JPH04300652A - Removal of ion by ion exchanger - Google Patents
Removal of ion by ion exchangerInfo
- Publication number
- JPH04300652A JPH04300652A JP3092931A JP9293191A JPH04300652A JP H04300652 A JPH04300652 A JP H04300652A JP 3092931 A JP3092931 A JP 3092931A JP 9293191 A JP9293191 A JP 9293191A JP H04300652 A JPH04300652 A JP H04300652A
- Authority
- JP
- Japan
- Prior art keywords
- adsorbing
- ion
- ion exchanger
- ions
- adsorption
- 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.)
- Pending
Links
- 150000002500 ions Chemical class 0.000 claims abstract description 88
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 239000002002 slurry Substances 0.000 claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 5
- 238000001179 sorption measurement Methods 0.000 claims description 45
- 238000003795 desorption Methods 0.000 claims description 41
- 238000000034 method Methods 0.000 claims description 12
- 238000000926 separation method Methods 0.000 abstract description 9
- 239000000706 filtrate Substances 0.000 abstract description 7
- 238000003756 stirring Methods 0.000 abstract description 4
- 239000007864 aqueous solution Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 abstract 3
- 239000007787 solid Substances 0.000 abstract 1
- 238000005342 ion exchange Methods 0.000 description 8
- 239000002245 particle Substances 0.000 description 8
- 239000002253 acid Substances 0.000 description 7
- 239000003513 alkali Substances 0.000 description 6
- 230000000717 retained effect Effects 0.000 description 4
- 238000007086 side reaction Methods 0.000 description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 2
- 150000001450 anions Chemical class 0.000 description 2
- 150000001767 cationic compounds Chemical class 0.000 description 2
- 238000004090 dissolution Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229910001411 inorganic cation Inorganic materials 0.000 description 2
- 150000002892 organic cations Chemical class 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 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 description 1
- IVORCBKUUYGUOL-UHFFFAOYSA-N 1-ethynyl-2,4-dimethoxybenzene Chemical compound COC1=CC=C(C#C)C(OC)=C1 IVORCBKUUYGUOL-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000000382 dechlorinating effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005868 electrolysis reaction Methods 0.000 description 1
- 229910001412 inorganic anion Inorganic materials 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 239000003014 ion exchange membrane Substances 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
Landscapes
- Treatment Of Water By Ion Exchange (AREA)
Abstract
Description
【０００１】0001
【産業上の利用分野】本発明は、イオン交換体を用い水
性液からある種のイオンを経済的に且つ効率良く除去す
る方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for economically and efficiently removing certain ions from an aqueous liquid using an ion exchanger.
【０００２】0002
【従来の技術】水性液中のある種のイオンをイオン交換
体を用いて除去する方法においては、イオン交換体を繰
り返し使用するために吸着と脱着の操作を交互に行う必
要がある。この操作を行う場合、従来はイオン交換体を
塔に充填して使用するいわゆる充填塔方式が採用されて
きた。しかし、充填塔方式には以下に述べる欠点がある
。すなわち、イオン交換体が球状のイオン交換樹脂のよ
うな形状ではなく特殊な形状や粒子径が小さい場合に充
填塔方式を採用すると、イオン交換体充填部の通液部に
おける圧力損失が大きいので、水性液の必要量を流すこ
とが経済的に困難になる。さらに、吸着又は脱着のイオ
ン交換反応に酸又はアルカリを使用する場合は、イオン
交換体充填部は低いｐＨ又は高いｐＨの水性液と直接接
触することになり、イオン交換体の一部が溶失したり、
イオン交換体と酸又はアルカリとの副反応が起こるとい
った経済的に不都合な問題が生じる。2. Description of the Related Art In a method for removing certain ions from an aqueous liquid using an ion exchanger, it is necessary to perform adsorption and desorption operations alternately in order to use the ion exchanger repeatedly. When performing this operation, a so-called packed column system has conventionally been adopted in which a column is filled with an ion exchanger. However, the packed column system has the following drawbacks. In other words, if the packed column method is adopted when the ion exchanger is not shaped like a spherical ion exchange resin but has a special shape or a small particle size, the pressure loss in the liquid passage section of the ion exchanger packed section will be large. It becomes economically difficult to flow the required amount of aqueous liquid. Furthermore, when acids or alkalis are used in ion exchange reactions for adsorption or desorption, the ion exchanger packing comes into direct contact with aqueous liquids of low or high pH, causing some of the ion exchanger to dissolve. or
Economically disadvantageous problems arise, such as side reactions between the ion exchanger and the acid or alkali.
【０００３】0003
【発明が解決しようとする課題】本発明は上記実情に鑑
み、経済的で効率の良いイオン除去方法を提供すること
を目的とする。SUMMARY OF THE INVENTION In view of the above circumstances, it is an object of the present invention to provide an economical and efficient ion removal method.
【０００４】0004
【課題を解決するための手段】本発明者らは上記目的を
達成せんとして鋭意研究を重ねた結果、本発明を完成す
るに至った。すなわち、本発明は、イオン交換体を使用
してイオンを含有する水性液から該イオンを吸着除去す
るに際し、吸着反応槽に水性液とイオン交換体とを供給
し水性液中のイオンをイオン交換体に吸着させ、該イオ
ンを吸着したイオン交換体を含有する吸着スラリーを吸
着反応槽から取り出して吸着側分離機に供給し該イオン
を吸着したイオン交換体からなる吸着ケーキを吸着スラ
リーから分離し、吸着ケーキと吸着ケーキから該イオン
を脱着する成分と純水からなる脱着液とを脱着反応槽に
送り吸着ケーキから該イオンを脱着させ、該イオンを脱
着したイオン交換体を含有する脱着スラリーを脱着反応
槽から取り出して脱着側分離機に供給しイオン交換体か
らなる脱着ケーキを脱着スラリーから分離し、該脱着ケ
ーキを吸着反応槽に戻して循環使用することを特徴とす
るイオンの吸着除去方法を内容とする。[Means for Solving the Problems] The present inventors have conducted extensive research to achieve the above object, and as a result, have completed the present invention. That is, in the present invention, when adsorbing and removing ions from an aqueous liquid containing ions using an ion exchanger, the aqueous liquid and the ion exchanger are supplied to an adsorption reaction tank, and the ions in the aqueous liquid are ion-exchanged. The adsorption slurry containing the ion exchanger that has adsorbed the ions is taken out from the adsorption reaction tank and supplied to the adsorption side separator, and the adsorption cake consisting of the ion exchanger that has adsorbed the ions is separated from the adsorption slurry. , a desorption liquid consisting of an adsorption cake and a component for desorbing the ions from the adsorption cake and pure water is sent to a desorption reaction tank to desorb the ions from the adsorption cake, and a desorption slurry containing the ion exchanger from which the ions have been desorbed is produced. A method for adsorption and removal of ions, which comprises taking the desorption cake out of the desorption reaction tank and feeding it to a desorption side separator to separate a desorption cake made of an ion exchanger from the desorption slurry, and returning the desorption cake to the adsorption reaction tank for circulation use. The content is
【０００５】本発明を図面に基づいて説明する。図１は
本発明の実施態様の一例を示すもので、吸着反応槽１に
は主としてイオン交換体からなる脱着ケーキ８と、イオ
ン交換されるべきイオンを含む水性液１１が連続的に供
給される。吸着反応槽１は攪拌状態に保たれ、イオン交
換体はスラリー状態でイオン交換反応を起こし該イオン
を吸着する。この吸着スラリー５はポンプによって連続
的に吸着側分離機３に供給され固液分離される。吸着濾
液９は系外に排出され、主としてイオンを吸着したイオ
ン交換体からなる吸着ケーキ７は脱着反応槽２に供給さ
れる。脱着反応槽２には該吸着ケーキ７と共にイオン交
換体から該イオンを脱着する成分と純水からなる脱着液
１２が連続的に供給される。脱着反応槽２は攪拌状態に
保たれ、イオン交換体はスラリー状態でイオン交換反応
を起こし該イオンを脱着する。この脱着スラリー６はボ
ンプによって連続的に脱着側分離機４に供給され固液分
離される。該イオンを含む脱着濾液１０は系外に排出さ
れ、主としてイオン交換体からなる脱着ケーキ８は吸着
反応槽１に供給される。本実施態様のごとく、吸着・脱
着及びスラリーの固液分離の操作が連続的に実施し得る
ことが本発明の利点の一つである。The present invention will be explained based on the drawings. FIG. 1 shows an example of an embodiment of the present invention, in which an adsorption reaction tank 1 is continuously supplied with a desorption cake 8 mainly composed of an ion exchanger and an aqueous liquid 11 containing ions to be ion-exchanged. . The adsorption reaction tank 1 is kept in an agitated state, and the ion exchanger causes an ion exchange reaction in a slurry state and adsorbs the ions. This adsorption slurry 5 is continuously supplied to the adsorption side separator 3 by a pump and subjected to solid-liquid separation. The adsorption filtrate 9 is discharged to the outside of the system, and the adsorption cake 7 mainly composed of an ion exchanger adsorbing ions is supplied to the desorption reaction tank 2. The desorption reaction tank 2 is continuously supplied with the adsorption cake 7 as well as a desorption liquid 12 consisting of a component for desorbing the ions from the ion exchanger and pure water. The desorption reaction tank 2 is maintained in an agitated state, and the ion exchanger causes an ion exchange reaction in a slurry state to desorb the ions. This desorption slurry 6 is continuously supplied to the desorption side separator 4 by a pump and subjected to solid-liquid separation. The desorption filtrate 10 containing the ions is discharged to the outside of the system, and the desorption cake 8 mainly consisting of an ion exchanger is supplied to the adsorption reaction tank 1. One of the advantages of the present invention is that the operations of adsorption/desorption and solid-liquid separation of the slurry can be performed continuously as in this embodiment.
【０００６】本発明でいう水性液とは、ある種のイオン
を含有する有機塩、有機物、無機塩、或いは無機物の水
溶液をいい、ある種のイオンとは、水性液からイオン交
換反応を利用して除去するあらゆる種類の有機や無機の
陽イオン又は陰イオンをいい特に限定されない。[0006] The aqueous liquid as used in the present invention refers to an aqueous solution of an organic salt, an organic substance, an inorganic salt, or an inorganic substance containing a certain kind of ion. It refers to all kinds of organic or inorganic cations or anions that are removed by the process, but is not particularly limited.
【０００７】本発明において用いられるイオン交換体は
、有機又は無機の陽イオン交換体又は陰イオン交換体で
あり特に限定されず、またその形状は球形、非定形、繊
維状、鱗片状等特に限定されないが、粒子径（ストーク
ス径）は１μｍ以上が好ましく、５μｍ以上が更に好ま
しい。粒子径が１μｍより小さい場合は固液分離の分離
効率が低く、またイオン交換体の系外への損失が大きく
経済的でない。しかし、本発明においては充填塔方式で
は経済的に使用できないような小粒子径のものを使用で
き、これは充填塔方式では使用できない特殊な形状のも
のも使用できることと相まって、本発明の利点の一つで
ある。The ion exchanger used in the present invention is an organic or inorganic cation exchanger or anion exchanger, and is not particularly limited, and its shape is particularly limited, such as spherical, amorphous, fibrous, and scaly. However, the particle diameter (Stokes diameter) is preferably 1 μm or more, more preferably 5 μm or more. When the particle size is smaller than 1 μm, the separation efficiency of solid-liquid separation is low, and the loss of the ion exchanger to the outside of the system is large, making it uneconomical. However, in the present invention, particles with small diameters that cannot be economically used in a packed column system can be used, and this, together with the ability to use particles with a special shape that cannot be used in a packed column system, is an advantage of the present invention. There is one.
【０００８】本発明において用いられるイオン交換体の
量は、処理対象のイオンの種類及び量、イオン交換体の
種類、イオン交換反応の条件（時間、温度、ｐＨ等）に
依存するので一概にはいえないが、吸着反応槽、脱着反
応槽のいずれの槽のスラリー濃度も５００ｇ／１以下で
あることが好ましい。スラリー濃度が５００ｇ／１より
高くなるとスラリーの取扱いが困難になり、系内で閉塞
トラブルといった不都合が生じることがある。本発明に
おいて吸着反応槽及び脱着反応槽のスラリーの保持量は
、それぞれのイオン交換反応速度（時間）により決定さ
れる。イオン交換反応が速い場合は保持量は少なく、イ
オン交換反応が遅い場合は保持量は多くなる。[0008] The amount of ion exchanger used in the present invention depends on the type and amount of ions to be treated, the type of ion exchanger, and the conditions of the ion exchange reaction (time, temperature, pH, etc.). However, it is preferable that the slurry concentration in both the adsorption reaction tank and the desorption reaction tank is 500 g/1 or less. When the slurry concentration is higher than 500 g/1, it becomes difficult to handle the slurry, and problems such as clogging problems may occur in the system. In the present invention, the amount of slurry retained in the adsorption reaction tank and the desorption reaction tank is determined by the respective ion exchange reaction rates (time). When the ion exchange reaction is fast, the amount retained is small, and when the ion exchange reaction is slow, the amount retained is large.
【０００９】吸着反応槽及び脱着反応槽の攪拌には、イ
オン交換体の形状等に応じて攪拌機による攪拌、ポンプ
による循環、空気などの気体を吹き込む方法等が用いら
れる。本発明において用いられる吸着側分離機又は脱着
側分離機の型式は特に限定されず、使用するイオン交換
体の形状等に応じて遠心分離機、吸引濾過器、加圧濾過
器等が用いられるが、連続運転により本発明を実施する
場合は連続型分離機が用いられる。分離ケーキである吸
着ケーキや脱着ケーキの脱着反応槽や吸着反応槽への移
送方法も特に限定されない。分離ケーキをベルトコンベ
アで移送してもよいし、分離機を反応槽の上に設置して
ケーキを反応槽に落下させてもよい。系外に排出される
吸着濾液あるいは脱着濾液に若干のイオン交換体が存在
し、その損失が見逃せない場合は、濾液を系外に排出す
る前に濾過精度の高い仕上げ濾過を行ってイオン交換体
を回収すればよい。[0009] For stirring the adsorption reaction tank and desorption reaction tank, methods such as stirring with a stirrer, circulation with a pump, and blowing in a gas such as air are used depending on the shape of the ion exchanger. The type of adsorption-side separator or desorption-side separator used in the present invention is not particularly limited, and centrifuges, suction filters, pressure filters, etc. may be used depending on the shape of the ion exchanger used. , a continuous separator is used when the present invention is carried out in continuous operation. The method for transferring the adsorption cake or desorption cake, which is the separation cake, to the desorption reaction tank or adsorption reaction tank is also not particularly limited. The separated cake may be transferred by a belt conveyor, or a separator may be installed above the reaction tank and the cake may be dropped into the reaction tank. If some ion exchanger is present in the adsorption filtrate or desorption filtrate discharged outside the system, and the loss cannot be overlooked, perform a final filtration with high filtration accuracy to remove the ion exchanger before discharging the filtrate outside the system. All you have to do is collect it.
【００１０】本発明において吸着反応又は脱着反応に酸
又はアルカリが必要である場合は、吸着反応槽又は脱着
反応槽に酸又はアルカリを直接添加してもよいし、水性
液又は脱着液に予め添加しておいてもよい。本発明にお
いてはイオン交換体をスラリー状態で使用するため、ｐ
Ｈを制御しながら酸又はアルカリを添加することができ
るので、いずれの方法においても低いｐＨ又は高いｐＨ
によるイオン交換体の溶失やイオン交換体と酸又はアル
カリとの副反応を防止できる。In the present invention, if an acid or alkali is required for the adsorption reaction or desorption reaction, the acid or alkali may be added directly to the adsorption reaction tank or desorption reaction tank, or it may be added to the aqueous liquid or desorption liquid in advance. You can leave it as is. In the present invention, since the ion exchanger is used in a slurry state, p
Since acid or alkali can be added while controlling H, either method can be used at low or high pH.
It is possible to prevent the dissolution of the ion exchanger and side reactions between the ion exchanger and acid or alkali.
【００１１】[0011]
【実施例】以下、本発明を実施例に基づき更に具体的に
説明するが、本発明はこの実施例に限定されるものでは
ない。
実施例
イオン交換膜法電解工程から抜き出した淡塩水について
脱塩素を行った後、表１に示す条件で硫酸イオンを連続
的に除去した。イオン交換体として灼熱減量（４０℃で
１６時間乾燥し吸着水分を除いた後１０００℃で１時間
加熱し、加熱前後の重量変化量を加熱前の重量で除し、
パーセント表示したもの）が１６〜２４重量％、粒子径
が７〜８μｍの水酸化ジルコニウム約１．４ｔを系内に
保有させ、月間３６ｔの割合で硫酸イオンを除去できた
。EXAMPLES The present invention will be explained in more detail below based on Examples, but the present invention is not limited to these Examples. Example After dechlorinating the fresh salt water extracted from the ion-exchange membrane electrolysis process, sulfate ions were continuously removed under the conditions shown in Table 1. Loss on ignition as an ion exchanger (dry at 40°C for 16 hours to remove adsorbed moisture, then heat at 1000°C for 1 hour, divide the weight change before and after heating by the weight before heating,
Approximately 1.4 tons of zirconium hydroxide with a particle size of 7 to 8 μm and a particle size of 16 to 24% by weight (expressed as a percentage) was retained in the system, and sulfate ions could be removed at a rate of 36 tons per month.
【００１２】0012
【表１】[Table 1]
【００１３】[0013]
【発明の効果】本発明は、イオン交換体をスラリー状と
して吸着と再生を繰り返すことにより従来の充填塔方式
よりも経済的にイオン交換反応を実施できるという知見
に基づくものである。すなわち、本発明は従来の充填塔
方式と比べて単位時間に一定量のイオンを除去するのに
必要なイオン交換体の量が少なくてすむという利点があ
る。また、イオン交換体をスラリー状で取り扱うため、
従来は経済的な理由から使用できなかった特殊な形状や
小さな粒子径のイオン交換体も使用できることも利点の
一つである。さらに、反応槽にｐＨを制御しながら酸又
はアルカリを添加することができるので、低いｐＨ又は
高いｐＨの水性液との直接接触によるイオン交換体の溶
失や副反応を防止できることも経済的に極めて有利な点
である。The present invention is based on the knowledge that by repeating adsorption and regeneration of an ion exchanger in the form of a slurry, an ion exchange reaction can be carried out more economically than in the conventional packed column system. That is, the present invention has the advantage that the amount of ion exchanger required to remove a certain amount of ions per unit time is smaller than that of the conventional packed column system. In addition, since the ion exchanger is handled in slurry form,
Another advantage is that ion exchangers with special shapes and small particle sizes, which could not be used in the past due to economic reasons, can also be used. Furthermore, since acid or alkali can be added to the reaction tank while controlling the pH, it is also economically possible to prevent ion exchanger dissolution and side reactions due to direct contact with aqueous liquids of low or high pH. This is an extremely advantageous point.
【図１】本発明の実施態様の一例を示す工程図である。FIG. 1 is a process diagram showing an example of an embodiment of the present invention.
１ 吸着反応槽
２ 脱着反応槽
３ 吸着側分離機
４ 脱着側分離機
５ 吸着スラリー
６ 脱着スラリー
７ 吸着ケーキ
８ 脱着ケーキ1 Adsorption reaction tank
2 Desorption reaction tank 3 Adsorption side separator
4 Desorption side separator 5 Adsorption slurry
6 Desorption slurry 7 Adsorption cake
8 Desorption cake
Claims (1)
する水性液から該イオンを吸着除去するに際し、吸着反
応槽に水性液とイオン交換体とを供給し水性液中のイオ
ンをイオン交換体に吸着させ、該イオンを吸着したイオ
ン交換体を含有する吸着スラリーを吸着反応槽から取り
出して吸着側分離機に供給し該イオンを吸着したイオン
交換体からなる吸着ケーキを吸着スラリーから分離し、
吸着ケーキと吸着ケーキから該イオンを脱着する成分と
純水からなる脱着液とを脱着反応槽に送り吸着ケーキか
ら該イオンを脱着させ、該イオンを脱着したイオン交換
体を含有する脱着スラリーを脱着反応槽から取り出して
脱着側分離機に供給しイオン交換体からなる脱着ケーキ
を脱着スラリーから分離し、該脱着ケーキを吸着反応槽
に戻して循環使用することを特徴とするイオンの吸着除
去方法。Claim 1: When using an ion exchanger to adsorb and remove ions from an aqueous liquid containing ions, the aqueous liquid and the ion exchanger are supplied to an adsorption reaction tank, and the ions in the aqueous liquid are removed by the ion exchanger. An adsorption slurry containing an ion exchanger adsorbing the ions is taken out from the adsorption reaction tank and supplied to an adsorption separator to separate an adsorption cake consisting of the ion exchanger adsorbing the ions from the adsorption slurry,
A desorption solution consisting of an adsorption cake, a component that desorbs the ions from the adsorption cake, and pure water is sent to a desorption reaction tank to desorb the ions from the adsorption cake, and a desorption slurry containing the ion exchanger that has desorbed the ions is desorbed. A method for adsorption and removal of ions, which comprises taking the desorption cake out of the reaction tank and feeding it to a desorption side separator to separate a desorption cake made of an ion exchanger from the desorption slurry, and returning the desorption cake to the adsorption reaction tank for circulation use.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3092931A JPH04300652A (en) | 1991-03-29 | 1991-03-29 | Removal of ion by ion exchanger |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3092931A JPH04300652A (en) | 1991-03-29 | 1991-03-29 | Removal of ion by ion exchanger |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04300652A true JPH04300652A (en) | 1992-10-23 |
Family
ID=14068241
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3092931A Pending JPH04300652A (en) | 1991-03-29 | 1991-03-29 | Removal of ion by ion exchanger |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04300652A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0699628A2 (en) | 1994-08-30 | 1996-03-06 | CHLORINE ENGINEERS CORP., Ltd. | Brine treatment method |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5437083A (en) * | 1977-08-27 | 1979-03-19 | Kobe Steel Ltd | Method of activating selective ion exchanbe body |
| JPS5845705A (en) * | 1981-09-11 | 1983-03-17 | Mitsubishi Rayon Co Ltd | Enhancement of rate of adsorption of oxyacid to titanic acid |
-
1991
- 1991-03-29 JP JP3092931A patent/JPH04300652A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5437083A (en) * | 1977-08-27 | 1979-03-19 | Kobe Steel Ltd | Method of activating selective ion exchanbe body |
| JPS5845705A (en) * | 1981-09-11 | 1983-03-17 | Mitsubishi Rayon Co Ltd | Enhancement of rate of adsorption of oxyacid to titanic acid |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0699628A2 (en) | 1994-08-30 | 1996-03-06 | CHLORINE ENGINEERS CORP., Ltd. | Brine treatment method |
| US5578218A (en) * | 1994-08-30 | 1996-11-26 | Chlorine Engineers Corp., Ltd. | Brine treatment method |
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