JPS63107754A - Method for separating and transferring ion exchange resin - Google Patents
Method for separating and transferring ion exchange resinInfo
- Publication number
- JPS63107754A JPS63107754A JP61253775A JP25377586A JPS63107754A JP S63107754 A JPS63107754 A JP S63107754A JP 61253775 A JP61253775 A JP 61253775A JP 25377586 A JP25377586 A JP 25377586A JP S63107754 A JPS63107754 A JP S63107754A
- Authority
- JP
- Japan
- Prior art keywords
- water
- transfer
- resin
- ion exchange
- exchange resin
- 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
- 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 title claims abstract description 20
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000003456 ion exchange resin Substances 0.000 title claims description 25
- 229920003303 ion-exchange polymer Polymers 0.000 title claims description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 238000012546 transfer Methods 0.000 claims abstract description 69
- 239000011347 resin Substances 0.000 claims abstract description 57
- 229920005989 resin Polymers 0.000 claims abstract description 57
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 230000005484 gravity Effects 0.000 claims abstract description 19
- 238000011001 backwashing Methods 0.000 claims abstract description 4
- 239000010410 layer Substances 0.000 claims description 33
- 238000007664 blowing Methods 0.000 claims description 3
- 150000002500 ions Chemical class 0.000 claims description 3
- 239000002344 surface layer Substances 0.000 claims description 3
- 150000001450 anions Chemical class 0.000 abstract description 6
- 239000003729 cation exchange resin Substances 0.000 abstract description 3
- 101100148729 Caenorhabditis elegans sar-1 gene Proteins 0.000 abstract 1
- 230000002378 acidificating effect Effects 0.000 abstract 1
- 239000003957 anion exchange resin Substances 0.000 abstract 1
- 230000009969 flowable effect Effects 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 229920003048 styrene butadiene rubber Polymers 0.000 description 9
- 239000011734 sodium Substances 0.000 description 8
- 239000012530 fluid Substances 0.000 description 6
- 230000000052 comparative effect Effects 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 5
- 238000011069 regeneration method Methods 0.000 description 5
- 229920001467 poly(styrenesulfonates) Polymers 0.000 description 4
- 239000012492 regenerant Substances 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229940023913 cation exchange resins Drugs 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- 229910021642 ultra pure water Inorganic materials 0.000 description 2
- 239000012498 ultrapure water Substances 0.000 description 2
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 235000002597 Solanum melongena Nutrition 0.000 description 1
- 244000061458 Solanum melongena Species 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000004020 conductor Substances 0.000 description 1
- 238000005115 demineralization Methods 0.000 description 1
- 230000002328 demineralizing effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000002555 ionophore Substances 0.000 description 1
- 230000000236 ionophoric effect Effects 0.000 description 1
- NJPPVKZQTLUDBO-UHFFFAOYSA-N novaluron Chemical compound C1=C(Cl)C(OC(F)(F)C(OC(F)(F)F)F)=CC=C1NC(=O)NC(=O)C1=C(F)C=CC=C1F NJPPVKZQTLUDBO-UHFFFAOYSA-N 0.000 description 1
- 239000013307 optical fiber Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 230000000276 sedentary effect Effects 0.000 description 1
- 238000009491 slugging Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
Landscapes
- Treatment Of Liquids With Adsorbents In General (AREA)
- Treatment Of Water By Ion Exchange (AREA)
Abstract
Description
【発明の詳細な説明】
〔座業上の利用分野〕
本発明は純水、超純水製造装置、特に火力発電所、原子
力発電所の復水処理用の復水脱塩装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Field of Sedentary Use] The present invention relates to a pure water or ultrapure water production apparatus, and particularly to a condensate desalination apparatus for condensate treatment in thermal power plants and nuclear power plants.
２ａＩ類のイオン交換樹脂、特に強酸性陽イオン交換樹
脂（以下ＢＡＲと記す）と強酸性陽イオン交換樹脂（以
下ＳＢＲと記す）の混合樹脂層は純水、超純水製造装置
のポリラシャ−及び火力・原子力発電所の復水脱塩装置
に不可欠のものである。The mixed resin layer of 2aI class ion exchange resins, especially strong acid cation exchange resins (hereinafter referred to as BAR) and strong acid cation exchange resins (hereinafter referred to as SBR), is used in pure water, ultrapure water production equipment, and It is essential for condensate desalination equipment in thermal and nuclear power plants.
従来ＰＷＲ型原子力発電所の復水処理で要求される水質
は最もきびしぐ下記の如くである。The most severe water quality requirements for condensate treatment in conventional PWR nuclear power plants are as follows.
Ｎａ″濃度 α０２ ｐｐｂ以下 ａｔ″″濃度 α０５ ｐｐｂ以下 これらのイオン濃度は低ければ低い程よい。Na″ concentration α02 ppb or less at″″ concentration α05 ppb or less The lower the concentration of these ions, the better.
これらのイオンの混合樹脂層からのリーク量は入口水質
条件、混合樹脂層の運転条件（ＬＶ等）を除くと混合樹
脂層内の塩型樹脂の割合によって支配さｎている。The amount of these ions leaking from the mixed resin layer is controlled by the proportion of salt type resin in the mixed resin layer, excluding the inlet water quality conditions and the operating conditions (LV, etc.) of the mixed resin layer.
すなわちＲ−ａｔ ＜塩素型アニオン樹脂）、Ｒ−Ｎａ
（ナトリウム型カチオン樹脂）の存在割合が多い程Ｎａ
”、 ＯＬ−のり−クが増大する。これらのＲ−Ｎａ、
Ｒ−ＯＬが生成する原因は原水に由来するＮａ”、 ０
Ｌ−ｆ除くと下記の理由が主である。That is, R-at <chlorine type anion resin), R-Na
The higher the proportion of (sodium type cation resin), the more Na
”, OL-Ni-k increases.These R-Na,
The cause of R-OL generation is Na'', 0 derived from raw water.
Excluding L-f, the following reasons are the main reasons.
Ｒ−Ｎａ ： ＢＡＲ，８ＢＲの分離移送が不完全で８
ＢＲ層中に混入し７ｔｊ ＢＡＲがＳＢＲの再生剤であ
るＮａＯＨと接触して生成する。R-Na: BAR, 8BR separation transfer is incomplete and 8
7tj BAR mixed into the BR layer is generated when it comes into contact with NaOH, which is a regenerant for SBR.
ｕ−ａｔ：（１）再生剤ＮａＯＨ中の不純物（ＮａＯＡ
）によって生成する。u-at: (1) Impurities in the regenerant NaOH (NaOA
).
（２）Ｒ−Ｎａと同様分離が不完全で８ＡＲ層中に残留
したＳＢＲがＢＡＲの再生剤であるＨＯｌと接触して生
成する。(2) Similar to R-Na, SBR remaining in the 8AR layer due to incomplete separation is generated when it comes into contact with HOl, which is a BAR regenerant.
Ｒ−Ｎａ生成を少なくする方法は洩々研究され代表的に
は特詐第１０２７７５０号によってすでに解決されてい
る。Methods for reducing R-Na generation have been extensively researched, and a typical method has already been solved by Tokko No. 1027750.
Ｒ−ａｔ生成の主厚因（１）はＮａＯＨの品質向上によ
って問題は小さくなっている。（２）については従来の
技術では分離移送が不完全でＢＡＲ層に全ＳＢＨの１〜
２ｓ程度の日ＢＲが残留し再生毎にこれが蓄積される几
め平衡状態では混合樹脂層のＲ−０１は全日ＢＨの２０
数チの値となっている。The main thickness factor (1) for the generation of R-at has become less of a problem as the quality of NaOH has improved. Regarding (2), in the conventional technology, separation and transfer is incomplete, and 1 to 1 of all SBHs are transferred to the BAR layer.
In a refined equilibrium state where about 2s of daily BR remains and is accumulated every time it is regenerated, R-01 of the mixed resin layer is 20% of the total daily BH.
The value is in the hundreds.
従来の樹脂の分離移送方法金弟８図に晶づいて説明する
。The conventional method for separating and transferring resin will be explained with reference to Figure 8.
逆洗によって混合樹脂層をＢＡＲ層１と８ＢＲ層２の２
つの層に分離した後塔下部からスルージング水ｔ−ＬＶ
２．５ｍ／時程度でスルージング水導入等３から導入し
、ＢＡＲ層２を若干流動させながら塔上部の加圧水導入
管４から加圧水又は加圧空気導入管５から加圧空気全導
入してＢＢＲをアニオン再生塔へ移送する。By backwashing, the mixed resin layer is separated into BAR layer 1 and 8BR layer 2.
Slewing water t-LV from the bottom of the column after separation into two layers.
BBR is carried out by introducing slugging water, etc. from 3 at a rate of about 2.5 m/hour, and while causing the BAR layer 2 to flow slightly, pressurized water is introduced from the pressurized water introduction pipe 4 at the top of the tower, or pressurized air is completely introduced from the pressurized air introduction pipe 5. is transferred to the anion regeneration tower.
移送管６の開口部は第８図では塔中心軸上に設けらｎて
いるが、塔壁近くに設けられている場合もあり、又樋を
利用しているものもある。Although the opening of the transfer pipe 6 is provided on the central axis of the tower in FIG. 8, it may be provided near the tower wall, or a gutter may be used.
又開口部の高さは両樹脂層の境界面の若干下部とするの
が普通である。Further, the height of the opening is usually set to be slightly below the interface between the two resin layers.
このような移送を行う際には、第９図に示す如（ＳＢＲ
２’が数１１１Ｉ〜２０数■残留することは避けられな
い。When carrying out such a transfer, as shown in Figure 9 (SBR
It is inevitable that 2' remains from several 111 I to several 20 ■.
この理由は塔壁に近い８ＢＲ程移送管の開口部に達する
のに時間がかかり、その間に開口部付近の樹脂が移送さ
ｎｌかつ塔下部からのスルージング水鳴より樹脂面が平
面となり、開９部と樹脂層面との間にある距離が生じ１
３ＢＲは移送されなくなってしまうからである。The reason for this is that the closer the 8BR is to the tower wall, the longer it takes to reach the opening of the transfer pipe, and during that time, the resin near the opening is transferred, and the resin surface becomes flat due to the sluicing water noise from the lower part of the tower. A certain distance is created between part 9 and the resin layer surface.
This is because 3BR will no longer be transferred.
この現象はスルージング水量を増しＢＡＲ層の展開率七
人きくしても、又開口部の高さ、形状を変えても同じよ
うに起こ９、ＢＢＨの完全な分離移送は達成さｎない。This phenomenon occurs in the same way even if the amount of sluicing water is increased and the expansion rate of the BAR layer is increased, or even if the height and shape of the opening are changed9, complete separation and transfer of BBH is not achieved.
これら残留し九ＳＤＲは８ＡＲの再生剤のＨＣｔと接触
してＲ−Ｃ３ｔが生成してしまう。These remaining 9SDRs come into contact with HCt of the 8AR regenerant to generate R-C3t.
〔発明が解決しようとしている問題点〕本発明は前記（
２）の問題を解決するものであジ、分離移送時残留する
８ＢＲｔ−出来るだけ少なくし、イオン交換時における
処理水質を向上せしめようとするものである。[Problems to be solved by the invention] The present invention solves the problems described above (
This is to solve the problem of 2).Secondly, it aims to reduce the amount of 8BRt remaining during separation and transfer as much as possible and improve the quality of treated water during ion exchange.
本発明は、比重の異なる２種類のイオン交換樹脂を充填
し几塔において逆洗によってイオン交換樹脂を２層に分
離しｔ後塔上部から加圧水又は加圧空気を、塔下部から
スルージング水を導入して大部分の比重の小さいイオン
交換樹脂を樹脂移送管により移送し、該移送後に、比重
の大きいイオン変換樹脂層上に残留している少量の比重
の小さいイオン交換樹脂を更に分離する方法において、
比重の大きいイオン交換樹脂ｔ−流動状態に保ちながら
、塔の片側から塔壁に沿って設けた水吹き出し部から水
を吹き出し、原水の吹き出し部の反対側の塔壁近くに設
は友樹脂移送管の開口部に向う比重の小さいイオン交換
樹脂のｉｎを起し、該イオン交換樹脂を樹脂移送管の開
口部に集めながら、又は集め几後該開口部から比１の小
さいイオン交換樹脂を抜き出して移送することを特徴と
するイオン交換樹脂の分離移送方法であって、従来の分
離移送方法の問題点を解決すべく実用規模の直径の大き
い塔を用いて鋭意研究し次結果、本発明をなすに到つ友
ものである。The present invention involves filling two types of ion exchange resins with different specific gravities, separating the ion exchange resins into two layers by backwashing in a tower, and then supplying pressurized water or pressurized air from the top of the tower and sluicing water from the bottom of the tower. A method in which most of the ion exchange resin with low specific gravity is introduced and transferred through a resin transfer pipe, and after the transfer, a small amount of ion exchange resin with low specific gravity remaining on the ion exchange resin layer with high specific gravity is further separated. In,
Ion exchange resin with a large specific gravity - While maintaining the fluidized state, water is blown out from a water outlet installed along the tower wall from one side of the tower, and the resin is transferred to a place near the tower wall on the opposite side of the raw water outlet. Inject the ion exchange resin with a small specific gravity toward the opening of the pipe, and while collecting the ion exchange resin at the opening of the resin transfer pipe, or after collecting, extract the ion exchange resin with a small specific gravity of 1 from the opening. This is a method for separating and transporting ion exchange resins, which is characterized by transporting ion exchange resins.In order to solve the problems of conventional separation and transport methods, we conducted extensive research using a practical-scale column with a large diameter, and as a result, we have developed the present invention. It is a friend to eggplant.
以下、図面に基づいて本発明の詳細な説明する。Hereinafter, the present invention will be described in detail based on the drawings.
本発明は第１図に示す如く比重の大きいＳＡＲ層１の上
に残留している斜線部で示す比重の小さいＥＢＲ２’を
分離移送するに当って樹脂分離境界面の近傍、好ましく
は下部で、かつ塔片側の塔壁に沿って移送用スルージン
グＷｓｔ−１そしてその反対側の位置に樹脂移送管６の
開口部６′を設は塔下部集水装置から管３を経て低流速
逆洗水ＱＩｔ−導人し、８ＡＲ１を流動状態とし、更に
吹き出させることにより第２図及び第３図に示す如く樹
脂移送管の開ロ部６′周辺にＳＢＲが集ってきたところ
（図中斜線部）を移送管上の樹脂移送弁７（第１図及び
第３図参照）を開として移送管６を経て移送してしまう
ものである。As shown in FIG. 1, when the EBR 2' with a low specific gravity shown by the hatched area remaining on the SAR layer 1 with a high specific gravity is separated and transferred, in the vicinity of the resin separation interface, preferably at the bottom, In addition, a transfer sluging Wst-1 is provided along the tower wall on one side of the tower, and an opening 6' of the resin transfer pipe 6 is installed on the opposite side of the tower. QIt-conductor, 8AR1 was brought into a fluid state, and by further blowing out, SBR gathered around the opening 6' of the resin transfer pipe as shown in Figures 2 and 3 (the shaded area in the figure). ) is transferred through the transfer pipe 6 by opening the resin transfer valve 7 (see FIGS. 1 and 3) on the transfer pipe.
すなわち本発明はＢＡＲ層１を流動状態とし、かつ更に
塔片側に設は移送用スルージング管８から水を上方へ吹
き出させることにより日ＢＲ２’の開口部に向う流れを
起し、８ＢＲ’ｉ開口部周辺に集め次後排出するように
したものである。That is, the present invention brings the BAR layer 1 into a fluidized state, and further blows water upward from a transfer sluging pipe 8 installed on one side of the column, thereby causing a flow toward the opening of the 8BR'i. It collects around the opening and then discharges it.
本発明で最も重要なのは移送用スルージング管８の位置
、吹き出す水の流速及び吹き出し方向である。The most important factors in the present invention are the position of the transfer sluging pipe 8, the flow rate of the water to be blown out, and the direction of the blown water.
代表的な移送用スルージング管８の位置、吹き出し方向
は第３図及び第４図並びに第５図に示す如き方向が好ま
しい。第２図、第３図は塔壁に沿って移送用スルージン
グ管８として曲管を設は次もので、水の吹き出し方向は
上方に向けて吹出すようになっている。この時一部、曲
管の両端から円周方向に吹き出すのも効果的である。第
４図及び第５図に示すものは直管を用いたもので塔壁に
向って斜め上方に吹き出させ（第５図参照）塔壁とぶつ
かって生じる反転流を利用している。この時も直管両端
から円周方向にも吹き出すようにすｎば効果的である。The typical position of the transfer sluging pipe 8 and the blowing direction are preferably as shown in FIGS. 3, 4, and 5. In FIGS. 2 and 3, a curved pipe is installed along the tower wall as a transfer sluging pipe 8, and the water is blown out in an upward direction. At this time, it is also effective to blow some of the fluid out from both ends of the curved pipe in the circumferential direction. The one shown in FIGS. 4 and 5 uses a straight pipe, which blows out obliquely upward toward the tower wall (see FIG. 5) to utilize the reversed flow generated when it collides with the tower wall. At this time, it is also effective to blow out from both ends of the straight pipe in the circumferential direction as well.
移送用スルージング管８よりこのように水を吹き出すと
、吹き出し口上部の樹脂面が盛ジ上がり、この盛り上が
りが次々に移送管６の開口部６′の万に向かい全体とし
て、８ＢＲ２’！ｒＬ開ロ部６′に向かって流れていく
のである。When water is blown out from the transfer sluging pipe 8 in this way, the resin surface above the outlet rises, and this rise successively moves towards the opening 6' of the transfer pipe 6, resulting in a total of 8BR2'! It flows toward the rL opening portion 6'.
開口部６′に向かう８ＢＲ２’の流ｔが強すぎると流ｎ
が開口部側の塔壁にぶつか９反転流が生じ、この反転流
が生ずると一度果つ７’（８ＢＲが再び反転流にのって
分散してしまう。それ故、吹き出し流速は樹脂移送管の
開口部側において反転流が生じないようにきめるのが好
ましい。実験の結果、塔断面積に対してＬＶｎ５〜２ｍ
／時の流速がよいことがわかつ几。If the flow t of 8BR2' toward the opening 6' is too strong, the flow n
hits the column wall on the opening side and a reverse flow occurs, and once this reverse flow occurs, the 7' (8BR) that is once produced is again carried by the reverse flow and dispersed. It is preferable to decide so that reverse flow does not occur on the opening side of the tube.As a result of experiments, LVn 5 to 2 m relative to the column cross-sectional area.
/ It turns out that the flow rate of time is good.
曲管又は直管の両端からも吹き出させるのに塔壁近くの
ＳＢＲもスムーズに開口部に向かわせる九めである。The ninth feature allows the SBR near the tower wall to smoothly flow toward the opening, even though it can blow out from both ends of a curved or straight pipe.
又、樹脂分離境界面から移送用スルージング管８までの
距離は３００〜６００■、好ましくは４００〜５００ｍ
である。この距離が小さいと水の吹き出しが突沸状態と
なり、又大きすぎると拡散してしまい効果が小さくなる
。Further, the distance from the resin separation interface to the transfer sluging pipe 8 is 300 to 600 m, preferably 400 to 500 m.
It is. If this distance is too small, the water ejected will be in a bumping state, and if it is too large, it will diffuse and the effect will be reduced.
ＥＩＡＲｉ流動状態とする塔下部集水装置からの逆洗水
ＱＩの流速は移送用スルージング管８からの水の吹き出
しにより移送管６の開口ｍ ｂ’へ向かって［３る８Ｂ
ＲがＢＡＲ層内にもぐり込まないように、かつＢＡＲが
流動状態となるような量で導入する。実験の結果、この
流速（Ｑｌ）はＬＶ３〜５ｍ／時の低逆洗流速とするの
がよいことがわかった。開口部に向かう８ＢＲがＢＡＲ
層にもぐり込まないようにするにはこの流速は大きい万
が好ましい。しかし大きすぎるとＢＡＲの逆洗展開率が
大きくなり移送後のＢＡＲの定量性に誤差が生じやすい
ので、前記の範囲内の値とするのが好ましい。The flow rate of the backwash water QI from the lower part of the tower water collection device to be brought into the EIARi fluidized state is as follows:
R is introduced in such an amount that it does not sink into the BAR layer and that the BAR is in a fluid state. As a result of experiments, it was found that this flow rate (Ql) is preferably a low backwash flow rate of LV3 to 5 m/hour. 8BR facing the opening is the BAR
It is preferable that this flow rate is high in order to prevent it from penetrating into the layer. However, if it is too large, the backwash development rate of BAR increases and errors tend to occur in the quantitative nature of BAR after transfer, so it is preferable to set the value within the above range.
又、移送用スルージノグ管８からの吹き出しを間けつ的
に行う万が樹脂移送管開口部６′附近において反転流が
生じにくくなることがわかった。水の吹き出し５〜５０
秒、休止１５〜６０秒のように間けつ的に行うと８ＢＲ
ｉｊはつきりとし九波状になって開口部に向ってａｎる
。It has also been found that if the resin is blown out from the transfer sluge nog tube 8 intermittently, reverse flow is less likely to occur near the opening 6' of the resin transfer tube. Water bubbles 5-50
If you do it intermittently like 15 to 60 seconds of rest, 8BR
ij forms a sharp nine-wave shape and anans toward the opening.
第２図乃至第５図に示す如く樹脂移送管の開口部６′の
周辺に８ＢＲが集まったら、弁７を開としＱｌ＋ Ｑ重
及び塔上部からの加圧水４又は加圧空気５を用いていつ
きに移送してしまう。When 8BR has gathered around the opening 6' of the resin transfer pipe as shown in Figs. 2 to 5, the valve 7 is opened and it is irrigated using the Ql + Q weight and pressurized water 4 or pressurized air 5 from the top of the tower. It will be transferred to.
以下本発明を復水脱塩装置の分離塔を例にして工程毎に
詳しく説明する。Hereinafter, the present invention will be explained in detail for each step using a separation column of a condensate desalination apparatus as an example.
第６図は本発明の実施態様の一例を示す説明図である。FIG. 6 is an explanatory diagram showing an example of an embodiment of the present invention.
脱塩塔（図示せず）から移送されてき次混合樹脂を分離
塔において逆洗水流入弁９逆洗排水弁１０を開とし、Ｌ
Ｖ８〜１０ ｒｎ ７時で十分逆洗分離全行う。沈静後
スルージング水弁１１を開とし、Ｌ Ｖ ｎ ７〜１．
５ ｍ ７時でスルージング水を導入し、かつ塔上部の
加圧水弁１２樹脂移送管６の弁７を開とし升９．１０は
閉として大部分の８ＢＲ２ｔ−アニオン再生塔（図示せ
ず）に移送する。The mixed resin transferred from the demineralization tower (not shown) is transferred to the separation tower, with the backwash water inlet valve 9 and the backwash drain valve 10 open, and the L
V8-10 rn Complete backwash separation at 7 o'clock. After settling down, open the sluicing water valve 11 and set L V n 7 to 1.
5 m At 7 o'clock, sluicing water was introduced, and the pressurized water valve 12 at the top of the tower opened the valve 7 of the resin transfer pipe 6. Cells 9 and 10 were closed, and the main part of the 8BR2t-anion regeneration tower (not shown) was Transport.
スルージング水流速會Ｌｖα７〜１．５ ｍ ７時と小
さくすると、ＢＡＲ層はほとんど実質的に流動せずＳＢ
Ｒ層のみが若干流動している。このような移送を行うと
樹脂面は移送用スルージング管側から開口部側に向けて
傾斜しているが、均一にし次とすると第７図に示す如く
開口部６′はＢＡＲ層内に入っている状態となる位置に
ある。Sluicing water flow velocity Lvα 7 to 1.5 m If it is as low as 7 o'clock, the BAR layer will hardly flow and the SB
Only the R layer is slightly fluid. When such a transfer is performed, the resin surface is inclined from the transfer sluicing pipe side to the opening side, but if it is made uniform, the opening 6' will enter the BAR layer as shown in FIG. It is in a position where it is in a state of being.
スルージング水の流速を大きくするとその分ＢＡＲ層の
逆洗展開率が大きくなジ、アニオン再生塔へ移送される
８ＡＲが多くなり第７図に示す開口部６′と表層表面と
の距ＦＩＩ ／、’が小さくなり残留し九日ＢＲ２の完
全な移送には好ましくない。When the flow rate of the sluicing water is increased, the backwash development rate of the BAR layer increases accordingly, and more 8AR is transferred to the anion regeneration tower, resulting in the distance FII / between the opening 6' and the surface layer surface shown in FIG. ,' become small and remain, which is not preferable for complete transfer of 9-day BR2.
次いで逆洗水排水弁１０、低流速逆洗弁１３全開とし、
他の弁は閉とじＬＶ五５〜４．５ ｍ ７時で日ＡＲ１
ｉ’ｉ流動状態とする。そして本発明の方法によって残
留ＥＩＢＲ’ｉ移送する。低流速逆洗弁１３の開度は水
温等を考慮し常に一定のＢＡＲＯ展ｙ＊率となるように
コントロールすることが重要である。Next, the backwash water drain valve 10 and the low flow backwash valve 13 are fully opened,
Other valves are closed LV 55-4.5 m Day AR1 at 7 o'clock
i'i Let it be in a fluid state. The residual EIBR'i is then transferred by the method of the invention. It is important to control the opening degree of the low flow rate backwash valve 13 so that a constant BARO expansion y* rate is maintained in consideration of water temperature, etc.
次いで移送用スルージング水弁１４ｔ−開としＬＶα５
〜２ｍ／時で移送用スルージング水を導入し、上部に向
って吹き出させる。すると前述の如く吹き出し部の上部
の樹脂層が盛り上が９、第２図乃至第５図に示す如き８
ＢＨの流れができしだいに開口部に集まっていく。この
工程はＣＬ５〜２分程度でよい。次いで弁７，１３゜１
４を開とし、その個の弁は閉として移送管開口部６′の
まわりに集められ７’ｊ ８ＢＲ２’を移送してしまう
。Next, the transfer sluicing water valve 14t is opened and LVα5
Transfer sluicing water is introduced at ~2 m/h and blown towards the top. Then, as mentioned above, the resin layer at the top of the blowout part bulges 9, and as shown in FIGS. 2 to 5, 8.
As soon as the BH flows, it gradually gathers at the opening. This step may take about CL5 to 2 minutes. Then valve 7,13゜1
4 is open and its respective valve is closed and collected around the transfer tube opening 6', transferring 7'j 8BR2'.
移送用スルージング水は連続的に吹き出してもよいが流
速が大きいと基壇にぶつかって反転流が生じ８ＢＲが集
まりにくいことがあり、この危険を避ける九め吹き出し
を間けつ的に行うのが好ましい。The sluicing water for transfer may be blown out continuously, but if the flow velocity is high, it may collide with the pedestal and cause a reverse flow, making it difficult for 8BR to collect, so it is preferable to blow out the water intermittently to avoid this danger. .
吹き出し５〜３０秒、休止１５〜６０秒と間けつ的に吹
き出すとＩ、 Ｖ １．５〜２．５ｍ／時と流量を大き
くしても第２図乃至第５図に示す状態を容易に達成でき
る。このような移送を数回くり返すことによジ残留ＳＢ
Ｒは完全にアニオン再生塔に移送されてしまう。If the air is blown out intermittently with 5 to 30 seconds of air and a pause of 15 to 60 seconds, the conditions shown in Figures 2 to 5 can be easily achieved even if the flow rate is increased to 1.5 to 2.5 m/hour. It can be achieved. By repeating such transfer several times, residual SB
R is completely transferred to the anion regeneration tower.
くり返す工程１ｉ−まとめると下記の如くである。The process of repeating step 1i is summarized as follows.
開状態の升Ａ 時間
逆洗分離 ９，１０ ３〜５分移送（
１）（あつめる工程）１０，１３，１４ １〜２分移
送（２）（移送） ７，１２，１３，１４ １〜２分
なお、移送（１）及び（２）は同時にすることもできる
。Cell A in open state Time backwash separation 9,10 3-5 minutes transfer (
1) (Gathering process) 10, 13, 14 1 to 2 minutes Transfer (2) (Transfer) 7, 12, 13, 14 1 to 2 minutes Note that transfers (1) and (2) can also be performed at the same time.
以下に本発明の効果を明確にするために比較例並びに実
施例を記載する。Comparative examples and examples will be described below to clarify the effects of the present invention.
比較例１
内径１８００φ、高さ５０００■の分離塔に８ＡＲとし
てＤｏｗｅｘ ＴＧ６５００（登録商標） ４５００Ｌ
１ 日ＢＲとしてＤｏｗｅｘ ＴＧ５５０Ａ（登録商標
）２０００ｔの混合樹脂を光てんし塔下部から逆洗水ｉ
ＬＶ１０ｍ／時で導入し樹脂を２層に分離した。ついで
塔下部からのスルージング水をＬＶ２．５ｍ／時で導入
し、同時に塔上部から加圧水ｆ Ｌ １４ ｍ ７時で
導入し８８Ｒ’ｉ再生塔に移送し次。樹脂移送管の開口
部は塔中６軸の１ケ所とし、７５φのものを用いた。又
その位置は樹脂境界面から１００ｍ下部に設けた。移送
後残留し九ＳＢＲは全ＳＢＲのα５〜ａ６％であっ次。Comparative Example 1 Dowex TG6500 (registered trademark) 4500L as 8AR in a separation column with an inner diameter of 1800φ and a height of 5000mm
1 As a day BR, 2000 tons of Dowex TG550A (registered trademark) mixed resin was backwashed from the lower part of the optical fiber tower.
The resin was introduced at a LV of 10 m/hour to separate into two layers. Next, sluging water was introduced from the lower part of the tower at a LV of 2.5 m/hour, and at the same time pressurized water f L 14 m was introduced from the upper part of the tower at 7 o'clock and transferred to the 88R'i regeneration tower. The resin transfer pipe had one opening on each of the six axes in the column, and had a diameter of 75φ. Further, the position was set 100 m below the resin boundary surface. The nine SBRs remaining after the transfer are α5~a6% of the total SBR.
残留ＢＢＲの調査方法
移送後Ｌｖ１ｏｍ／時で４０分間逆洗後、表層にあつま
つ九ＳＢＲｔ−すべてかきと９体積を測定し次。Investigation method for residual BBR After transfer, backwash at Lv1om/hour for 40 minutes, measure the volume of all the 9SBRt collected on the surface layer.
実施例１
比較例１と同一の大きさの塔を用い次。樹脂を比較例１
と同様に２層に分離し友後、塔下部からのスルージング
水ｆ Ｌ Ｖ ？、 ２ ｍ ７時、塔上部からの加圧
水Ｌ ”Ｉ ４ ｍ ７時で導入しＳＢＨの大部分を移
送し、次いで残留８ＢＨの移送を行つ次。Example 1 The following was carried out using a column of the same size as in Comparative Example 1. Comparative example 1 of resin
After separating into two layers in the same manner as above, the sluicing water from the bottom of the column f L V ? , 2 m At 7 o'clock, pressurized water L''I from the top of the column was introduced at 7 o'clock to transfer most of the SBH, and then the remaining 8 BH was transferred.
樹脂移送管開口部は第２図及び第３図に示す構成とし、
他の条件は比較例１と同じである。The resin transfer pipe opening has the configuration shown in FIGS. 2 and 3,
Other conditions are the same as in Comparative Example 1.
く残留１３ＢＨの移送〉
低流速逆洗水ｔ−Ｌ Ｖ ４ ｍ ７時で導入し、ＢＡ
Ｒを流動状態とし次。更に樹脂分離面の４５０ｍ下に股
は几移送用スルージング水管から水の吹き出しｆ Ｌ
１１ ｍ ７時で連続的に１分間行い、ついで移送を１
分間、Ｌ Ｖ ５ ｍ ７時の逆洗分離を５分間行い、
これらのくり返しを３回行つ之。Transfer of residual 13BH> Low-flow backwash water t-L V 4 m Introduced at 7 o'clock, BA
Let R be a fluid state and then. Furthermore, 450m below the resin separation surface, water is blown out from the sluicing water pipe for transporting the pipe.
11 m Continuously perform for 1 minute at 7 o'clock, then transfer for 1 minute.
backwash separation at 7 o'clock for 5 minutes,
Repeat these steps three times.
くり返し後前記移送工程のみを１０分間行っ友。After repeating the process, repeat the transfer process for 10 minutes.
残留しｆ／−ＢＢＲｆｆ、全ＢＢＲ（ＤαＤ２〜［１０
３５％であつｔｏ
実施例２
実施例１の中で移送用スルージング水の吹き出しを１５
秒休体′１に１５秒とかんけっ的に行った。他の条件は
実施例１と同じである。Residual f/-BBRff, total BBR (DαD2~[10
35% to Example 2 In Example 1, the sluicing water for transfer was 15%.
I went to the second rest '1 for 15 seconds. Other conditions are the same as in Example 1.
残留シフｔｊＥＩＢＲは全８ＢＲの（１０１５〜［１０
２５慢であった。The residual shift tjEIBR is (1015~[10
25 He was arrogant.
実施例３ 実施例１と同じ方法で光てん樹脂を下記の構成とし次。Example 3 Using the same method as in Example 1, the Koten resin was made into the following composition.
Ｄｏｗｅｘ ＨＧ Ｒ−Ｗ ２
Ｄｏｗｅｘ ＴＧ ５５０ム
残留したＳＤＲは全ＳＢＲのα０２〜α０３５チであり
尺。Dowex HG R-W 2 Dowex TG 550 μm The remaining SDR is α02 to α035 of the total SBR.
以上述べ次如く本発明法によればＢＡＲ中に残留するＥ
ＩＢＲは従来法のπ〜πに減少できる。As stated above, according to the method of the present invention, E remaining in BAR
The IBR can be reduced from π to π of the conventional method.
それ故、生成するＲ−ＯＡ （塩素型アニオン樹脂）の
ｉｔｋ少なくでき処理水質が大きく向上し比。Therefore, the amount of R-OA (chlorine type anion resin) produced can be reduced, and the quality of treated water can be greatly improved.
第１因は本発明方法を説明するためのイオノ父換樹脂の
分離装置の一例の縦断面図、第２図は第１図のムーＡ線
における横断面図、第５図は第１図の移送用スルージ７
グＷ８の作用を説明する次めの樹脂境界部分の一部縦断
面図、第４図は第１図乃至第３図と異なる形の移送用ス
ルージング管を設けた装置の第１図Ａ−Ａ線における断
面図、第５図は同スルージング管の作用を説明する之め
の樹脂境界部分の一部縦断面図、第６図は本発明の一実
施例を説明するための装置の縦断面図、第７図は同樹脂
境界部分の一部断面を示し、第８図は従来例全説明する
友めの装置の縦断面図、第９図は同樹脂境界部分の一部
縦断面図を示す。
１−−− ＢＡＲ層、２−−− ＳＢＲ層、３・・・ス
ルージング水導入管、４・・・加圧水導入管、５・・・
加圧空ｆｉ導入管、６・・・樹脂移送管、７・・・樹脂
移送弁、８・・・移送用スルージング管、９・・・逆洗
水流入弁、１ｏ・・・逆洗排水弁、１１・・・スルージ
ング水升、１２・・・加圧水弁、１３・・・低流速逆洗
弁、１４・・・移送用スルージング水弁
特許出願人 荏原インフィルコ株式会社同
株式会社 荏原製作所
向 荏原総合研死所
代 理 人 中 本 宏同
井 上 昭
同 吉 嶺 桂
第１図
第２図 第３図
第４図 第５図
す１
第６図The first factor is a longitudinal cross-sectional view of an example of an ionophore conversion resin separation apparatus for explaining the method of the present invention, FIG. 2 is a cross-sectional view taken along the Mu A line in FIG. 1, and FIG. Transfer sluge 7
The next partial vertical cross-sectional view of the resin boundary part explaining the action of the plug W8, FIG. A cross-sectional view taken along line A, FIG. 5 is a partial vertical cross-sectional view of the resin boundary portion for explaining the action of the sluging tube, and FIG. 6 is a vertical cross-sectional view of the device for explaining an embodiment of the present invention. 7 is a partial cross-sectional view of the resin boundary portion, FIG. 8 is a vertical cross-sectional view of a companion device to fully explain the conventional example, and FIG. 9 is a partial longitudinal cross-sectional view of the resin boundary portion. shows. 1--- BAR layer, 2--- SBR layer, 3... sluicing water introduction pipe, 4... pressurized water introduction pipe, 5...
Pressurized air fi introduction pipe, 6...Resin transfer pipe, 7...Resin transfer valve, 8...Transfer sluicing pipe, 9...Backwash water inflow valve, 1o...Backwash drain valve , 11...Sluging water tank, 12...Pressurized water valve, 13...Low flow rate backwash valve, 14...Sluging water valve for transfer Patent applicant: Ebara Infilco Co., Ltd.
For Ebara Corporation, Ebara Research Institute Mortuary Representative Hiroto Nakamoto
Shodo Inoue Yoshimine Katsura Figure 1 Figure 2 Figure 3 Figure 4 Figure 5 S1 Figure 6
Claims (1)
において逆洗によつてイオン交換樹脂を２層に分離した
後塔上部から加圧水又は加圧空気を、塔下部からスルー
ジング水を導入して大部分の比重の小さいイオン交換樹
脂を樹脂移送管により移送し、該移送後に、比重の大き
いイオン交換樹脂層上に残留している少量の比重の小さ
いイオン交換樹脂を更に分離する方法において、比重の
大きいイオン交換樹脂を流動状態に保ちながら、塔の片
側から塔壁に沿つて設けた水吹き出し部から水を吹き出
し、該水の吹き出し部の反対側の塔壁近くに設けた樹脂
移送管の開口部に向う比重の小さいイオン交換樹脂の流
れを起し、該イオン交換樹脂を樹脂移送管の開口部に集
めながら、又は集めた後該開口部から比重の小さいイオ
ン交換樹脂を抜き出して移送することを特徴とするイオ
ン交換樹脂の分離移送方法。 ２、前記水の吹き出し部を樹脂の表層より下部に設け、
且つ水を上方向に吹き出すようにした特許請求の範囲第
１項記載のイオン交換樹脂の分離移送方法。 ３、水の吹き出しを間けつ的に行う特許請求の範囲第１
項又は第２項記載のイオン交換樹脂の分離移送方法。[Claims] 1. After separating the ion exchange resin into two layers by backwashing in a column filled with two types of ion exchange resins with different specific gravity, pressurized water or pressurized air is supplied from the upper part of the column and from the lower part of the column. Sluicing water is introduced to transfer most of the ion exchange resin with low specific gravity through the resin transfer pipe, and after the transfer, a small amount of ion exchange resin with low specific gravity remaining on the ion exchange resin layer with high specific gravity is removed. In a method for further separation, water is blown from one side of the tower from a water outlet provided along the tower wall while keeping the ion exchange resin with a large specific gravity in a fluidized state, and then the water is blown out from a water outlet provided along the column wall from one side of the tower, and the water is blown out from a water outlet near the column wall on the opposite side of the water outlet. The ion exchange resin with a low specific gravity is caused to flow toward the opening of the resin transfer tube provided in the resin transfer tube, and the ion exchange resin with a low specific gravity is collected at the opening of the resin transfer tube, or after the ion exchange resin is collected, the ions with a low specific gravity are transferred from the opening. A method for separating and transporting ion exchange resin, which comprises extracting and transporting the exchange resin. 2. The water blowing part is provided below the surface layer of the resin,
A method for separating and transferring an ion exchange resin according to claim 1, wherein the water is blown upward. 3. Claim 1 in which water is spouted intermittently
A method for separating and transferring an ion exchange resin according to item 1 or 2.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61253775A JPH0661466B2 (en) | 1986-10-27 | 1986-10-27 | Separation and transfer method of ion exchange resin |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61253775A JPH0661466B2 (en) | 1986-10-27 | 1986-10-27 | Separation and transfer method of ion exchange resin |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS63107754A true JPS63107754A (en) | 1988-05-12 |
| JPH0661466B2 JPH0661466B2 (en) | 1994-08-17 |
Family
ID=17255971
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61253775A Expired - Lifetime JPH0661466B2 (en) | 1986-10-27 | 1986-10-27 | Separation and transfer method of ion exchange resin |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0661466B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10202119A (en) * | 1997-01-28 | 1998-08-04 | Kurita Water Ind Ltd | Mixed-bed type ion-exchange resin tower |
| CN115739208A (en) * | 2022-12-12 | 2023-03-07 | 河南海之德高新环保科技有限公司 | Temporary storage collecting device for resin extraction and collecting method thereof |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3034911U (en) * | 1996-08-20 | 1997-03-07 | 淑霞 黄陳 | Electric tool |
-
1986
- 1986-10-27 JP JP61253775A patent/JPH0661466B2/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10202119A (en) * | 1997-01-28 | 1998-08-04 | Kurita Water Ind Ltd | Mixed-bed type ion-exchange resin tower |
| JP4502084B2 (en) * | 1997-01-28 | 2010-07-14 | 栗田工業株式会社 | Mixed bed type ion exchange resin tower and method for forming the mixed bed |
| CN115739208A (en) * | 2022-12-12 | 2023-03-07 | 河南海之德高新环保科技有限公司 | Temporary storage collecting device for resin extraction and collecting method thereof |
| CN115739208B (en) * | 2022-12-12 | 2024-02-20 | 河南海之德高新环保科技有限公司 | Temporary storage and collection device for resin extraction and collection method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0661466B2 (en) | 1994-08-17 |
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