JPS6019041A - Backwash separation method for mixed resin - Google Patents
Backwash separation method for mixed resinInfo
- Publication number
- JPS6019041A JPS6019041A JP58125462A JP12546283A JPS6019041A JP S6019041 A JPS6019041 A JP S6019041A JP 58125462 A JP58125462 A JP 58125462A JP 12546283 A JP12546283 A JP 12546283A JP S6019041 A JPS6019041 A JP S6019041A
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- resin
- backwash
- anion exchange
- cation 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
- 239000011347 resin Substances 0.000 title claims description 48
- 229920005989 resin Polymers 0.000 title claims description 48
- 238000000926 separation method Methods 0.000 title description 53
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 64
- 239000003957 anion exchange resin Substances 0.000 claims description 55
- 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 51
- 239000003729 cation exchange resin Substances 0.000 claims description 48
- 238000005342 ion exchange Methods 0.000 claims description 24
- 230000002093 peripheral effect Effects 0.000 claims description 20
- 238000000034 method Methods 0.000 claims description 14
- 238000011001 backwashing Methods 0.000 claims description 9
- 239000003456 ion exchange resin Substances 0.000 description 11
- 229920003303 ion-exchange polymer Polymers 0.000 description 11
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 6
- 150000002500 ions Chemical class 0.000 description 6
- 229910001415 sodium ion Inorganic materials 0.000 description 6
- 238000007796 conventional method Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 5
- 239000011734 sodium Substances 0.000 description 5
- 230000001172 regenerating effect Effects 0.000 description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 238000010612 desalination reaction Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 101100441097 Dictyostelium discoideum crlG gene Proteins 0.000 description 1
- OKIZCWYLBDKLSU-UHFFFAOYSA-M N,N,N-Trimethylmethanaminium chloride Chemical compound [Cl-].C[N+](C)(C)C OKIZCWYLBDKLSU-UHFFFAOYSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940023913 cation exchange resins Drugs 0.000 description 1
- 229920001429 chelating resin Polymers 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011888 foil Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
本発明はカチオン交換樹脂とアニオン交換樹脂の混合樹
脂を逆洗分離する際の改良に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to improvements in backwashing and separating a mixed resin of a cation exchange resin and an anion exchange resin.
従来から工業用水等を原水とする純水製造装置あるいは
火力発電所、原子力発電所等の復水脱塩装置などにカチ
オン交換樹脂とアニオン交換樹脂の混合樹脂を用いる混
床式イオン交換装置が用いられている。当該混床式イオ
ン交換装置はカチオン交換樹脂とアニオン交換樹脂の混
合樹脂を用いて被処理水を処理するのであるから、処理
後に両イオン交換樹脂を再生するにあたり、当該混合樹
脂をカチオン交換樹脂とアニオン交換樹脂に分離する必
要がある。従来の分離方法は稀に力性ソーダ溶液などの
ような比重液を用いて分離する方法も採用されているが
２通常は以下のような水流による逆洗分離が行なわれて
いる。すなわちまず当該混合樹脂が充填されているイオ
ン交換塔の下部から、当該混合樹脂が約１００％膨張す
るような流速１通常Ｌｖ（線速度。Mixed-bed ion exchange equipment that uses a mixed resin of cation exchange resin and anion exchange resin has traditionally been used in pure water production equipment that uses industrial water as raw water or condensate desalination equipment in thermal power plants, nuclear power plants, etc. It is being The mixed bed type ion exchange equipment treats the water to be treated using a mixed resin of a cation exchange resin and an anion exchange resin, so when regenerating both ion exchange resins after treatment, the mixed resin is used as a cation exchange resin. It is necessary to separate the anion exchange resin. In the conventional separation method, a method of separation using a specific gravity liquid such as a strength soda solution has been adopted in rare cases; however, the following backwash separation using water flow is usually performed. That is, first, from the lower part of the ion exchange column filled with the mixed resin, the flow rate is 1 normal Lv (linear velocity) such that the mixed resin expands about 100%.
以下同様）７〜１２ ｍ ／ Ｈの逆洗水を流入して当
該混合樹脂を膨張流動させる。このように混合樹脂を膨
張流動させると上昇流水中における両イオン交換樹脂の
沈降速度に差が生じ。(Similarly below) 7 to 12 m/H of backwash water is flowed in to expand and flow the mixed resin. When the mixed resin is expanded and flowed in this way, a difference occurs in the settling speed of both ion exchange resins in the rising water.
比重の大きいカチオン交換樹脂が下部に、比重の小さい
アニオン交換樹脂が上部に集合し。Cation exchange resins with higher specific gravity gather at the bottom, and anion exchange resins with lower specific gravity gather at the top.
膨張状態にあるカチオン交換樹脂とアニオン交換樹脂の
二層が形成される。そしてこのような２層が形成された
後に、逆洗水の流入を止めると膨張状態にあるカチオン
交換樹脂とアニオン交換樹脂が水中を沈降し、下層がカ
チオン交換樹脂層、上層がアニオン交換樹脂層となった
分離層を形成することができる。Two layers of expanded cation exchange resin and anion exchange resin are formed. After such two layers are formed, when the inflow of backwash water is stopped, the expanded cation exchange resin and anion exchange resin settle in the water, and the lower layer is the cation exchange resin layer and the upper layer is the anion exchange resin layer. A separation layer can be formed.
このような逆洗分離を行なった後、二層を形成した−１
：ｔ、あるいはたとえば上層のアニオン交換樹脂を別浴
に取シ出してカチオン交換樹脂は酸で、アニオン交換樹
脂はアルカリで再生し、水洗を行なったｅ−１’Ｊ生済
みの両イオン交換樹脂を混合してふたたび通水に供して
いる。After performing such backwash separation, two layers were formed -1
:t, or e-1'J finished amphoteric ion exchange resin, for example, by taking out the upper layer anion exchange resin into a separate bath, regenerating the cation exchange resin with acid and the anion exchange resin with alkali, and washing with water. The mixture is mixed and subjected to water passage again.
ところで高純度の処理水が要求される電子工業用の純水
製造装置あるいは火力発電所や原子力発電所の復水脱塩
装置などの混床式イオン交換装置においても混合樹脂を
分離するにあたり、上述した水流による逆洗分離が実施
されているが、当該混床式イオン交換装置において、た
びたび純度上昇不良という問題が生じ、この原因を種々
検討した結果、以下に説明する従来の逆洗分離方法にお
ける分離不完全が大きな要因となっていることが判明し
た。By the way, when separating mixed resins in mixed bed ion exchange equipment such as pure water production equipment for the electronics industry that requires high purity treated water or condensate desalination equipment for thermal power plants and nuclear power plants, the above-mentioned method is necessary. However, in the mixed bed type ion exchange equipment, the problem of insufficient increase in purity frequently occurred.As a result of various investigations into the causes of this problem, we found that the conventional backwash separation method described below It was found that incomplete separation was a major factor.
すなわち従来の逆洗分離方法においては第１図に示した
ように混合樹脂１が充填されているイオン交換塔２の下
部から前述したごと＜ ＬＶ÷〜１２ｍ／Ｈの逆洗水３
を流入し、充填樹脂層高に対して約１００％のレベルＬ
まで混合樹脂を膨張流動させるが、当該逆洗により大部
分の混合樹脂は膨張流動するものの、支持板４の周縁部
５に存在する混合樹脂１′は膨張流動しないでそのまま
残留する。この混合樹脂１′中におけるアニオン交換樹
脂は全アニオン交換樹脂量の３〜５％に達することがあ
る。That is, in the conventional backwash separation method, as shown in FIG. 1, backwash water 3 of < LV ÷ ~ 12 m/H is collected from the bottom of the ion exchange tower 2 filled with the mixed resin 1 as described above.
flows in, and the level L is about 100% of the height of the filled resin layer.
Although most of the mixed resin expands and flows due to the backwashing, the mixed resin 1' existing on the peripheral edge 5 of the support plate 4 remains as it is without expanding and flowing. The anion exchange resin in this mixed resin 1' may amount to 3 to 5% of the total amount of anion exchange resin.
また逆洗水を流入して膨張状態にあるカチオン交換樹脂
とアニオン交換樹脂の二層を形成した後に逆洗水の流入
を止めて両イオン交換樹脂を沈降させると、第２図に示
したようにカチオン交換樹脂層６とアニオン交換樹脂層
７の分離面８が乱れる。たとえば分離面に付設されてい
る一方の覗き窓（図示せず）とその裏側に旧設されてい
る他方の覗き窓（図示せず）から分離面を観察すると２
両者の分離面のレベルに４０１１１１１１前後の差が生
じていることが確認された。In addition, if backwash water is flowed in to form two layers of expanded cation exchange resin and anion exchange resin, and then the flow of backwash water is stopped to allow both ion exchange resins to settle, as shown in Figure 2. The separation surface 8 between the cation exchange resin layer 6 and the anion exchange resin layer 7 is disturbed. For example, if you observe the separation surface from one viewing window (not shown) attached to the separation surface and the other viewing window (not shown) that was previously installed on the back side, you will see 2.
It was confirmed that there was a difference of around 40111111 in the level of the separation plane between the two.
支持板４の周縁部５に存在する混合樹脂１′がそのまま
残留するのは当該部分に水が流れにくいことに起因する
ものであ９５寸だ分離面８が乱れるのは逆洗水３の流速
が乱流域にあるため膨張流動する両イオン交換樹脂がた
とえばうす巻き状の乱流状態となり、逆洗水の流入を止
めて両イオン交換樹脂を沈降させる際に、この乱流状態
を保っだ捷ま沈降することに起因している。このように
支持板４の周縁部５に混合樹脂１′がそのま寸残留した
り。The reason why the mixed resin 1' remaining on the peripheral edge 5 of the support plate 4 is due to the fact that water is difficult to flow in that area.The separation surface 8 is disturbed due to the flow rate of the backwash water 3. Because the resin is in a turbulent region, the expanding and flowing ion exchange resin becomes, for example, a thinly coiled turbulent flow state. This is caused by sedimentation. In this way, the mixed resin 1' remains as it is on the peripheral edge 5 of the support plate 4.
あるいは分離面８が乱れると以下の再生において障害が
生じそのため処理水純度の上昇が不良となる。Alternatively, if the separation surface 8 is disturbed, problems occur in the subsequent regeneration, resulting in a poor increase in the purity of the treated water.
すなわち第２図においてカチオン交換樹脂層６を再生す
るために、たとえば塩酸９を通薬した際に混合樹脂１′
中のアニオン交換樹脂がＣ１形となる。また分離面８が
乱れているため分離面に内設されているコレクター（図
示せず）の下部にアニオン交換樹脂層７が。That is, in FIG. 2, in order to regenerate the cation exchange resin layer 6, for example, when hydrochloric acid 9 is passed through, the mixed resin 1'
The anion exchange resin inside is C1 type. Furthermore, since the separation surface 8 is disturbed, an anion exchange resin layer 7 is formed at the bottom of a collector (not shown) installed inside the separation surface.
ある因はコレクターの上部にカチオン交換樹脂層６が存
在するので、塩酸９を通薬した際にコレクターの下部に
存在するアニオン交換樹脂がＣ１形とな９３寸だアニオ
ン交換樹脂層７を再生するために力性ソーダ溶液１ｏを
通薬した際にコレクターの上部に存在するカチオン交換
樹脂がＮａ形となる。なお第２図に示したまうな一塔で
両イオン交換樹脂を再生せず２分離したカチオン交換樹
脂層６とアニオン交換樹脂層７を別塔に分け、別々に再
生する場合においてもカチオン交換樹脂層６中に混合樹
脂１′が混入することは同様であり。One reason is that the cation exchange resin layer 6 exists in the upper part of the collector, so when hydrochloric acid 9 is passed through it, the anion exchange resin present in the lower part of the collector becomes C1 type and regenerates the 93-dimensional anion exchange resin layer 7. Therefore, when the sodium hydroxide solution 1o is passed through the collector, the cation exchange resin present in the upper part of the collector becomes Na type. Note that even if both ion exchange resins are not regenerated in one tower as shown in Figure 2, but the separated cation exchange resin layer 6 and anion exchange resin layer 7 are separated into separate towers and regenerated separately, the cation exchange resin layer Similarly, mixed resin 1' is mixed in 6.
さらに分離面８が乱れているので両イオン交換樹脂層を
別塔に分ける際にカチオン交換樹脂層中にアニオン交換
・樹脂が、またアニオン交換樹脂層中にカチオン交換樹
脂が混入し。Furthermore, since the separation surface 8 is disturbed, when both ion exchange resin layers are separated into separate columns, the anion exchange resin mixes into the cation exchange resin layer, and the cation exchange resin mixes into the anion exchange resin layer.
したがってこれら混入したアニオン交換樹脂がＣ１形に
、カチオン交換樹脂がＮａ形になることは同様である。Therefore, the mixed anion exchange resin becomes the C1 type, and the cation exchange resin becomes the Na type.
仁のように再生後においてｃｌ形のアニオン交換樹脂あ
るいはＮａ形のカチオン交換樹脂が存在しているとそれ
だけ処理水の純度上昇が不良となり、特にＰＷＲ型原子
力発電所の復水脱塩装置においては処理水のＮａイオン
リーク、 ＣＩイオンリークの制限が厳しく。If Cl-type anion exchange resin or Na-type cation exchange resin is present after regeneration, the purity of the treated water will be poorer, especially in the condensate desalination equipment of PWR nuclear power plants. Strict restrictions on Na ion leak and CI ion leak from treated water.
したがって再生後におけるＣ］形のアニオン交換樹脂あ
るいはＮａ形のカチオン交換樹脂の混入量を出来るたけ
低減しなければならない。Therefore, the amount of C] type anion exchange resin or Na type cation exchange resin mixed in after regeneration must be reduced as much as possible.
本発明は前述したような従来の逆洗分離方法の欠点を解
決し、支持板の周縁部に混合樹脂を残留させず、かつ分
離面を乱さない逆洗分離方法を提供することを目的とす
るものであり、カチオン交換樹脂とアニオン交換樹脂の
混合樹脂が充填されているイオン交換塔の下部から逆洗
水を流入してカチオン交換樹脂とアニオン交換樹脂の膨
張層を形成し、その後に沈整することによりカチオン交
換樹脂とアニオン交換樹脂を分離するにあたり、イオン
交換塔の下部から気体およびまだはＬＶ １３ｍ ／
Ｈ以上の逆洗水を流入して、イオン交換塔の支持板周縁
部に存在する混合樹脂を当該周縁部から離脱させる工程
と、イオン交換塔の下部からＬＶ７〜１２ｍ／Ｈの逆洗
水を流入して、カチオン交換樹脂とアニオン交換樹脂の
膨張層を形成する工程と、すくなくとも逆洗水の流速を
Ｌｖ５ｍ／Ｈ以下に低下させて、当該膨張層を膨張状態
を維持しだま捷沈下させる工程と、逆洗水の流入を止め
て膨張状態にあるカチオン交換樹脂とアニオン交換樹脂
を沈整する工程とを順に行なうことを特徴とする混合樹
脂の逆洗分離方法に関するものである。The present invention solves the drawbacks of the conventional backwash separation method as described above, and aims to provide a backwash separation method that does not leave mixed resin on the peripheral edge of the support plate and does not disturb the separation surface. Backwash water is introduced from the bottom of the ion exchange tower filled with a mixed resin of cation exchange resin and anion exchange resin to form an expanded layer of cation exchange resin and anion exchange resin, and then settles. In separating the cation exchange resin and anion exchange resin by
A step in which backwash water of LV 7 to 12 m/H is introduced from the lower part of the ion exchange tower to separate the mixed resin present at the peripheral edge of the support plate of the ion exchange tower from the peripheral edge of the support plate of the ion exchange tower. A step of flowing in and forming an expanded layer of cation exchange resin and anion exchange resin, and a step of reducing the flow rate of backwash water to at least Lv5m/H or less to maintain the expanded state of the expanded layer and allowing it to sink. The present invention relates to a method for backwashing and separating a mixed resin, which comprises sequentially performing the following steps: and a step of stopping the flow of backwash water to settle the expanded cation exchange resin and anion exchange resin.
以下に本発明の詳細な説明する。The present invention will be explained in detail below.
従来の逆洗分離方法の第１の欠点は支持板の周縁部に混
合樹脂が残留することであり。The first drawback of the conventional backwash separation method is that the mixed resin remains on the peripheral edge of the support plate.
この原因は支持板周縁部の、水の流れが緩慢であるため
に当該部分の混合樹脂が膨張流動しないことによる。ま
た第２の欠点は分離面が乱れることであり、この原因は
乱流状態にある膨張樹脂をそのまま沈降させるところに
ある。本発明は基本的にはまず気体およびまたは通常の
逆洗流速より速い流速の逆洗水を流入して支持板周縁部
の混合樹脂を当該周縁部から離脱させ１次いで通常の逆
洗流速の逆洗水を流入してカチオン交換樹脂とアニオン
交換樹脂の膨張層を形成し２次いで通常の逆洗流速より
遅い流速の逆洗水を流入して乱流状態にある前記膨張層
を整え、その後に膨張層を沈整するという４工程を順に
行なって逆洗分離を行なうものである。This is because the flow of water around the peripheral edge of the support plate is slow, so that the mixed resin in that area does not expand and flow. The second drawback is that the separation surface is disturbed, and the cause of this is that the expanded resin in a turbulent state is allowed to settle as it is. Basically, the present invention first injects gas and/or backwash water at a flow rate higher than the normal backwash flow rate to separate the mixed resin from the peripheral edge of the support plate, and then reverse the normal backwash flow rate. Washing water is flowed in to form an expanded layer of cation exchange resin and anion exchange resin, and then backwash water is flowed in at a flow rate slower than the normal backwash flow rate to adjust the expanded layer in a turbulent flow state. Backwash separation is performed by sequentially performing four steps of settling the expanded layer.
以下に本発明の逆洗分離方法を工程ごとに゛図面を参照
して以下に説９Ｊする。The backwash separation method of the present invention will be explained step by step below with reference to the drawings.
まず第３図に示したごとく混合樹脂１が充填されている
イオン交換塔２の下部から気体たとえば空気１１４たは
高流速の逆洗水１２あるいは空気１１と高流速の逆洗水
１２を流入して支持板４の上部、特に支持板４の周縁部
に存在する混合樹脂１′を完全に離脱させる。この場合
空気１１の流入量としては、たとえばｌ・９ ｋｇ ／
ｃａ Ｇの圧力で充填樹脂量とほぼ同量の空気を約１
分間で流入する程度で充分である。First, as shown in FIG. 3, a gas such as air 114 or high-flow backwash water 12 or air 11 and high-flow backwash water 12 are introduced from the lower part of the ion exchange tower 2 filled with mixed resin 1. The mixed resin 1' existing on the upper part of the support plate 4, particularly at the peripheral edge of the support plate 4, is completely removed. In this case, the inflow amount of the air 11 is, for example, l·9 kg/
At a pressure of ca G, approximately the same amount of air as the amount of filled resin is
It is sufficient for the amount to flow within minutes.
また当該逆洗水１２の流入量はすくなくともＬＶ１３ｍ
／Ｈ以上とし、好ましくは２０ｍｐＨ前後とするとよい
。なお空気１１あるいは箔該逆洗水１２をそれぞれ単独
で流入しても支持板４の周縁部に存在する混合樹脂を完
全に離脱させることができるが、空気１１と当該逆洗水
１２を同時に流入した方がより効果的である。In addition, the inflow amount of the backwash water 12 is at least LV13m.
/H or higher, preferably around 20 mpH. Note that even if the air 11 or the foil backwash water 12 flows in separately, the mixed resin present at the peripheral edge of the support plate 4 can be completely removed, but it is not possible to completely remove the mixed resin existing at the peripheral edge of the support plate 4. It is more effective to do so.
また本工程の目的は支持板４の周縁部にある混合樹脂１
′を離脱するところにあるので、空気１１およびまたは
当該逆洗水１２の流入時間をあまり長くする必要が々く
、たとえば２分以下の単時間で充分であり２通常は１分
前後とする。なおこの工程の時間をあまり長くするとイ
オン交換塔２の上部に付設した逆洗水排出管（図示せず
）にネットなどを巻いてない場合は、ここから混合樹脂
が流出するので好ましくない。Also, the purpose of this process is to remove the mixed resin 1 on the peripheral edge of the support plate 4
', it is not necessary to make the inflow time of the air 11 and/or the backwash water 12 too long; for example, a single time of 2 minutes or less is sufficient, and usually it is around 1 minute. Note that if the time for this step is too long, the mixed resin will flow out from the backwash water discharge pipe (not shown) provided at the top of the ion exchange tower 2 unless a net or the like is wrapped around it, which is not preferable.
このように支持板４の周縁部に存在する混合樹脂１′を
当該周縁部から離脱させた直後に。Immediately after the mixed resin 1' existing on the peripheral edge of the support plate 4 is separated from the peripheral edge in this way.
第４図に示したごとくイオン交換塔２の下部から通常の
逆洗流速、すなわち充填樹脂層高に対して約１００％樹
脂層高が膨張するような流速であるＬＶ７〜１２ ｎｔ
／ Ｈの逆洗水３を流入して混合樹脂を分離し、膨張
状態にあるカチオン交換樹脂層６′とアニオン交換樹脂
層７′を形成させる。なお当該逆洗水３の流入時間はカ
チオン交換樹゛脂とアニオン交換樹脂を分離するのに必
要にして充分な［１ｈ間行ない１通常は３０分前後であ
る。前述したごとく当該逆洗工程時の膨張状態にある両
イオン交換樹脂層は乱流となっており、第４図に示した
ごとく両イオン交換樹脂の分離面８′は流動的であり乱
れている。As shown in Fig. 4, the normal backwash flow rate from the lower part of the ion exchange tower 2, that is, the flow rate at which the resin bed height expands by about 100% with respect to the packed resin bed height, is LV7 to 12 nt.
/H backwash water 3 is introduced to separate the mixed resin and form a cation exchange resin layer 6' and an anion exchange resin layer 7' in an expanded state. The inflow time of the backwash water 3 is necessary and sufficient to separate the cation exchange resin and anion exchange resin [1 hour, usually about 30 minutes. As mentioned above, both ion exchange resin layers in an expanded state during the backwashing process are in a turbulent flow, and as shown in Figure 4, the separation surface 8' of both ion exchange resins is fluid and turbulent. .
次に本発明は以上のような通常の逆洗流速による逆洗分
離を実施しだ後、第５図に示したように低流速の逆洗水
１３を流入し、膨張状態にあるカチオン交換樹脂層６′
とアニオン交換樹脂層７′を沈下させる。本工程は乱流
状態で膨張している両イオン交換樹脂を膨張させたまま
沈下させることにより層流状態とし。Next, in the present invention, after carrying out the backwash separation at the normal backwash flow rate as described above, backwash water 13 at a low flow rate is introduced as shown in FIG. layer 6'
and sink the anion exchange resin layer 7'. In this process, both ion exchange resins, which are expanding in a turbulent flow state, are allowed to sink while remaining expanded to create a laminar flow state.
これによって第５図に示したように分離面８′を平坦な
面に整えるものであるが、この目的を達成するだめには
当該逆洗水１３のＬＶを５ｍ／Ｈ以下にすることが必要
であり、好ましくはＬＶ３ｍ／Ｈ前後とする。また当該
逆洗水１３の流入時間はそれ程長時間行なう必要がな（
１０分前後の流入で分離面８′を整えることができる。As a result, the separation surface 8' is made flat as shown in Fig. 5, but in order to achieve this purpose, it is necessary to make the LV of the backwash water 13 5 m/H or less. and preferably around LV3m/H. Also, the inflow time of the backwash water 13 does not need to be so long (
The separation surface 8' can be prepared by flowing in for about 10 minutes.
なおＬＶ’７〜１２ｍ／Ｈの通常の逆洗流速の逆洗水３
を流入した後に＋ ’Ｌ Ｖ ５ ｐｎ ／ Ｈ以下の
低流速の逆洗水１３に切り変える場合、その流量を多段
階に低下させても、あるいは一段階で低下させてもその
効果は同様である。要はすくなくとも沈整する前に５
ｍ ／ Ｈ以下の低流速の逆洗水を流入することが大切
である。In addition, backwash water 3 with a normal backwash flow rate of LV'7 to 12 m/H
When switching to backwash water 13 with a low flow rate of +'L V 5 pn/H or less after flowing in, the effect is the same whether the flow rate is reduced in multiple steps or in one step. be. The point is at least 5 before settling.
It is important to inflow backwash water at a low flow rate of less than m/H.
このように低流速の逆洗水１３の流入により乱流状態に
あった膨張層を整えた後、当該逆洗水１３の流入を止め
膨張層を沈整する。After the expansion layer, which was in a turbulent state, is adjusted by the inflow of the backwash water 13 at a low flow rate, the inflow of the backwash water 13 is stopped and the expansion layer is settled.
本発明の以上のような工程により第６図に示したように
、支持板４の周縁部に混合樹脂１′が残留することなく
、かつカチオン交換樹脂層６とアニオン交換樹脂Ｎ７の
分離面８は平坦となり、従来の逆洗分離において生じて
いた欠点を全て解決することができる。したがって両イ
オン交換樹脂を再生する際に、ＣＩ形のアニオン交換樹
脂あるいはＮａ形のカチオン交換樹脂の生成量を大幅に
低減させることができ、従来の混床式イオン交換装置で
生じていた純度上昇不良という欠点を効果的に解決でき
る。Through the above steps of the present invention, as shown in FIG. 6, the mixed resin 1' does not remain on the peripheral edge of the support plate 4, and the separation surface 8 of the cation exchange resin layer 6 and the anion exchange resin N7 is removed. becomes flat, which solves all the drawbacks of conventional backwash separation. Therefore, when regenerating both ion exchange resins, it is possible to significantly reduce the amount of CI type anion exchange resin or Na type cation exchange resin produced, resulting in an increase in purity that would occur with conventional mixed bed ion exchange equipment. The defect of defects can be effectively solved.
以下に本発明の効果を明確にするだめに実施例を説明す
る。Examples will be described below in order to clarify the effects of the present invention.
実施例−１
内径’ ＋ ２ ”６；”Ｑ；’Ｈ直線部高さ２，５０
０ｍｍのイオン交換塔に’１ｏｏｔの強酸性カチオン交
換樹脂アンバーライト（登録商標）工Ｒ−１２４と、
’７００ｔの強塩基性アニオン交換樹脂アンバーライト
ＩＲＡ−９００の混合樹脂を充填し、以下の本発明の逆
洗分離方法と従来の逆洗分離方法でカチオン交換樹脂と
アニオン交換樹脂を分離した。Example-1 Inner diameter' + 2 "6;"Q;'H straight part height 2,50
0mm ion exchange column with '1 root of strong acidic cation exchange resin Amberlite (registered trademark) R-124,
A mixed resin of 700 tons of strongly basic anion exchange resin Amberlite IRA-900 was filled, and the cation exchange resin and anion exchange resin were separated by the following backwash separation method of the present invention and a conventional backwash separation method.
（１）本発明方法
イオン交換塔の下部から１．９ｋｆ／ｃｒｌＧの圧縮空
気を１．４７７１″／分で１分間流入すると同時にｈｖ
、ｚｏｍ／Ｈの逆洗水を１分間流入し、その後にｂｖ１
ｏｍ／Ｈの逆洗水をイオン交換塔の下部から３０分間流
入してカチオン交換樹脂とアニオン交換樹脂を逆洗分離
し９次いで逆洗水の流速を：ｓｍ／Ｈに低下させ、この
低流速逆洗を約１０分間行なった後、逆洗水の流入を止
めて沈整した。(1) Method of the present invention Compressed air of 1.9 kf/crlG is introduced from the bottom of the ion exchange column at 1.4771″/min for 1 minute, and at the same time hv
, zom/H backwash water for 1 minute, then bv1
The cation exchange resin and the anion exchange resin were backwashed and separated by flowing backwash water of 1.0 m/H from the bottom of the ion exchange tower for 30 minutes.9 Then, the flow rate of the backwash water was reduced to: sm/H, and this low flow rate After backwashing was performed for about 10 minutes, the inflow of backwash water was stopped and settling was performed.
（２）従来方法
イオン交換塔の下部からＬＶＩＯｍ／Ｈの逆洗水を３０
分間流入してカチオン交換樹脂とアニオン交換樹脂を逆
洗分離した後、逆洗水の流入を止めて沈整した。(2) Conventional method Backwash water of LVIOm/H from the bottom of the ion exchange tower
After the cation exchange resin and anion exchange resin were backwashed and separated for a minute, the backwash water was stopped flowing and settled.
以上のような本発明方法と従来方法で逆洗分離を行ない
、カチオン交換樹脂とアニオン交換樹脂の分離状態を観
察したところ以上の様な結果であった。Backwash separation was performed using the method of the present invention and the conventional method as described above, and the state of separation of the cation exchange resin and anion exchange resin was observed, and the results were as described above.
まず本発明方法においては２分離面に付設されている一
方の覗き窓と、その裏側に付設されている他方の覗き窓
における分離面の位置は等しく、さらに分離された上部
のアニオン交換樹脂のみを注意深く塔外に取り出しだ後
、カチオン交換樹脂層のみについて、もう一度本発明の
逆洗方法を実施してもカチオン交換樹脂層の上部にアニ
オン交換樹脂層は形成されなかった。従来方法では前記
一方の覗き窓と前記他方の覗き窓における分離面の位置
が約４０ｍｍ程相違しており、さらに同じように上部の
アニオン交換樹脂のみを塔外に取り出した後、カチオン
交換樹脂層のみについて。First, in the method of the present invention, the positions of the separation surfaces of one observation window attached to the two separation planes and the other observation window attached to the back side of the separation plane are equal, and furthermore, only the separated upper anion exchange resin can be seen. After being carefully taken out of the tower, only the cation exchange resin layer was subjected to the backwashing method of the present invention once again, but no anion exchange resin layer was formed above the cation exchange resin layer. In the conventional method, the positions of the separation planes in the one observation window and the other observation window differ by about 40 mm, and in the same way, after only the upper anion exchange resin is taken out of the tower, the cation exchange resin layer is removed. About only.
今度は本発明の逆洗方法を実施した結果、カチオン交換
樹脂層の上部に約３０１１ｍのアニオン交換樹脂が形成
された。このアニオン交換樹脂量は全アニオン交換樹脂
の約５％に相当する。すなわち従来の逆洗方法では全ア
ニオン交換樹脂の約５チが支持板周縁部に残留していた
ことが確認された。This time, as a result of implementing the backwashing method of the present invention, about 3011 m of anion exchange resin was formed on top of the cation exchange resin layer. This amount of anion exchange resin corresponds to about 5% of the total anion exchange resin. That is, it was confirmed that in the conventional backwashing method, about 5 cm of the total anion exchange resin remained on the peripheral edge of the support plate.
実施例−２ 実施例−１で用いたと同じイオン交換塔に。Example-2 In the same ion exchange column used in Example-1.
同じ量の同じ混合樹脂を充填し、以下の通水試験を行な
った。The same amount of the same mixed resin was filled and the following water flow test was conducted.
すなわち実施例−１の（１）で示した本発明の逆洗分離
方法でカチオン交換樹脂とアニオン イ交換樹脂を分離
し、常法により両樹脂を再生し、その後に０．５μｓ／
ｃｍの純水を通水して純度の上昇およびＣｌイオン、
Ｎａイオンのリークを測定した。一方比較するだめに実
施例−１の（２）で示した従来の逆洗分離方法でカチオ
ン交換樹脂とアニオン交換樹脂を分離し、同様に両樹脂
を再生し、同じように純水を通水して純度の上昇および
Ｃｌイオン、 Ｎａイオンのリークを測定した。That is, the cation exchange resin and the anion exchange resin are separated by the backwash separation method of the present invention shown in (1) of Example 1, and both resins are regenerated by a conventional method.
cm of pure water is passed through to increase the purity and Cl ions,
The leakage of Na ions was measured. On the other hand, in order to make a comparison, we separated the cation exchange resin and anion exchange resin using the conventional backwash separation method shown in Example 1 (2), regenerated both resins in the same way, and passed pure water in the same way. The increase in purity and the leakage of Cl ions and Na ions were measured.
なお再生剤の使用量は両者とも１００％ＨＣｌ１３０
ｙ ／ ｔ−Ｒおよび１００％ ＮａＯＨ２００ｔ ／
ｌ−Ｒとした。The amount of regenerating agent used was 100% HCl130 in both cases.
y/t-R and 100% NaOH200t/
It was set as l-R.
両者の通水結果を第７図に示した。Figure 7 shows the water flow results for both cases.
第７図に見られるように従来の逆洗分離方法を実施した
場合では純度の上昇が悪（ＣｌイオンＮａイオン共その
リーク量が大きい。As shown in FIG. 7, when the conventional backwash separation method is implemented, the increase in purity is poor (the leakage amount of both Cl and Na ions is large).
−力木発明の逆洗分離方法を実施した場合では純度の上
昇が良好で、 Ｃｌイオン、 Ｎａイオン共そのリーク
量が小さい。- When the backwash separation method of Rikiki's invention is implemented, the increase in purity is good, and the amount of leakage of both Cl ions and Na ions is small.
第１図および第２図は従来の逆洗分離方法における分離
の状態を示した説明図であり。
第１図は逆洗分離前の状態説明図、第２図は逆洗分離後
の状態説明図である。
また第３図〜第６図はいずれも本発明の逆洗分離方法に
おける分離の状態を示した説明図であり、第３図は逆洗
分離前の状態説明図。
第４図、第５図は逆洗分離中の状態説明図。
第６図は逆洗分離後の状態説明図である。また第７図は
実施例における通水結果を示すグラフであり、縦軸にＣ
１イオン、Ｎａイオンのリークおよび導電率を示し、横
すｌ＋に通水時間を示す。なおグラフ中の実線は本発明
方法。
点線は従来方法を示し、■印は導電率、Ｘ印ばＣ１イオ
ンリーク、Δ印はＮａリークをそれぞれ示す。
１・・・混合樹脂 ２・・・イオン交換塔３・・・逆洗
水 ４・・・支持板
５・・・周縁部 ６・・・カチオン交換樹脂層７・・・
アニオン交換樹脂層 ８・・・分離面９・・・塩酸 ｌ
Ｏ・・・力性ソーダ溶液１１・・・空気 １２・・・高
流速の逆洗水１３・・・低流速の逆洗水
第５図
第６図FIGS. 1 and 2 are explanatory diagrams showing the state of separation in a conventional backwash separation method. FIG. 1 is an explanatory diagram of the state before backwash separation, and FIG. 2 is an explanatory diagram of the state after backwash separation. Moreover, FIGS. 3 to 6 are all explanatory views showing the state of separation in the backwash separation method of the present invention, and FIG. 3 is an explanatory view of the state before backwash separation. FIG. 4 and FIG. 5 are state explanatory diagrams during backwash separation. FIG. 6 is an explanatory diagram of the state after backwash separation. Moreover, FIG. 7 is a graph showing the water flow results in the example, and the vertical axis shows C.
1 ion, Na ion leakage and conductivity are shown, and the horizontal line 1+ shows the water flow time. The solid line in the graph represents the method of the present invention. The dotted line indicates the conventional method, the symbol ■ indicates conductivity, the symbol X indicates C1 ion leak, and the symbol Δ indicates Na leak. DESCRIPTION OF SYMBOLS 1...Mixed resin 2...Ion exchange tower 3...Backwash water 4...Support plate 5...Peripheral part 6...Cation exchange resin layer 7...
Anion exchange resin layer 8... Separation surface 9... Hydrochloric acid l
O...Powerful soda solution 11...Air 12...High flow rate backwash water 13...Low flow rate backwash water Figure 5 Figure 6
Claims (1)
されているイオン交換塔の下部から逆洗水を流入してカ
チオン交換樹脂とアニオン交換樹脂の膨張層を形成し、
その後に沈整することによりカチオン交換樹脂とアニオ
ン交換樹脂を分離するにあたり、イオン交換塔の下部か
ら気体およびまたはＬｖ１３ｍ／Ｈ以上の逆洗水を流入
して、イオン交換塔の支持板周縁部に存在する混合樹脂
を当該周縁部から離脱させる工程と、イオン交換塔の下
部からＬＶ’ｉ’〜１２ｍ／Ｈの逆洗水を流入して、カ
チオン交換樹脂とアニオン交換樹脂の膨張層を形成する
工程と、すくなくとも逆洗水の流速をＬＶ５ｍ／Ｈ以下
に低下させて、当該膨張層を膨張状態を維持したまま沈
下させる工程と、逆洗水の流入を止めて膨張状態にある
カチオン交換樹脂とアニオン交換樹脂を沈整する工程と
を順に行なうことを特徴とする混合樹脂の逆洗分離方法Backwash water is introduced from the bottom of the ion exchange tower filled with a mixed resin of cation exchange resin and anion exchange resin to form an expanded layer of cation exchange resin and anion exchange resin,
In order to separate the cation exchange resin and anion exchange resin through subsequent settling, gas and/or backwash water of Lv13m/H or more is flowed from the lower part of the ion exchange tower to the peripheral edge of the support plate of the ion exchange tower. A step of separating the existing mixed resin from the peripheral portion, and flowing backwash water of LV'i' ~ 12 m/H from the lower part of the ion exchange tower to form an expanded layer of cation exchange resin and anion exchange resin. a step of reducing the flow rate of the backwash water to at least LV5m/H or less to allow the expansion layer to sink while maintaining the expanded state; and a step of stopping the inflow of the backwash water and removing the cation exchange resin from the expanded state. A method for backwashing and separating mixed resins, characterized by sequentially performing the step of settling an anion exchange resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58125462A JPS6019041A (en) | 1983-07-12 | 1983-07-12 | Backwash separation method for mixed resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP58125462A JPS6019041A (en) | 1983-07-12 | 1983-07-12 | Backwash separation method for mixed resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS6019041A true JPS6019041A (en) | 1985-01-31 |
| JPH046422B2 JPH046422B2 (en) | 1992-02-05 |
Family
ID=14910684
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP58125462A Granted JPS6019041A (en) | 1983-07-12 | 1983-07-12 | Backwash separation method for mixed resin |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6019041A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02126943A (en) * | 1988-11-06 | 1990-05-15 | Kotobuki Kogyo Kk | Method for regenerating ion-exchange resin of mixed-bed deionizer |
| JP2004255292A (en) * | 2003-02-26 | 2004-09-16 | Japan Organo Co Ltd | Method for filling condensed water desalting apparatus with ion exchange resin |
| JP2012086123A (en) * | 2010-10-18 | 2012-05-10 | Japan Organo Co Ltd | Method for separating mixed resin of mixed bed resin packed column |
| WO2025173294A1 (en) * | 2024-02-14 | 2025-08-21 | 栗田工業株式会社 | Separation tower for mixture of ion-exchange resins and method for separating mixture of ion-exchange resins using same |
-
1983
- 1983-07-12 JP JP58125462A patent/JPS6019041A/en active Granted
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH02126943A (en) * | 1988-11-06 | 1990-05-15 | Kotobuki Kogyo Kk | Method for regenerating ion-exchange resin of mixed-bed deionizer |
| JP2004255292A (en) * | 2003-02-26 | 2004-09-16 | Japan Organo Co Ltd | Method for filling condensed water desalting apparatus with ion exchange resin |
| JP2012086123A (en) * | 2010-10-18 | 2012-05-10 | Japan Organo Co Ltd | Method for separating mixed resin of mixed bed resin packed column |
| WO2025173294A1 (en) * | 2024-02-14 | 2025-08-21 | 栗田工業株式会社 | Separation tower for mixture of ion-exchange resins and method for separating mixture of ion-exchange resins using same |
| JP2025124134A (en) * | 2024-02-14 | 2025-08-26 | 栗田工業株式会社 | Mixed ion exchange resin separation column and mixed ion exchange resin separation method using the same |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH046422B2 (en) | 1992-02-05 |
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