JPH0133227B2 - - Google Patents
Info
- Publication number
- JPH0133227B2 JPH0133227B2 JP21944086A JP21944086A JPH0133227B2 JP H0133227 B2 JPH0133227 B2 JP H0133227B2 JP 21944086 A JP21944086 A JP 21944086A JP 21944086 A JP21944086 A JP 21944086A JP H0133227 B2 JPH0133227 B2 JP H0133227B2
- Authority
- JP
- Japan
- Prior art keywords
- layer
- cation
- exchange resin
- resin
- tower
- 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.)
- Expired
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 39
- 239000011347 resin Substances 0.000 claims description 34
- 229920005989 resin Polymers 0.000 claims description 34
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 30
- 230000008929 regeneration Effects 0.000 claims description 29
- 238000011069 regeneration method Methods 0.000 claims description 29
- 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 description 28
- 150000001768 cations Chemical class 0.000 claims description 28
- 239000003729 cation exchange resin Substances 0.000 claims description 27
- 238000005115 demineralization Methods 0.000 claims description 21
- 230000002328 demineralizing effect Effects 0.000 claims description 21
- 239000003957 anion exchange resin Substances 0.000 claims description 18
- 238000000034 method Methods 0.000 claims description 18
- 229910021529 ammonia Inorganic materials 0.000 claims description 14
- 239000002253 acid Substances 0.000 claims description 12
- 150000001450 anions Chemical class 0.000 claims description 12
- 238000010612 desalination reaction Methods 0.000 claims description 6
- 230000002378 acidificating effect Effects 0.000 claims description 5
- 239000003513 alkali Substances 0.000 claims description 5
- 238000011001 backwashing Methods 0.000 claims description 2
- 238000011033 desalting Methods 0.000 claims description 2
- 239000003456 ion exchange resin Substances 0.000 claims description 2
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 2
- 238000005201 scrubbing Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 description 9
- 150000002500 ions Chemical class 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000005260 corrosion Methods 0.000 description 3
- 230000007797 corrosion Effects 0.000 description 3
- 229910001385 heavy metal Inorganic materials 0.000 description 3
- 239000011734 sodium Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 238000010494 dissociation reaction Methods 0.000 description 2
- 230000005593 dissociations Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 229910001415 sodium ion Inorganic materials 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- -1 ammonium ions Chemical class 0.000 description 1
- 238000005349 anion exchange Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 238000005341 cation exchange Methods 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000012492 regenerant Substances 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 150000003385 sodium Chemical class 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、ボイラやタービンなどのスケール生
成および腐蝕を防止するために復水中に含有する
不純物を除去するため復水を浄化処理する方法に
関するものである。[Detailed Description of the Invention] [Field of Industrial Application] The present invention relates to a method for purifying condensate to remove impurities contained in the condensate in order to prevent scale formation and corrosion in boilers, turbines, etc. It is something.
一般に、火力発電所においてはボイラで生成さ
れた高温高圧の水蒸気によつて発電用タービンを
回転させ、使用後の水蒸気は復水器で凝縮させた
のち、再びボイラ給水として使用するという水循
環を行つているが、配管の腐蝕生成物や復水器冷
却水のリークなどによる塩類やシリカなどの不純
物が循環水中に蓄積されるのを防ぐために、大型
ユニツトでは復水処理装置を設けるのが普通であ
る。この復水処理装置には、種々の方式がある
が、普通に多く用いられているものはＨ形の強酸
性カチオン交換樹脂（以下カチオン交換樹脂とよ
ぶ）とOH形の強塩基性アニオン交換樹脂（以下
アニオン交換樹脂とよぶ）を混合して充填した脱
塩塔である。一方、循環水のPH調整をすることに
より配管の腐蝕を防ぐことは広く行われており、
この目的のため循環水中にはアンモニアが注入さ
れる。復水処理装置の目的は先に示したような不
純物を除去することであるが、その機能からして
本来「不純物」ではないアンモニウムイオンもＨ
形のカチオン交換樹脂に吸着されるため、これが
カチオン交換樹脂の負荷となり、結局脱塩塔の再
生頻度が高くなるという問題が生ずる。
Generally, in thermal power plants, high-temperature, high-pressure steam generated in a boiler rotates a power generation turbine, and the used steam is condensed in a condenser and then used again as boiler feed water, which is a water cycle. However, in order to prevent impurities such as salts and silica from accumulating in the circulating water due to corrosion products in pipes or leaks of condenser cooling water, it is common to install a condensate treatment device in large units. be. There are various types of condensate treatment equipment, but the most commonly used ones are H-type strongly acidic cation exchange resin (hereinafter referred to as cation exchange resin) and OH-type strongly basic anion exchange resin. This is a desalination tower filled with a mixture of (hereinafter referred to as anion exchange resin). On the other hand, it is widely practiced to prevent corrosion of pipes by adjusting the pH of circulating water.
Ammonia is injected into the circulating water for this purpose. The purpose of the condensate treatment equipment is to remove the impurities shown above, but due to its function, ammonium ions, which are not originally "impurities", are also
This results in a problem in that the desalting tower has to be regenerated more frequently because it becomes a load on the cation exchange resin.
即ち、再生頻度が高くなるということはそれだ
け高価な再生剤を多量に消費することになり不経
済なので、再生頻度を低く抑えるために本来アン
モニアブレークの時点で通水を停止して再生すべ
きところを、アンモニアブレーク以後も通水を続
けるいわゆる「アンモニアサイクル」方式が採用
されつつある。アンモニアサイクルは脱塩塔の再
生から次の再生までの通水継続時間が長くとれる
ので経済的ではあるが、アンモニアブレーク以後
の処理水質を良好に保つことが難しく、この問題
を解決することがアンモニアサイクル成否の鍵で
あると言つても過言ではない。これまでにも数々
の手段によつてこの問題の解決が図られてきた
が、それぞれ一長一短があり決定的有効な方法は
見い出されていない。 In other words, increasing the regeneration frequency means consuming a large amount of expensive regenerating agent, which is uneconomical, so in order to keep the regeneration frequency low, water flow should normally be stopped at the point of ammonia break for regeneration. The so-called "ammonia cycle" method, in which water continues to flow even after the ammonia break, is being adopted. The ammonia cycle is economical because it allows water to continue flowing for a long time from one regeneration to the next regeneration in the desalination tower, but it is difficult to maintain the quality of treated water after the ammonia break, and solving this problem requires ammonia It is no exaggeration to say that this is the key to the success or failure of the cycle. A number of methods have been used to solve this problem, but each has its own merits and demerits, and no definitively effective method has been found.
本来、混床式脱塩塔はＨサイクルで用いたとき
にその特長を発揮する。すなわちＨ形のカチオン
交換樹脂とOH形のアニオン交換樹脂の混合樹脂
層は、流入水の水質や樹脂相のイオン組成あるい
は再生後の水洗状況などによらず、良好な処理水
質を与えるというすぐれた性質をもつているが、
NH4形のカチオン交換樹脂とOH形のアニオン交
換樹脂の混合樹脂層にはこの性質はない。これは
流入水中の不純物イオンと樹脂相内イオンのイオ
ン交換反応生成物が、前者ではH2Oであり、後
者ではNH4OHであることによる。H2Oの解離定
数は非常に小さい（Kw＝10-14）ので、Ｈ／OH
混床塔におけるカチオン交換反応とアニオン交換
反応は不可逆的に進行するが、NH4OHの解離は
無視できない（Ｋ＝1.8×10-5）ので、NH4／OH
混床塔においては塔底部で逆反応を生じ、Na+イ
オンcl-、SO4 2-イオンを脱離する可能性がある。
したがつてアンモニアサイクルで用いる脱塩塔は
その出口部の樹脂中に不純物を含んでいてはなら
ないし、またアンモニアサイクルの場合は混床で
ある必要はないとも言える。 Originally, mixed bed demineralization towers exhibit their advantages when used in the H cycle. In other words, the mixed resin layer of an H-type cation exchange resin and an OH-type anion exchange resin has an excellent property of providing good treated water quality regardless of the quality of the inflow water, the ionic composition of the resin phase, or the washing conditions after regeneration. Although it has properties,
A mixed resin layer of an NH 4 type cation exchange resin and an OH type anion exchange resin does not have this property. This is because the ion exchange reaction products between impurity ions in the inflow water and ions in the resin phase are H 2 O in the former case and NH 4 OH in the latter case. Since the dissociation constant of H 2 O is very small (Kw=10 -14 ), H/OH
Although the cation exchange reaction and anion exchange reaction in the mixed bed column proceed irreversibly, the dissociation of NH 4 OH cannot be ignored (K = 1.8 × 10 -5 ), so NH 4 /OH
In a mixed bed column, a reverse reaction may occur at the bottom of the column, and Na + ions, cl - , and SO 4 2- ions may be desorbed.
Therefore, the demineralization tower used in the ammonia cycle must not contain impurities in the resin at its outlet, and in the case of the ammonia cycle, it is not necessary to have a mixed bed.
従来、アンモニアサイクルの最大の問題はアン
モニアブレーク以後に処理水中にナトリウムイオ
ンがリークすることであつた。このナトリウムリ
ークに対処する手段として従来法では再生時にカ
チオン交換樹脂とアニオン交換樹脂の分離をよく
してアニオン交換樹脂再生塔へ混入するカチオン
交換樹脂量を減らすことや、出じたNa形の樹脂
をアンモニア水や消石灰溶液のような薬品を用い
てNH4形やCa形に交換することが行われてきた。
しかしこのために再生に要する時間が長くなり、
また余分な薬品を使わなくてはならないという不
利があつた。
Traditionally, the biggest problem with ammonia cycles has been the leakage of sodium ions into the treated water after the ammonia break. As a means of dealing with this sodium leak, conventional methods include improving the separation of cation exchange resin and anion exchange resin during regeneration to reduce the amount of cation exchange resin mixed into the anion exchange resin regeneration tower, and reducing the amount of cation exchange resin that comes out of the anion exchange resin regeneration tower. It has been used to exchange NH4 and Ca forms using chemicals such as aqueous ammonia and slaked lime solution.
However, this increases the time required for playback,
Another disadvantage was that extra chemicals had to be used.
本発明は、これら従来の諸問題に関して抜本的
な解決手段を与えるものであり、従来の復水脱塩
方法の欠点を除去し、極めて高純度の処理水を安
定して得る方法を提供することを目的としたもの
である。 The present invention provides a drastic solution to these conventional problems, and provides a method for stably obtaining treated water of extremely high purity by eliminating the drawbacks of the conventional condensate desalination method. The purpose is to
また本発明の他の目的は復水脱塩処理のための
再生剤量を著しく低減させ運転維持管理を容易で
経済的にすることが可能な有効な復水処理方法と
することにある。 Another object of the present invention is to provide an effective condensate treatment method capable of significantly reducing the amount of regenerant for condensate desalination treatment and making operation and maintenance easy and economical.
本発明は、復水をイオン交換樹脂を充填した脱
塩塔によつて処理するに際し、脱塩塔として２塔
以上用い通水の下流側から強酸性カチオン交換樹
脂層（以下第２カチオン層とする）、強塩基性ア
ニオン交換樹脂層（以下アニオン層とする）、強
酸性カチオン交換樹脂層（以下第１カチオン層と
する）の順に配置できるように第１カチオン層を
充填された第１脱塩塔と上層にアニオン層、下層
に第２カチオン層を充填された第２脱塩塔とを配
備し、第１脱塩塔、第２脱塩塔の順に復水を流入
させて各層に順次直列に通水して処理水を流出さ
せることとし、このとき３つの樹脂層に用いる樹
脂は前記通水工程終了後の全樹脂を再生塔に移送
して逆洗分離したときに、下層のカチオン交換樹
脂のうち下部に位置する樹脂すなわち上下両樹脂
層の界面から離れた部分の樹脂を酸による再生後
に脱塩塔内の第２カチオン層として用い、また上
層のアニオン交換樹脂をアルカリによる再生後に
アニオン層として用いて、残つたカチオン交換樹
脂を酸による再生後に第１カチオン層として用
い、通水および再生をくりかえすことにより復水
を脱塩処理することを特徴とする復水処理方法で
ある。この際、アンモニアサイクルによる運転を
前提としているので、前記第２カチオン層、アニ
オン層は再生後の通水開始時点で不純物イオンを
含有していてはならない。しかし、アニオン層に
Na形のカチオン交換樹脂が混入することはさし
つかえない。 When treating condensate with a demineralization tower filled with ion exchange resin, the present invention uses two or more towers as the demineralization tower and starts from a strongly acidic cation exchange resin layer (hereinafter referred to as the second cation layer) from the downstream side of the flowing water. ), a strongly basic anion exchange resin layer (hereinafter referred to as the anion layer), and a strongly acidic cation exchange resin layer (hereinafter referred to as the first cation layer) are arranged in this order. A salt tower and a second demineralization tower filled with an anion layer in the upper layer and a second cation layer in the lower layer are installed, and condensate is introduced into the first demineralization tower and then the second demineralization tower in order to sequentially enter each layer. Water is passed in series to drain the treated water, and at this time, the resin used for the three resin layers is removed from the cations in the lower layer when all the resin after the water passing process is transferred to the regeneration tower and backwashed and separated. The lower part of the exchange resin, that is, the part of the resin away from the interface between the upper and lower resin layers, is used as the second cation layer in the demineralization tower after being regenerated with acid, and the anion exchange resin in the upper layer is used as the second cation layer in the demineralization tower after being regenerated with alkali. This is a condensate treatment method characterized in that the remaining cation exchange resin is used as an anion layer, the remaining cation exchange resin is used as a first cation layer after regeneration with an acid, and condensate is desalinated by repeating water passage and regeneration. At this time, since operation is based on an ammonia cycle, the second cation layer and anion layer must not contain impurity ions at the time of starting water flow after regeneration. However, in the anion layer
Contamination with Na-type cation exchange resin is not a problem.
本発明の実施態様を図面を参照して説明する
と、第１図に示す例では脱塩工程を二塔の脱塩塔
１，１′を用いて行うもので、この場合第１塔１
は第１カチオン層ａを設け、第２塔１′には上層
より順にアニオン層ｂ、第２カチオン層ｃを設け
たものの２塔を直列にしたものに通水して処理す
るもので、この場合、脱塩工程では第１カチオン
ａのみを逆洗およびスクラビングすることが可能
であり、特にボイラ起動時など懸濁粒子の多い水
を処理するのに適している。 An embodiment of the present invention will be described with reference to the drawings. In the example shown in FIG.
The first cation layer a is provided, and the second column 1' is provided with an anion layer b and a second cation layer c in order from the upper layer, and water is passed through the two columns connected in series for treatment. In this case, it is possible to backwash and scrub only the first cation a in the desalination step, and it is particularly suitable for treating water with many suspended particles, such as when starting a boiler.
即ち、復水２を第１塔１の塔頂部より流入さ
せ、下向流で通水し、第２塔１′を経て第２塔
１′の塔底部から処理水３を流出させるものであ
る。この場合、樹脂の再生は次のようにして行
う。まず通水工程を終了した全樹脂を第２図に示
すような再生塔に移送する。続いて逆洗分離を行
いカチオン交換樹脂とアニオン交換樹脂を分離す
る。ここで下層のカチオン交換樹脂層のうち上下
両樹脂層の界面から離れた下部の樹脂はほとんど
アニオン交換樹脂を含まない純粋なカチオン交換
樹脂であり、これを酸によつて再生したのち第２
塔１′の第２カチオン層ｃとして用いる。上層の
アニオン交換樹脂をアルカリによつて再生したの
ち第２塔１′内のアニオン層ｂとして用いる。残
りのカチオン交換樹脂は、酸で再生したのち、前
記第１塔１′内の第１カチオン層ａとして用いる。 That is, the condensate 2 is introduced from the top of the first column 1, passed through in a downward flow, and the treated water 3 is discharged from the bottom of the second column 1' via the second column 1'. . In this case, the resin is recycled as follows. First, all the resin that has undergone the water passage process is transferred to a regeneration tower as shown in FIG. Subsequently, backwash separation is performed to separate the cation exchange resin and the anion exchange resin. Here, the resin in the lower part of the lower cation exchange resin layer away from the interface between the upper and lower resin layers is pure cation exchange resin containing almost no anion exchange resin, and after being regenerated with acid, the second
It is used as the second cation layer c of column 1'. After the anion exchange resin in the upper layer is regenerated with an alkali, it is used as the anion layer b in the second column 1'. The remaining cation exchange resin is used as the first cation layer a in the first column 1' after being regenerated with an acid.
なお樹脂の再生には次のような方法を用いると
再生塔一塔だけで再生ができ非常に効率的であ
る。すなわち、第２図例の再生塔４に移送された
全樹脂を逆洗分離したのち、塔底部から酸を上向
流で通液し、塔頂部からアルカリを下向流で通液
し、カチオン交換樹脂層とアニオン交換樹脂層の
界面付近に設けられた集水機構５から排出するこ
とにより、両樹脂を同時に再生するのである。再
生後、各脱塩塔１，１′に樹脂を移送すればよい。
ただし、この場合、集水機構５は上下両樹脂層界
面より下側のカチオン交換樹脂層ａ内に設け、ア
ニオン交換樹脂が酸と接触しないようにする必要
がある。 It should be noted that if the following method is used to regenerate the resin, it can be regenerated with only one regeneration tower and is very efficient. That is, after backwashing and separating all the resins transferred to the regeneration tower 4 in the example in Figure 2, acid is passed in an upward flow from the bottom of the tower, alkali is passed in a downward flow from the top of the tower, and cations are removed. Both resins are simultaneously regenerated by discharging the water from a water collecting mechanism 5 provided near the interface between the exchange resin layer and the anion exchange resin layer. After regeneration, the resin may be transferred to each demineralization tower 1, 1'.
However, in this case, the water collecting mechanism 5 must be provided in the cation exchange resin layer a below the interface between the upper and lower resin layers to prevent the anion exchange resin from coming into contact with the acid.
図中６はアルカリ供給管、７は上部デイストリ
ビユータ、８は酸供給管、９は逆洗水供給管、１
０は下部デイストリビユータ、１１は逆洗廃水流
出管である。 In the figure, 6 is an alkali supply pipe, 7 is an upper distributor, 8 is an acid supply pipe, 9 is a backwash water supply pipe, 1
0 is a lower distributor, and 11 is a backwash wastewater outflow pipe.
本発明方法によれば、アンモニアサイクルで用
いるため樹脂の再生頻度を低く抑えることができ
て経済的であり、しかも第２カチオンに不純物を
ほとんど含まずアニオン層中のNa形樹脂からリ
ークするNa+イオンは第２カチオン層で捕捉され
るため、処理水中の不純物リークを著しく低くす
ることができ、さらに第１カチオン層或いは第２
カチオン層のみを別個に再生することが可能であ
つて、しかも第１カチオン層を空気でスクラビン
グする以外、空気を用いないので樹脂粒の破砕が
かなりの程度抑えられることになるし、また第１
段に分けてカチオン交換樹脂層をおいているため
に後段のアニオン交換樹脂の重金属による汚染を
防止できる。即ち、カチオン交換樹脂は重金属
（水）酸化物の微細懸濁粒子を効率よく捕捉する
性質をもつており、この性質は特に再生後のＨ形
樹脂で著しいが、NH4形の樹脂でもかなりの程
度捕捉するので、後段のアニオン交換樹脂の重金
属汚染がかなり防げることとなるし、従来の復水
処理システムで生じた諸問題点を適確に解決し、
運転維持管理も容易で質的にも良好で経済的な処
理水を得ることができるものである。 According to the method of the present invention, since it is used in an ammonia cycle, the regeneration frequency of the resin can be kept low, making it economical.Moreover, the second cation contains almost no impurities, and Na + leaks from the Na type resin in the anion layer. Since ions are captured in the second cation layer, the leakage of impurities into the treated water can be significantly reduced.
It is possible to regenerate only the cation layer separately, and since no air is used other than scrubbing the first cation layer with air, the crushing of resin particles can be suppressed to a considerable extent.
Since the cation exchange resin layer is placed in separate stages, it is possible to prevent the anion exchange resin in the latter stage from being contaminated by heavy metals. In other words, cation exchange resins have the property of efficiently trapping fine suspended particles of heavy metal (hydr)oxides, and this property is particularly remarkable in H-form resins after regeneration, but even in NH4- form resins, they can trap quite a lot of suspended particles. Since the condensate treatment system captures a large amount of water, heavy metal contamination of the anion exchange resin in the subsequent stage can be significantly prevented, and various problems that have arisen with conventional condensate treatment systems can be appropriately resolved.
It is easy to operate and maintain, and it is possible to obtain treated water that is of good quality and is economical.
図面は、本発明の実施例を示し、第１図は系統
説明図、第２図は本発明の実施に用いられる再生
塔の縦断面図である。
ａ……第１カチオン層、ｂ……アニオン層、ｃ
……第２カチオン層、１，１′，１″……脱塩塔、
２……復水、３……処理水、４……再生塔、５…
…集水機構。
The drawings show an embodiment of the present invention, with FIG. 1 being an explanatory diagram of the system, and FIG. 2 being a longitudinal cross-sectional view of a regeneration tower used in carrying out the present invention. a...first cation layer, b...anion layer, c
...Second cation layer, 1,1',1''...Demineralization tower,
2... Condensate, 3... Treated water, 4... Regeneration tower, 5...
...Water collection mechanism.
Claims (1)
つて処理するに際し、脱塩塔として２塔以上用い
通水の下流側から強酸性カチオン交換樹脂層（以
下第２カチオン層とする）、強塩基性アニオン交
換樹脂層（以下アニオン層とする）、強酸性カチ
オン交換樹脂層（以下第１カチオン層とする）の
順に配置できるように第１カチオン層を充填され
た第１脱塩塔と上層にアニオン層、下層に第２カ
チオン層を充填された第２脱塩塔とを配備し、第
１脱塩塔、第２脱塩塔の順に復水を流入させて各
層に順次直列に通水して処理水を流出させること
とし、このとき３つの樹脂層に用いる樹脂は前記
通水工程終了後の全樹脂を再生塔に移送して逆洗
分離したときに、下層のカチオン交換樹脂のうち
下部に位置する樹脂すなわち上下両樹脂層の界面
から離れた部分の樹脂を酸による再生後に脱塩塔
内の第２カチオン層として用い、また上層のアニ
オン交換樹脂をアルカリによる再生後にアニオン
層として用い、残つたカチオン交換樹脂を酸によ
る再生後に第１カチオン層として用いて、通水お
よび再生をくりかえすことにより復水を脱塩処理
することを特徴とする復水処理方法。 ２ 前記脱塩工程がアンモニアサイクルで運転す
るものである特許請求の範囲第１項記載の復水処
理方法。 ３ 前記再生工程が、脱塩塔への通水工程終了後
に脱塩塔内の全樹脂を一旦再生塔に移送して逆洗
分離を行つたのち、再生塔頂部のデイストリビユ
ータよりアルカリを下向流で流し、再生塔底部の
デイストリビユータより酸を上向流で流し、上下
両樹脂層の界面よりやや下部のカチオン交換樹脂
層内に設けた集水機構より排出させて処理される
ものである特許請求の範囲第１項又は第２項記載
の復水処理方法。 ４ 前記脱塩工程が、第１カチオン層だけの逆流
およびスクラビングも行うものである特許請求の
範囲第１〜３項のいずれか一つの項記載の復水処
理方法。[Claims] 1. When condensate is treated with a demineralization tower filled with an ion exchange resin, two or more towers are used as the demineralization tower, and a strongly acidic cation exchange resin layer (hereinafter referred to as the second The first cation layer was filled so that the first cation exchange resin layer (hereinafter referred to as the cation layer), the strongly basic anion exchange resin layer (hereinafter referred to as the anion layer), and the strongly acidic cation exchange resin layer (hereinafter referred to as the first cation layer) could be arranged in this order. A first demineralization tower and a second demineralization tower filled with an anion layer in the upper layer and a second cation layer in the lower layer are provided, and condensate is introduced into the first demineralization tower and the second demineralization tower in this order. Water is passed through each layer sequentially in series to drain the treated water, and at this time, the resin used for the three resin layers is obtained by transferring all the resin after the water passing step to a regeneration tower and backwashing and separating it. Of the cation exchange resin in the lower layer, the lower resin, that is, the resin in the part away from the interface between the upper and lower resin layers, is used as the second cation layer in the demineralization tower after being regenerated with acid, and the anion exchange resin in the upper layer is used as the second cation layer in the demineralization tower. A condensate treatment method characterized in that the remaining cation exchange resin is used as an anion layer after regeneration by acid, and the remaining cation exchange resin is used as a first cation layer after regeneration by acid, and the condensate is desalinated by repeating water passage and regeneration. . 2. The condensate treatment method according to claim 1, wherein the desalination step is operated using an ammonia cycle. 3. In the regeneration process, after the completion of the water flow process to the demineralization tower, all the resin in the demineralization tower is once transferred to the regeneration tower and backwashed and separated, and then the alkali is removed from the distributor at the top of the regeneration tower. The acid is flowed in a countercurrent flow, and the acid is flowed in an upward flow from a distributor at the bottom of the regeneration tower, and is discharged through a water collection mechanism installed in the cation exchange resin layer slightly below the interface between the upper and lower resin layers. A condensate treatment method according to claim 1 or 2. 4. The condensate treatment method according to any one of claims 1 to 3, wherein the desalting step also performs backflow and scrubbing of only the first cation layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21944086A JPS6265785A (en) | 1986-09-19 | 1986-09-19 | Treatment of condensate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21944086A JPS6265785A (en) | 1986-09-19 | 1986-09-19 | Treatment of condensate |
Related Parent Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10166378A Division JPS5528734A (en) | 1978-08-21 | 1978-08-21 | Condensed water treating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6265785A JPS6265785A (en) | 1987-03-25 |
| JPH0133227B2 true JPH0133227B2 (en) | 1989-07-12 |
Family
ID=16735440
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21944086A Granted JPS6265785A (en) | 1986-09-19 | 1986-09-19 | Treatment of condensate |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6265785A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH047080A (en) * | 1990-04-24 | 1992-01-10 | Ebara Infilco Co Ltd | Method for regenerating condensed water desalting apparatus |
| JP2002143845A (en) * | 2000-11-10 | 2002-05-21 | Japan Organo Co Ltd | Ion exchange device |
| CN102225813B (en) * | 2011-04-13 | 2013-03-13 | 中国石油化工股份有限公司 | Multi-stage fluidized ion exchange desalination method for recycling biochemical tail water as circulating cooling water |
-
1986
- 1986-09-19 JP JP21944086A patent/JPS6265785A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6265785A (en) | 1987-03-25 |
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