JPH0530504B2 - - Google Patents
Info
- Publication number
- JPH0530504B2 JPH0530504B2 JP25329885A JP25329885A JPH0530504B2 JP H0530504 B2 JPH0530504 B2 JP H0530504B2 JP 25329885 A JP25329885 A JP 25329885A JP 25329885 A JP25329885 A JP 25329885A JP H0530504 B2 JPH0530504 B2 JP H0530504B2
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- ion exchange
- resin
- organic substances
- eluted
- 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 - Lifetime
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 46
- 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 43
- 239000003456 ion exchange resin Substances 0.000 claims description 35
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 35
- 239000000126 substance Substances 0.000 claims description 34
- 239000011347 resin Substances 0.000 claims description 24
- 229920005989 resin Polymers 0.000 claims description 24
- 238000010612 desalination reaction Methods 0.000 claims description 17
- 239000003957 anion exchange resin Substances 0.000 claims description 16
- 239000003729 cation exchange resin Substances 0.000 claims description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- 238000001179 sorption measurement Methods 0.000 claims description 10
- 238000003860 storage Methods 0.000 claims description 8
- 150000001450 anions Chemical class 0.000 claims description 6
- 150000001768 cations Chemical class 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 5
- 238000000034 method Methods 0.000 claims description 5
- 238000001223 reverse osmosis Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000006227 byproduct Substances 0.000 claims description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims 3
- GETQZCLCWQTVFV-UHFFFAOYSA-N trimethylamine Chemical compound CN(C)C GETQZCLCWQTVFV-UHFFFAOYSA-N 0.000 claims 2
- USSHTWOXWQEPPI-UHFFFAOYSA-N 6-sulfonylcyclohexa-2,4-diene-1-carboxylic acid Chemical compound OC(=O)C1C=CC=CC1=S(=O)=O USSHTWOXWQEPPI-UHFFFAOYSA-N 0.000 claims 1
- SRSXLGNVWSONIS-UHFFFAOYSA-N benzenesulfonic acid Chemical compound OS(=O)(=O)C1=CC=CC=C1 SRSXLGNVWSONIS-UHFFFAOYSA-N 0.000 claims 1
- 229940092714 benzenesulfonic acid Drugs 0.000 claims 1
- 238000004140 cleaning Methods 0.000 description 12
- 238000005115 demineralization Methods 0.000 description 9
- 230000002328 demineralizing effect Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 8
- 238000005070 sampling Methods 0.000 description 8
- 239000005416 organic matter Substances 0.000 description 7
- 238000005406 washing Methods 0.000 description 7
- 230000008929 regeneration Effects 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 101150050055 LCP3 gene Proteins 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229920001577 copolymer Polymers 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 125000000524 functional group Chemical group 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002901 radioactive waste Substances 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
Landscapes
- Treatment Of Liquids With Adsorbents In General (AREA)
Description
［産業上の利用分野］
本発明はイオン交換樹脂からの溶出物の除去方
法に関する。即ち混床式脱塩装置において採水運
転に供されるまでの保管期間（待機期間）中の新
品のアニオン交換樹脂とカチオン交換樹脂又は再
生が完了したアニオン交換樹脂とカチオン交換樹
脂を混合し、純水又は復水等の洗浄水を循環しな
がら、イオン交換樹脂から溶出した物質（主に有
機物）を吸着装置及びイオン交換樹脂自身に再吸
着させて採水運転時の溶出物の純水又は復水中へ
の漏洩を防ぐことを目的としている。
［従来の技術］
イオン交換樹脂は主にスチレンとDVBの共重
合体に官能基を付与したものであり、その製造過
程において未反応物や副生物等の有機物を含んで
おり各工程において充分に洗浄を行なつている
が、製品保管中に樹脂内部より浸出してくる。
このイオン交換樹脂より溶出してくる有機物の
特定及びその分析法について、カチオン交換樹脂
からの溶出物については第１表に、アニオン交換
樹脂からの溶出物については第２表に示す。
[Industrial Application Field] The present invention relates to a method for removing eluates from ion exchange resins. That is, mixing a new anion exchange resin and a cation exchange resin during a storage period (standby period) before being used for water sampling operation in a mixed bed desalination device, or an anion exchange resin and a cation exchange resin that have been regenerated, While circulating cleaning water such as pure water or condensate, the substances (mainly organic substances) eluted from the ion exchange resin are re-adsorbed onto the adsorption device and the ion exchange resin itself, and the eluted water during the water sampling operation is purified with pure water or The purpose is to prevent leakage into condensate. [Prior art] Ion exchange resin is mainly made by adding functional groups to a copolymer of styrene and DVB, and contains organic substances such as unreacted substances and by-products during the manufacturing process. Although cleaning is being carried out, the resin leaches out from inside the product while it is being stored. Regarding the identification and analysis of organic substances eluted from this ion exchange resin, the eluted substances from the cation exchange resin are shown in Table 1, and the eluted substances from the anion exchange resin are shown in Table 2.
【表】【table】
【表】
この溶出物のために、特にBWR型原子力発電
所における復水脱塩装置においては次のような運
転をしていた。
(1) イオン交換樹脂充填時にカチオン交換樹脂、
アニオン交換樹脂を夫々カチオン樹脂再生塔、
アニオン樹脂再生塔にホツパーより水を使用し
充填する。
(2) 充填したイオン交換樹脂は夫々の再生搭で空
気撹拌（スクラツビング）、逆洗により溶出物
を洗浄し、樹脂槽に移送し、アニオン樹脂、カ
チオン樹脂を混合し最終洗浄を行なう。最終洗
浄の終点は導電率により、1μs／cm以下である
ことを確認する。
(3) 最終洗浄後の樹脂は脱塩塔に移送し保管す
る。
(4) 保管後約１時間程度の再循環運転を行ない、
導電率が0.1μs／cm以下になつた時点で採水運
転を開始する。
［発明が解決しようとする問題点］
上記の運転においては次のような理由により脱
塩塔よりイオン交換樹脂の溶出物が漏洩する可能
性がある。
(1) 最終洗浄によりある程度のイオン交換樹脂の
溶出物は除去出来るが、保管中に樹脂内部より
浸出してくる有機性溶出物が多量にある。
(2) 採水運転前の再循環操作は時間が短く（１時
間程度）、溶出物を充分に除去出来ない。
(3) 再循環操作は脱塩塔を通過した水を入口ヘツ
ダーに戻すため樹脂よりの溶出物は他の脱塩塔
を通過して下流へ通過する。
第３図はこの再循環操作を示す。１は復水管
入口、２は復水管出口、Ａ，Ｂ，Ｃは通水塔、
Ｄは停止塔、８は再循環ラインである。
(4) 原子力発電所において、主に使用されている
洗浄水は復水であり、放射性廃棄物処理設備に
て処理し再使用に供されるため、有機物を含ん
でいる可能性がある。
イオン交換樹脂より溶出してくる有機物は、
樹脂から溶出してくる時点では主に非導電性物
質であり、導電率では管理できず、原子炉にお
けるγ線、中性子等の照射又は熱により分解し
導電性物質に変化し原子炉の導電率を上昇させ
る危険性がある。
又イオン交換樹脂の洗浄を充分に行なうため
には、多量の純水（有機物の少ない水）が必要
であり、原子力発電所のランニングコストの上
昇につながる。
本発明はこれらの問題の原因となる、イオン
交換樹脂からの溶出有機物質の漏洩を防止せん
とするにある。
［問題点を解決するための手段］
本発明はイオン交換樹脂からの有機溶出物を除
去するための方法であり、従来の新品のアニオン
交換樹脂とカチオン交換樹脂または再生が完了し
たアニオン交換樹脂とカチオン交換樹脂が運転に
供給されるまでの保管期間（待機期間）を利用
し、カチオン交換樹脂とアニオン交換樹脂を混合
してその洗浄水による循環路中に活性炭フイルタ
ー、プリコート式フイルター又は逆浸透膜装置等
の吸着装置を設け、純水又は復水を循環しなが
ら、イオン交換樹脂を洗浄し、フイルターで除去
しきれなかつた有機物の中カチオン樹脂から溶出
してくるものをアニオン樹脂に、アニオン樹脂か
ら溶出してくるものをカチオン樹脂自身に夫々吸
着させ有機物をフイルター並びにイオン交換樹脂
に固定化し、採水時に純水又は復水中への有機物
の漏洩を防止する。
また、カチオン交換樹脂とアニオン交換樹脂を
個別にして、その洗浄水による循環路中に活性炭
フイルター、プリコート式フイルター又は逆浸透
膜装置等の吸着装置を設け、有機物をフイルター
に固定化することも採水時に純水又は復水中への
有機物の漏洩防止に有効である。
［作用］
イオン交換樹脂製造時、イオン交換樹脂内部に
存在する有機物質（未反応成分等）は有機物質が
イオン交換樹脂の表面に浸出してくるまでの時間
が長いため従来の方法において洗浄水量を増加し
ても効果がなく、長時間にわたり洗浄を続ける必
要がある。
本発明では新樹脂充填後、採水運転に供される
まで、通常イオン交換樹脂が再生搭、樹脂貯槽あ
るいは脱塩塔の予備塔内に保管されていることを
利用し、この保管期間に循環洗浄を行なうもので
あり、即ち充填を完了したアニオン交換樹脂とカ
チオン交換樹脂を混合した状態で、樹脂貯槽また
は脱塩塔の予備塔内に保管し、洗浄水の循環路に
活性炭フイルター、プリコート式フイルター又は
逆浸透膜等の吸着装置をもうけ、純水又は復水を
循環しながら洗浄する。
通水方法はダウンブローでSV＝５以上がよい。
洗浄時間は長時間ほど有効であり、通常２日以上
循環洗浄を続けることが望ましい。洗浄水を循環
する間にアニオン交換樹脂内部に残留していた有
機物、あるいはカチオン交換樹脂内部に残留して
いた有機物は洗浄水中に浸出し、吸着装置で吸着
されると共に吸着されなかつた有機物質は、アニ
オン交換樹脂とカチオン交換樹脂が混合してある
ため、洗浄水中に浸出した夫々の有機物は反対と
なるイオン交換樹脂に吸着され洗浄水中に浸出し
た有機物をイオン交換樹脂中に吸着除去すること
ができる。また、カチオン交換樹脂とアニオン交
換樹脂を個別に再生塔に保管し、洗浄水の循環路
に活性炭フイルター、プリコート式フイルター又
は逆浸透膜等の吸着装置を設け、イオン交換樹脂
より浸出してくる有機物を吸着除去することもで
きる。
以下に本発明の実施例を図にしたがつて説明す
ると、図は塔外再生方式の混床式復水脱塩装置の
系統図である。
実施例 １
第１図は、BWR型原子力発電所の復水脱塩装
置で全塔新樹脂でスタートアツプの例である。脱
塩塔は、塔径Φ3400mm、充填するイオン交換樹脂
量、カチオン4320、アニオン4800であり、運
転流量は1000m3／ｈであり、この脱塩塔８塔によ
り一次系の復水を全量処理する。脱塩塔内イオン
交換樹脂が全て新樹脂であるため、通水運転前に
LCP3−フイルタ４−脱塩塔７−HW6
（低圧復水ポンプ） （復水器水室）
の循環ループを構成させSV＝10以上（300m3／
Ｈ／塔）で全塔循環運転を行ない系統内の有機物
を復水器水室、低圧復水ポンプ、フイルタ、脱塩
塔の循環ループにおいて、フイルタ及びイオン交
換樹脂に吸着させる。
十分に有機物が吸着除去された後、採水運転に
入れる。
この場合フイルタは粉末イオン交換樹脂をプリ
コートするプリコートタイプのフイルタであり、
塔径Φ1650mm、過面積91m2、プリコート材使用
料は粉末カチオン交換樹脂68Kg−DRY、粉末ア
ニオン交換樹脂23Kg−DRYであり、運転流量は
700m3／ｈである。この過器は10等あり、必要
に応じて運転等数を変える。
実施例 ２
第２図は、BWR型原子力発電所の復水脱塩装
置で一塔ずつ新樹脂を充填し、採水に投入する場
合を示す。脱塩塔は、塔径Φ3400mm、充填するイ
オン交換樹脂量、カチオン4320、アニオン4800
であり、運転流量は、1000m3／ｈであり、この
脱塩塔８塔に一次系の復水を全量処理する。
各脱塩塔に専用の循環ラインを設置し新樹脂充
填、保管中の脱塩塔をSV＝10以上（250m3／ｈ）
以上で循環運転し、イオン交換樹脂からの有機物
をフイルタ及びイオン交換樹脂に吸着させる。
この場合のフイルタは粉末イオン交換樹脂をプ
リコートするプリコートタイプのフイルタであ
り、塔径Φ1000mm、過面積32m2、プリコート材
使用量は粉末カチオン交換樹脂24Kg−DRY、粉
末アニオン交換樹脂８Kg−DRYであり、運転流
量は250m3／ｈである。
循環ポンプは容量を大きくすることにより全塔
同時に循環運転に供することも可能と考えられ
る。
次に以上の実施例による脱塩塔出口のTOC濃
度の変化の測定結果を示す。[Table] Due to this eluate, condensate desalination equipment, especially in BWR nuclear power plants, was operated as follows. (1) When filling with ion exchange resin, cation exchange resin,
Anion exchange resin and cation resin regeneration tower, respectively
Fill the anion resin regeneration tower with water from the hopper. (2) The filled ion exchange resin is cleaned of eluates by air agitation (scrubbing) and backwashing in each regeneration tower, then transferred to a resin tank, where anion resin and cation resin are mixed for final cleaning. Confirm that the end point of the final cleaning is 1 μs/cm or less depending on the conductivity. (3) After the final cleaning, the resin is transferred to the demineralization tower and stored. (4) Perform recirculation operation for about 1 hour after storage,
Start water sampling operation when the conductivity becomes 0.1μs/cm or less. [Problems to be Solved by the Invention] In the above operation, there is a possibility that ion exchange resin eluate may leak from the desalting tower for the following reasons. (1) Although a certain amount of ion exchange resin eluates can be removed by final washing, a large amount of organic eluates leach from inside the resin during storage. (2) The recirculation operation before water sampling operation takes a short time (about 1 hour) and cannot sufficiently remove eluted substances. (3) In the recirculation operation, the water that has passed through the demineralization tower is returned to the inlet header, so the eluate from the resin passes through another demineralization tower and passes downstream. FIG. 3 illustrates this recirculation operation. 1 is the condensate pipe inlet, 2 is the condensate pipe outlet, A, B, C are the water towers,
D is a stop tower and 8 is a recirculation line. (4) The cleaning water mainly used at nuclear power plants is condensate, which may contain organic matter because it is treated in radioactive waste treatment equipment and reused. The organic substances eluted from the ion exchange resin are
When it is eluted from the resin, it is mainly a non-conductive substance, and cannot be controlled by conductivity; it decomposes into a conductive substance by irradiation with gamma rays, neutrons, etc. or heat in a nuclear reactor, and changes the reactor's conductivity. There is a risk of increasing the In addition, in order to sufficiently wash the ion exchange resin, a large amount of pure water (water with little organic matter) is required, which leads to an increase in the running cost of the nuclear power plant. The present invention aims to prevent the leakage of organic substances eluted from the ion exchange resin, which causes these problems. [Means for Solving the Problems] The present invention is a method for removing organic eluates from ion exchange resins, which uses a conventional new anion exchange resin and a cation exchange resin or a regenerated anion exchange resin. Utilizing the storage period (standby period) until the cation exchange resin is supplied for operation, mix the cation exchange resin and anion exchange resin and use an activated carbon filter, pre-coated filter, or reverse osmosis membrane in the circulation path of the cleaning water. An adsorption device such as a device is installed, and the ion exchange resin is washed while circulating pure water or condensed water. Among the organic substances that cannot be removed by the filter, those eluted from the cation resin are converted into anion resin. The organic substances eluted from the filter are adsorbed onto the cationic resin itself, and the organic substances are immobilized on the filter and ion exchange resin, thereby preventing leakage of organic substances into pure water or condensed water during water sampling. It is also possible to separate the cation exchange resin and anion exchange resin, and install an adsorption device such as an activated carbon filter, pre-coated filter, or reverse osmosis membrane device in the circulation path of the washing water, and fix the organic matter on the filter. Effective in preventing leakage of organic matter into pure water or condensed water. [Function] During the production of ion exchange resins, organic substances (unreacted components, etc.) existing inside the ion exchange resins are washed with less water than conventional methods because it takes a long time for the organic substances to leach onto the surface of the ion exchange resins. Even if the amount of water is increased, it is not effective and cleaning must be continued for a long time. The present invention takes advantage of the fact that ion exchange resin is normally stored in a regeneration tower, resin storage tank, or reserve tower of a desalination tower after filling with new resin until it is used for water sampling operation, and circulates during this storage period. In other words, the filled anion exchange resin and cation exchange resin are mixed together and stored in a resin storage tank or a preliminary tower of the desalination tower, and an activated carbon filter and pre-coated type are installed in the cleaning water circulation path. An adsorption device such as a filter or reverse osmosis membrane is installed, and cleaning is performed while circulating pure water or condensed water. The water flow method should be down blow and SV = 5 or higher.
The longer the cleaning time, the more effective it is, and it is usually desirable to continue circulating cleaning for two days or more. While the washing water is being circulated, the organic substances remaining inside the anion exchange resin or the organic substances remaining inside the cation exchange resin are leached into the washing water, and the organic substances that are not adsorbed are adsorbed by the adsorption device. Since an anion exchange resin and a cation exchange resin are mixed, each organic substance leached into the washing water is adsorbed by the opposite ion exchange resin, and the organic substances leached into the washing water can be adsorbed and removed by the ion exchange resin. can. In addition, the cation exchange resin and anion exchange resin are stored separately in a regeneration tower, and an adsorption device such as an activated carbon filter, pre-coated filter, or reverse osmosis membrane is installed in the circulation path of the washing water, and organic substances leached from the ion exchange resin are removed. can also be removed by adsorption. Embodiments of the present invention will be described below with reference to the drawings. The drawings are system diagrams of a mixed bed type condensate desalination apparatus using an outside column regeneration method. Example 1 Figure 1 is an example of starting up a condensate desalination equipment for a BWR type nuclear power plant using new resin for all towers. The demineralization tower has a diameter of 3400 mm, the amount of ion exchange resin packed is 4320 for cations, and 4800 for anions, and the operating flow rate is 1000 m 3 /h. The 8 demineralization towers treat the entire amount of condensate in the primary system. . Since the ion exchange resin in the demineralization tower is all new resin, a circulation loop of LCP3 - filter 4 - demineralization tower 7 - HW6 (low pressure condensate pump) (condenser water chamber) is configured before water flow operation. SV=10 or more ( 300m3 /
The organic matter in the system is adsorbed onto the filter and ion exchange resin in the circulation loop of the condenser water chamber, low-pressure condensate pump, filter, and desalination tower. After the organic matter has been sufficiently adsorbed and removed, water sampling operation begins. In this case, the filter is a pre-coated type filter that is pre-coated with powdered ion exchange resin.
The column diameter is Φ1650mm, the over area is 91m2 , the pre-coating materials used are powdered cation exchange resin 68Kg-DRY, powdered anion exchange resin 23Kg-DRY, and the operating flow rate is
700m 3 /h. There are 10 units of this filter, and the number of units to be operated can be changed as needed. Embodiment 2 Figure 2 shows a case in which new resin is filled one tower at a time in a condensate desalination equipment of a BWR type nuclear power plant and water is collected. The desalination tower has a tower diameter of Φ3400 mm, the amount of ion exchange resin packed, cation 4320, anion 4800.
The operating flow rate is 1000 m 3 /h, and all of the condensate in the primary system is treated in the eight demineralization towers. A dedicated circulation line is installed in each desalination tower, filled with new resin, and the stored desalination tower is SV=10 or more (250m 3 /h)
The circulation operation is performed as described above, and the organic matter from the ion exchange resin is adsorbed onto the filter and the ion exchange resin. The filter in this case is a pre-coated type filter that pre-coats powdered ion exchange resin, with a column diameter of Φ1000 mm, over area of 32 m 2 , and the amount of pre-coated materials used is 24 kg-DRY of powdered cation exchange resin and 8 kg-DRY of powdered anion exchange resin. , the operating flow rate is 250 m 3 /h. It is thought that by increasing the capacity of the circulation pump, it is possible to provide circulation operation to all columns at the same time. Next, the measurement results of changes in TOC concentration at the outlet of the demineralization tower according to the above examples will be shown.
【表】
［発明の効果］
本発明により混床式脱塩装置においてイオン交
換樹脂より溶出する有機物質が有効に効率良く除
去でき、採水運転時の溶出物の純水または復水中
への漏洩が防止できる。[Table] [Effects of the invention] According to the present invention, organic substances eluted from ion exchange resins can be effectively and efficiently removed in a mixed bed desalination equipment, and leakage of eluted substances into pure water or condensate during water sampling operation can be prevented. can be prevented.
第１図は本発明の塔外再生方式の混床式復水脱
塩装置の系統図で全塔新樹脂でスタートアツプの
場合を示す。第２図は本発明の塔外再生方式の混
床式復水脱塩装置の系統図で一塔づつ新樹脂を充
填し、採水に投入する場合を示す。第３図は従来
の混床式復水脱塩装置の再循環操作の系統図を示
す。
１……復水入口管、２……復水出口管、３……
低圧復水ポンプ（LPCP）、４……吸着装置（フ
イルタ）、５……高圧復水ポンプ（HPCP）、６…
…ホツトウエル（HW）、７……脱塩塔、８……
循環ライン、Ａ，Ｂ，Ｃは通水塔、Ｄは停止、
Ｘ，Ｙ，Ｚは夫々循環ラインを形成する箇所を示
す、Ｐはポンプ。
FIG. 1 is a system diagram of the mixed-bed condensate desalination apparatus of the present invention using the outside-column regeneration method, and shows the case where all the columns are started with new resin. FIG. 2 is a system diagram of a mixed-bed condensate desalination apparatus using an external regeneration method according to the present invention, and shows a case in which each tower is filled with new resin and water is collected. FIG. 3 shows a system diagram of the recirculation operation of a conventional mixed bed condensate desalination apparatus. 1... Condensate inlet pipe, 2... Condensate outlet pipe, 3...
Low pressure condensate pump (LPCP), 4...Adsorption device (filter), 5...High pressure condensate pump (HPCP), 6...
... Hotwell (HW), 7... Desalination tower, 8...
Circulation line, A, B, C are water towers, D is stopped,
X, Y, and Z indicate the locations where the circulation lines are formed, and P is the pump.
Claims (1)
するため、混床式脱塩装置においてカチオン交換
樹脂とアニオン交換樹脂を混合状態で貯槽に充填
し、純水又は復水を循環しながら、その循環路に
主として活性炭フイルター、プリコート式フイル
ター又は逆浸透膜の吸着装置を設け、吸着装置及
びイオン交換樹脂自身によりイオン交換樹脂より
の溶出有機物質を除去する方法。 ２ カチオン交換樹脂からの溶出有機物質が、ベ
ンゼンスルフオン酸、スルフオニール安息香酸を
主とするカチオン樹脂製造過程においての未反応
物質や副生物を含有するものである特許請求の範
囲第１項記載のイオン交換樹脂よりの溶出有機物
質を除去する方法。 ３ アニオン交換樹脂からの溶出有機物質が、メ
タノール、トリメチルアミンを主とするアニオン
樹脂製造過程においての未反応物質や副生物を含
有するものである特許請求の範囲第１項記載のイ
オン交換樹脂よりの溶出有機物質を除去する方
法。[Scope of Claims] 1. In order to remove organic substances eluted from ion exchange resins, in a mixed bed desalination device, a storage tank is filled with a cation exchange resin and an anion exchange resin in a mixed state, and pure water or condensed water is circulated. However, an adsorption device such as an activated carbon filter, a precoat filter, or a reverse osmosis membrane is installed in the circulation path, and organic substances eluted from the ion exchange resin are removed by the adsorption device and the ion exchange resin itself. 2. The organic substance eluted from the cation exchange resin contains unreacted substances and by-products in the cation resin manufacturing process mainly containing benzenesulfonic acid and sulfonylbenzoic acid. A method for removing organic substances eluted from ion exchange resins. 3. Organic substances eluted from the anion exchange resin contain unreacted substances and by-products in the anion resin manufacturing process mainly containing methanol and trimethylamine. Method for removing leached organic substances.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25329885A JPS62114662A (en) | 1985-11-12 | 1985-11-12 | Method for removing substance eluted from ion exchange resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25329885A JPS62114662A (en) | 1985-11-12 | 1985-11-12 | Method for removing substance eluted from ion exchange resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62114662A JPS62114662A (en) | 1987-05-26 |
| JPH0530504B2 true JPH0530504B2 (en) | 1993-05-10 |
Family
ID=17249339
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25329885A Granted JPS62114662A (en) | 1985-11-12 | 1985-11-12 | Method for removing substance eluted from ion exchange resin |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS62114662A (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP7648345B2 (en) * | 2020-06-05 | 2025-03-18 | オルガノ株式会社 | Pure water production method and production equipment |
-
1985
- 1985-11-12 JP JP25329885A patent/JPS62114662A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62114662A (en) | 1987-05-26 |
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