JPH046422B2 - - Google Patents
Info
- Publication number
- JPH046422B2 JPH046422B2 JP58125462A JP12546283A JPH046422B2 JP H046422 B2 JPH046422 B2 JP H046422B2 JP 58125462 A JP58125462 A JP 58125462A JP 12546283 A JP12546283 A JP 12546283A JP H046422 B2 JPH046422 B2 JP H046422B2
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- anion exchange
- resin
- backwash
- 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.)
- Expired - Lifetime
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 66
- 239000003957 anion exchange resin Substances 0.000 claims description 57
- 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 54
- 239000003729 cation exchange resin Substances 0.000 claims description 49
- 239000011347 resin Substances 0.000 claims description 43
- 229920005989 resin Polymers 0.000 claims description 43
- 238000005342 ion exchange Methods 0.000 claims description 22
- 230000002093 peripheral effect Effects 0.000 claims description 16
- 238000000034 method Methods 0.000 claims description 13
- 238000011001 backwashing Methods 0.000 claims description 12
- 239000007789 gas Substances 0.000 claims 1
- 230000001376 precipitating effect Effects 0.000 claims 1
- 238000000926 separation method Methods 0.000 description 51
- 239000000460 chlorine Substances 0.000 description 13
- 239000003456 ion exchange resin Substances 0.000 description 12
- 229920003303 ion-exchange polymer Polymers 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000010586 diagram Methods 0.000 description 8
- 150000002500 ions Chemical class 0.000 description 8
- 238000007796 conventional method Methods 0.000 description 5
- 229910001415 sodium ion Inorganic materials 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 230000001172 regenerating effect Effects 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 230000000694 effects Effects 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 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
- 229920001429 chelating resin Polymers 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000012530 fluid 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
- 239000008213 purified water Substances 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
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カ性ソー
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、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、通常LV（線速度、以下同様）７〜12m／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、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、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つた分離層を
形成することができる。 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 caustic soda solution is sometimes adopted, but the following backwash separation using water flow is usually performed. That is, first, backwash water is introduced from the lower part of the ion exchange tower filled with the mixed resin at a flow rate that causes the mixed resin to expand by about 100%, usually LV (linear velocity, hereinafter the same) 7 to 12 m/H. The mixed resin is expanded and fluidized. When the mixed resin is allowed to expand and flow in this way, a difference occurs in the settling speed of both ion exchange resins in the rising water, and the cation exchange resin with a higher specific gravity gathers at the bottom and the anion exchange resin with a lower specific gravity gathers at the top, resulting in an expanded state. Two layers of 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 separated layer can be formed.
このような逆洗分離を行なつた後、二層を形成
したまま、あるいはたとえば上層のアニオン交換
樹脂を別塔に取り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
を行なつた後再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 such backwash separation, the anion exchange resin in the upper layer may be taken out into a separate column, the cation exchange resin being regenerated with acid and the anion exchange resin with alkali, and then washed with water while the two layers are still formed. After this, the regenerated both ion exchange resins are mixed and water is passed through 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つていることが
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くLV7〜
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。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）とその裏側に付設され
ている他方の覗き窓（図示せず）から分離面を観
察すると、両者の分離面のレベルに40mm前後の差
が生じていることが確認された。 That is, in the conventional backwash separation method, as shown in FIG.
Backwash water 3 flows in at a rate of 12 m/H and causes the mixed resin to expand and flow to level L, which is about 100% of the height of the filled resin layer. The mixed resin 1' existing on the peripheral edge 5 of the 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. In addition, if backwash water is introduced to form two layers of expanded cation exchange resin and anion exchange resin, and then the 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) attached to the back side, the distance between the two separation surfaces will be approximately 40 mm. It was confirmed that there was a difference in
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り、また分離面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ず巻き状の
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、この乱流状態を保つ
たま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′がそのまま残
留したり、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。 The reason why the mixed resin 1' existing on the peripheral edge 5 of the support plate 4 remains is because water is difficult to flow in that area, and the reason why the separation surface 8 is disturbed is because the flow rate of the backwash water 3 is too low. Because it is in a turbulent area, the ion exchange resin expands and flows, creating a spiral-like turbulent flow state, and when the flow of backwash water is stopped and the ion exchange resin is allowed to settle, it settles while maintaining this turbulent flow state. This is due to this. If the mixed resin 1' remains as it is on the peripheral edge 5 of the support plate 4, or if the separation surface 8 is disturbed, problems will arise in the subsequent regeneration, which will impair the 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Cl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、あるい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Cl形となり、またアニオン交換樹
脂層７を再生するためにカ性ソーダ溶液１０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図に示したよ
うな一塔で両イオン交換樹脂を再生せず、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、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、したがつてこれら混入したアニオン交換樹脂
がCl形に、カチオン交換樹脂がNa形になること
は同様である。 That is, in FIG. 2, the cation exchange resin layer 6
For example, when hydrochloric acid 9 is passed through the anion exchange resin in the mixed resin 1' to regenerate it, the anion exchange resin becomes the Cl form. In addition, since the separation surface 8 is disturbed, an anion exchange resin layer 7 is present at the bottom of a collector (not shown) installed inside the separation surface, or a cation exchange resin layer 6 is present at the top of the collector.
When the anion exchange resin is passed through the collector, the anion exchange resin present at the bottom of the collector becomes Cl form, and when the caustic soda solution 10 is passed through to regenerate the anion exchange resin layer 7, the cation exchange resin present at the top of the collector becomes chlorine. The resin becomes Na form. Note that, instead of regenerating both ion exchange resins in one tower as shown in FIG. 2, the cation exchange resin layer 6 and the anion exchange resin layer 7 are separated.
Even when the cation exchange resin 1' is separated into separate columns and regenerated separately, the mixed resin 1' will be mixed into the cation exchange resin layer 6. Furthermore, since the separation surface 8 is disturbed, both ion exchange resin layers are separated into separate columns. During separation, anion exchange resin is mixed into the cation exchange resin layer and cation exchange resin is mixed into the anion exchange resin layer, so the mixed anion exchange resin becomes Cl form and the cation exchange resin becomes Na form. The same thing happens.
こ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、Clイオンリ
ークの制限が厳しく、したがつて再生後における
Cl形のアニオン交換樹脂あるいはNa形のカチオ
ン交換樹脂の混入量を出来るだけ低減しなければ
ならない。 In this way, the presence of Cl-type anion exchange resin or Na-type cation exchange resin after regeneration will cause a poor increase in the purity of the treated water, especially in the condensate desalination equipment of PWR type nuclear power plants. There are strict restrictions on Na ion leakage and Cl ion leakage in water, so
The amount of Cl type anion exchange resin or Na type cation exchange resin mixed in 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
Gas and or
A step in which backwashing water of LV13m/H or more is introduced to separate the mixed resin existing at the peripheral edge of the support plate of the ion exchange tower from the peripheral edge, and backwashing of LV7~12m/H from the lower part of the ion exchange tower. The step of introducing water to form an expanded layer of cation exchange resin and anion exchange resin, and the flow rate of backwash water at least LV5m/
The step of lowering the temperature to below H and allowing the expanded layer to settle while maintaining the expanded state, and the step of stopping the inflow of backwash water and settling the expanded cation exchange resin and anion exchange resin are performed in this order. The present invention relates to a method for backwashing and separating mixed resins, which is characterized by the following.
以下に本発明を詳細に説明する。 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、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、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、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工程を順に行なつて逆洗分離を行なうものであ
る。 The first drawback of the conventional backwash separation method is that the mixed resin remains on the periphery of the support plate, and this is caused by the slow flow of water around the periphery of the support plate. Due to no expansion 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 introduces 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 reverses 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明する。 Below, the backwash separation method of the present invention will be explained step by step 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１１ま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1.9Kg／cm2Ｇ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。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20m／Ｈ前後とするとよい。なお空気１１ある
いは当該逆洗水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。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
くする必要がなく、たとえば２分以下の単時間で
充分であり、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）にネツト
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。 First, as shown in FIG. 3, a gas such as air 11 or high-flow backwash water 12, or air 11 and high-flow backwash water 12, is 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, especially at the peripheral edge of the support plate 4, is completely removed. In this case, it is sufficient for the amount of air 11 to flow in, for example, at a pressure of 1.9 Kg/cm 2 G in an amount approximately equal to the amount of filled resin in about one minute. Further, the inflow rate of the backwash water 12 is set to be at least LV13m/H or more, preferably around 20m/H. Note that even if the air 11 or the backwash water 12 flows in alone, the mixed resin present at the peripheral edge of the support plate 4 can be completely removed, but if the air 11 and the backwash water 12 flow in at the same time. is more effective. Furthermore, since the purpose of this step is to separate the mixed resin 1' from the peripheral edge of the support plate 4, there is no need to make the inflow time of the air 11 and/or the backwash water 12 very long, for example, 2 minutes or less. A single period of time is sufficient, and usually 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 is wrapped around it, which is undesirable.
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、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
〜12m／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時間行
ない、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
層は乱流となつており、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。 Immediately after the mixed resin 1' existing on the peripheral edge of the support plate 4 is removed from the peripheral edge, the fourth
As shown in the figure, the normal backwash flow rate from the bottom of ion exchange tower 2, that is, approximately
LV7, a flow rate that causes 100% resin layer height expansion
Backwash water 3 of ~12 m/h 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 a sufficient time necessary to separate the cation exchange resin and anion exchange resin, and is usually around 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 FIG. 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た後、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、これによつて第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ためには当該逆洗水１
３のLVを5m／Ｈ以下にすることが必要であり、
好ましくはLV13m／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
なく10分間前後の流入で分離面８′を整えること
ができる。 Next, in the present invention, after performing 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. 6' and anion exchange resin layer 7' are allowed to sink. In this process, the amphoteric ion exchange resin, which is expanding in a turbulent flow state, is allowed to sink while remaining expanded to create a laminar flow state, thereby making the separation surface 8' a flat surface as shown in FIG. However, in order to achieve this purpose, the backwash water 1
It is necessary to make the LV of 3 below 5m/H,
Preferably the LV is around 13m/H. Further, the inflow time of the backwash water 13 does not need to be so long, and the separation surface 8' can be prepared by inflowing for about 10 minutes.
なおLV7〜12m／Ｈの通常の逆洗流速の逆洗水
３を流入した後に、LV5m／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5m／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, when switching to backwash water 13 with a low flow rate of LV5m/H or less after flowing backwash water 3 with a normal backwash flow rate of LV7 to 12m/H, even if the flow rate is reduced in multiple stages, Alternatively, the effect is the same even if it is lowered in one step. In short, it is important to at least introduce backwash water at a low flow rate of 5 m/H or less before settling.
このように低流速の逆洗水１３の流入により乱
流状態にあつた膨張層を整えた後、当該逆洗水１
３の流入を止め膨張層を沈整する。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層
７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。したがつて両イオン交換樹脂を再生する際
に、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。 After adjusting the expansion layer which was in a turbulent flow state due to the inflow of the backwash water 13 at a low flow rate, the backwash water 13 is
Stop the inflow of 3 and settle the expanded layer. As shown in FIG. 6, the above steps of the present invention prevent the mixed resin 1' from remaining on the peripheral edge of the support plate 4.
In addition, the separation surface 8 between the cation exchange resin layer 6 and the anion exchange resin layer 7 becomes flat, and all the drawbacks that have occurred in conventional backwash separation can be solved. Therefore, when regenerating both ion exchange resins, it is possible to significantly reduce the amount of Cl type anion exchange resin or Na type cation exchange resin produced, which was generated in conventional mixed bed ion exchange equipment. The drawback of poor purity increase can be effectively solved.
以下に本発明の効果を明確にするために実施例
を説明する。 Examples will be described below to clarify the effects of the present invention.
実施例 １
内径1200mm、直線部高さ2500mmのイオン交換塔
に700の強酸性カチオン交換樹脂アンバーライ
ト（登録商標）IR−124と、700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 A mixed resin of 700 strong acidic cation exchange resin Amberlite (registered trademark) IR-124 and 700 strong basic anion exchange resin Amberlite IRA-900 was placed in an ion exchange tower with an inner diameter of 1200 mm and a straight section height of 2500 mm. was filled, and the cation exchange resin and anion exchange resin were separated using the backwash separation method of the present invention and the conventional backwash separation method described below.
(1) 本発明方法
イオン交換塔の下部から1.9Kg／cm2Ｇの圧縮空
気を1.4m3／分で１分間流入すると同時に
LV20m／Ｈの逆洗水を１分間流入し、その後に
LV10m／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、次いで逆洗水の流速を3m／
Ｈに低下させ、この低流速逆洗を約10分間行なつ
た後、逆洗水の流入を止めて沈整した。(1) Method of the present invention At the same time, compressed air of 1.9 Kg/cm 2 G is introduced from the bottom of the ion exchange tower at a rate of 1.4 m 3 /min for 1 minute.
Inject backwash water at LV20m/H for 1 minute, then
Backwash water at LV10m/H from the bottom of the ion exchange tower
The cation exchange resin and anion exchange resin were backwashed and separated for 30 minutes, and then the flow rate of the backwash water was increased to 3 m/min.
After lowering the temperature to H and performing this low-flow backwashing for about 10 minutes, the inflow of backwashing water was stopped and settling was performed.
(2) 従来方法
イオン交換塔の下部からLV10m／Ｈの逆洗水
を45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 at LV10m/H was flowed from the lower part of the ion exchange tower for 45 minutes to backwash and separate the cation exchange resin and anion exchange resin, and then the backwash water was stopped 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
つた。 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、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た後、カチオン交換樹脂
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つた。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、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30mm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てアニオン交
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％が支持板周
縁部に残留していたことが確認された。 First, in the method of the present invention, the positions of the separation surface in one viewing window attached to the separation surface and the other viewing window attached to the back side thereof are equal;
Furthermore, even if only the separated upper anion exchange resin is carefully taken out of the tower and the cation exchange resin is subjected to the backwashing method of the present invention once again, no anion exchange resin layer is formed on top of the cation exchange resin layer. It was not done. In the conventional method, the positions of the separation surfaces 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. As a result of carrying out the backwashing method of the present invention for only this time, about 30 mm of anion exchange resin was formed on the top of the cation exchange resin layer. The total amount of anion exchange resin corresponds to about 5% of the anion exchange resin. That is, it was confirmed that in the conventional backwashing method, about 5% 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、同
じ量の同じ混合樹脂を充填し、以下の通水試験を
行なつた。Example 2 The same ion exchange tower used in Example-1 was filled with the same amount of the same mixed resin, 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
0.5〓／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
較するために実施例−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, a cation exchange resin and an 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.
Purity increases and Cl
The leakage of ions and Na ions was measured. On the other hand, for comparison, the cation exchange resin and anion exchange resin were separated using the conventional backwash separation method shown in (2) of Example 1, and both resins were regenerated in the same way, and purified water was passed in the same manner. 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％
HCl130g／ｌ−Ｒおよび100％NaOH200ｇ／ｌ
−Ｒとした。 The amount of regenerating agent used is 100% in both cases.
HCl130g/l-R and 100% NaOH200g/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くClイオンNa
イオン共そのリーク量が大きい。一方本発明の逆
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。 As shown in Figure 7, when the conventional backwash separation method is used, the increase in purity is poor and Cl ions and Na
The amount of ion leakage is large. On the other hand, when the backwashing separation method of the present invention is carried out, 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Clイオン、Naイオンのリークお
よび導電率を示し、横軸に通水時間を示す。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、×印はClイオンリーク、△
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、１０……カ性ソーダ
溶液、１１……空気、１２……高流速の逆洗水、
１３……低流速の逆洗水。
Figures 1 and 2 are explanatory diagrams showing the state of separation in a conventional backwash separation method. Figure 1 is an explanatory diagram of the state before backwash separation, and Figure 2 is an explanatory diagram of the state after backwash separation. It is a diagram. Moreover, FIGS. 3 to 6 are all explanatory diagrams showing the state of separation in the backwash separation method of the present invention, and FIG. 3 is an explanatory diagram of the state before backwash separation, and FIGS. 6 is an explanatory diagram of the state during backwash separation, and FIG. 6 is an explanatory diagram of the state after backwash separation. Moreover, FIG. 7 is a graph showing the water flow results in Examples, in which the vertical axis shows the leakage of Cl ions and Na ions and the electrical conductivity, and the horizontal axis shows the water flow time. In addition, the solid line in the graph shows the method of the present invention, the dotted line shows the conventional method, ○ mark shows conductivity, × mark shows Cl ion leak, △
Each mark indicates a Na leak. 1...Mixed resin, 2...Ion exchange tower, 3...
Backwash water, 4... Support plate, 5... Periphery, 6... Cation exchange resin layer, 7... Anion exchange resin layer,
8... Separation surface, 9... Hydrochloric acid, 10... Caustic soda solution, 11... Air, 12... High flow rate backwash water,
13...Low flow rate backwash water.
Claims (1)
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。1 By flowing backwash water 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 settling it. When separating the cation exchange resin and anion exchange resin, gas and or backwash water with a LV of 13 m/H or more is introduced from the bottom of the ion exchange tower.
A step of separating the mixed resin present at the peripheral edge of the support plate of the ion exchange tower from the peripheral edge, and a step of flowing backwash water of LV7 to 12 m/H from the lower part of the ion exchange tower to separate the cation exchange resin and anion exchange resin. a step of forming an inflatable layer, a step of reducing the flow rate of backwash water to at least LV5m/H or less and allowing the inflatable layer to sink while maintaining the inflated state, and a step of stopping the inflow of backwash water to maintain the inflated state. 1. A method for backwashing and separating a mixed resin, comprising sequentially performing the step of precipitating a cation exchange resin and 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 JPS6019041A (en) | 1985-01-31 |
| JPH046422B2 true 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) |
Families Citing this family (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 |
| JP3960930B2 (en) * | 2003-02-26 | 2007-08-15 | オルガノ株式会社 | Ion exchange resin filling method for condensate demineralizer |
| JP5568434B2 (en) * | 2010-10-18 | 2014-08-06 | オルガノ株式会社 | Separation method of mixed resin in mixed bed type resin packed tower |
| JP7758068B2 (en) * | 2024-02-14 | 2025-10-22 | 栗田工業株式会社 | Mixed ion exchange resin separation column and mixed ion exchange resin separation method using the same |
-
1983
- 1983-07-12 JP JP58125462A patent/JPS6019041A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS6019041A (en) | 1985-01-31 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JPH0328797A (en) | Method for removeing suspensible impurity of condensate by mixed end type condensate desalting device | |
| JPH046422B2 (en) | ||
| JP2940651B2 (en) | Pure water production equipment | |
| JP2002361247A (en) | Pure water production method | |
| JPH046423B2 (en) | ||
| JP2607534B2 (en) | Device for removing odor components in pure water | |
| JP3851491B2 (en) | Apparatus and method for purifying boron eluent | |
| JPH0432700B2 (en) | ||
| JP2607544B2 (en) | Ion exchange tower used for upflow regeneration | |
| JP2940648B2 (en) | Pure water production equipment | |
| JP2742975B2 (en) | Regeneration method of ion exchange device | |
| JP4315385B2 (en) | Ion exchange tower | |
| JPH10128128A (en) | Separation and regeneration method of ion exchange resin | |
| JP2003088765A (en) | Countercurrent regeneration type ion exchange apparatus and method for cleaning packed bed of ion exchange resin in the apparatus | |
| JPS59183398A (en) | Maintenance system of condensate desalt tower | |
| JP4216998B2 (en) | Regeneration method of mixed-bed type sugar liquid purification equipment | |
| JPH0771669B2 (en) | Ultrapure water production method | |
| JPS6340137B2 (en) | ||
| JPH0999244A (en) | Separation and regeneration method of ion exchange resin | |
| JP2005296749A (en) | Condensate demineralization method and device, and method for forming its packed bed | |
| JPS602102B2 (en) | How to regenerate ion exchange resin | |
| JP3543389B2 (en) | Separation and regeneration method of ion exchange resin | |
| JPS6132055B2 (en) | ||
| JPH0626348Y2 (en) | Ion exchange tower | |
| JPS63107754A (en) | Method for separating and transferring ion exchange resin |