高
い場合、特に復水器冷却水に海水を利用する汽力発電所
にとって利用価値は極めて大きいものである。[Effects of the Invention] As described above, according to the method of the present invention, in which the same desalination tower is filled with a hot bed type ion exchange resin layer divided into the front stage and the rear stage, the same amount of resin can be used as in the conventional method. Despite using
Even if a seawater leak occurs during the ammonia cycle, all desalination towers can be immediately switched from the ammonia cycle to the H cycle by simply opening and closing the valves. can safely continue generating electricity without reducing output, and during this time, by starting up spare units, etc., a stable power supply is ensured, and there is no negative impact on the boiler or turbine. Since it is possible to automatically switch from the ammonia cycle to the H cycle, not only is the operation extremely simple, but the response to seawater leaks is extremely quick and accurate, and the ammonia cycle condensate desalination In addition to making it possible to fully utilize its advantages, it also has the advantage of being able to safely deal with seawater leaks. The utility value for steam power plants that use seawater as water is extremely large.
第１図は本発明の実施態様を示すものであって、脱塩塔
に中間集水管を設けた場合の脱塩塔の縦断面図、第２図
は複数の脱塩塔を組合わせた場合の復水処理方法を示す
系統説明図であって、（１）は従来方法、（ＩＩ）は本
発明方法についてのものである。
１・・・脱塩塔、２・・・復水流入管、３・・・第１処
理水流出管、４・・・第２処理水流出管、５．６・・・
自動弁、７・・・処理水水質計、８・・・復水水質計、
９・・・温床式イオン交換樹脂層。Fig. 1 shows an embodiment of the present invention, and is a vertical cross-sectional view of a desalination tower when an intermediate water collection pipe is provided in the desalination tower, and Fig. 2 shows a case where a plurality of desalination towers are combined. FIG. 1 is a system explanatory diagram showing a condensate treatment method, in which (1) is a conventional method and (II) is a method of the present invention. 1... Desalination tower, 2... Condensate inflow pipe, 3... First treated water outflow pipe, 4... Second treated water outflow pipe, 5.6...
Automatic valve, 7... Treated water quality meter, 8... Condensate water quality meter,
9...Hot bed type ion exchange resin layer.
Claims (2)
を混合した温床式イオン交換樹脂層に下向流で通水する
復水脱塩処理方法において、同一の脱塩塔に前記温床式
イオン交換樹脂層を、前段の上層樹脂層と後段の下層樹
脂層として充填すると共に、流入する復水中の海水リー
ク検知機構を設け、平常時においては前記前段の上層樹
脂層のみに通水して処理し、アンモニアサイクルで復水
脱塩を続行し、復水中に海水リークが検知されたときに
は、自動弁の開閉操作により直ちに前記前段の上層樹脂
層からの流出水を前記後段の下層樹脂層にも通水を開始
し、引き続いて処理水を得ることを特徴とする復水処理
方法。(1) In a condensate desalination treatment method in which water is passed in a downward flow through a hot bed type ion exchange resin layer in which an H type cation exchange resin and an OH type anion exchange resin are mixed, the hot bed type The ion exchange resin layer is filled as an upper resin layer in the former stage and a lower resin layer in the latter stage, and a seawater leak detection mechanism in the inflowing condensate is provided, and under normal conditions, water is passed only to the upper resin layer in the former stage. When a seawater leak is detected in the condensate, the water flowing out from the upper resin layer of the previous stage is immediately transferred to the lower resin layer of the latter stage by opening and closing an automatic valve. A condensate treatment method characterized by starting water flow and subsequently obtaining treated water.
求の範囲第１項記載の処理方法。(2) The processing method according to claim 1, wherein a plurality of the desalting towers are arranged in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13569288A JPS63315189A (en) | 1988-06-03 | 1988-06-03 | Condensate treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP13569288A JPS63315189A (en) | 1988-06-03 | 1988-06-03 | Condensate treatment method |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP617280A Division JPS56102990A (en) | 1980-01-22 | 1980-01-22 | Disposal of condensate and its apparatus |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63315189A true JPS63315189A (en) | 1988-12-22 |
| JPH0312952B2 JPH0312952B2 (en) | 1991-02-21 |
Family
ID=15157683
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP13569288A Granted JPS63315189A (en) | 1988-06-03 | 1988-06-03 | Condensate treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63315189A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06315683A (en) * | 1993-04-30 | 1994-11-15 | Seisui Kogyo Kk | Mixed bed type ion exchange device and production of pure water and ultrapure water using mixed bed type ion exchange device |
| CN105110419A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Vibrating motor vibration and foam pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110416A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Vibrating motor vibration and rubber pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110415A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Self-balancing vibration and rubber pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110417A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Self-balancing vibration and foam pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105217726A (en) * | 2015-10-06 | 2016-01-06 | 吉首大学 | Electric and magnetic oscillation spring shock absorption fluidized bed-type ion exchange water processor |
| CN107285519A (en) * | 2017-07-25 | 2017-10-24 | 浙江浙能绍兴滨海热电有限责任公司 | A kind of condensed water precision processing system |
| CN110067610A (en) * | 2018-01-24 | 2019-07-30 | 三菱日立电力系统株式会社 | The operation method and steam power plant of generating equipment |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101467832B1 (en) * | 2013-12-18 | 2014-12-02 | (주)부로무역 | An aqueous solution of a salt spreader manufacturer |
-
1988
- 1988-06-03 JP JP13569288A patent/JPS63315189A/en active Granted
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06315683A (en) * | 1993-04-30 | 1994-11-15 | Seisui Kogyo Kk | Mixed bed type ion exchange device and production of pure water and ultrapure water using mixed bed type ion exchange device |
| CN105110419A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Vibrating motor vibration and foam pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110416A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Vibrating motor vibration and rubber pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110415A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Self-balancing vibration and rubber pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105110417A (en) * | 2015-10-06 | 2015-12-02 | 吉首大学 | Self-balancing vibration and foam pad shock absorption fluidized bed type ion exchange water treatment device |
| CN105217726A (en) * | 2015-10-06 | 2016-01-06 | 吉首大学 | Electric and magnetic oscillation spring shock absorption fluidized bed-type ion exchange water processor |
| CN107285519A (en) * | 2017-07-25 | 2017-10-24 | 浙江浙能绍兴滨海热电有限责任公司 | A kind of condensed water precision processing system |
| CN110067610A (en) * | 2018-01-24 | 2019-07-30 | 三菱日立电力系统株式会社 | The operation method and steam power plant of generating equipment |
| CN110067610B (en) * | 2018-01-24 | 2021-10-15 | 三菱动力株式会社 | Method for operating power plant and thermal power plant |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0312952B2 (en) | 1991-02-21 |
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