JPH07171351A - Redesalting of concentrated drained water discharged from desulfurization process - Google Patents
Redesalting of concentrated drained water discharged from desulfurization processInfo
- Publication number
- JPH07171351A JPH07171351A JP5319825A JP31982593A JPH07171351A JP H07171351 A JPH07171351 A JP H07171351A JP 5319825 A JP5319825 A JP 5319825A JP 31982593 A JP31982593 A JP 31982593A JP H07171351 A JPH07171351 A JP H07171351A
- Authority
- JP
- Japan
- Prior art keywords
- water
- concentrated
- concentration
- desalting
- discharged
- 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
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、飲料水等の脱塩精製設
備から排出される濃縮排水を再脱塩して更に濃縮する方
法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for re-desalting concentrated wastewater discharged from a desalination and refining facility for drinking water or the like for further concentration.
【０００２】[0002]
【従来の技術】地下水、湖水、海水、河川水などは、飲
料水又は工業水として広く利用されているが、多かれ少
なかれ、食塩などの可溶性塩などとともに、硫酸カルシ
ウムなどの難溶性塩が含有されている。BACKGROUND ART Ground water, lake water, sea water, river water, etc. are widely used as drinking water or industrial water, but more or less contain soluble salts such as salt and poorly soluble salts such as calcium sulfate. ing.
【０００３】このため、塩濃度の高い水は、蒸留法、逆
浸透法、電気透析法等により脱塩精製した後、飲料水や
工業水に供されている。一方、上記脱塩精製設備により
排出される、濃縮された塩類を含む排水は、そのまま河
川や海に放流されている。For this reason, water having a high salt concentration is desalted and purified by a distillation method, a reverse osmosis method, an electrodialysis method or the like, and then supplied to drinking water or industrial water. On the other hand, the wastewater containing the concentrated salt discharged from the desalination and refining equipment is discharged as it is to a river or the sea.
【０００４】[0004]
【発明が解決しようとする課題】しかしながら、上記の
ような脱塩プロセスから排出される濃縮排水は、高濃度
の塩分を含むため、そのまま河川、湖等に放流すると、
それらの塩濃度を上昇させ、環境汚染を引き起こす虞れ
がある。したがって、上記濃縮排水は、下水配管を通し
て直接海に放流することが望まれるが、海から遠い地域
においては、数十ｋｍあるいは数百ｋｍも下水配管を通
さなければならず、排出設備費が増大するという問題が
あった。However, since the concentrated wastewater discharged from the desalination process as described above contains a high concentration of salt, if it is discharged directly to a river, lake, etc.,
There is a risk of increasing their salt concentration and causing environmental pollution. Therefore, it is desirable that the concentrated wastewater be discharged directly to the sea through the sewer pipe, but in the area far from the sea, it must be passed through the sewer pipe for several tens of kilometers or hundreds of kilometers, which increases the discharge facility cost. There was a problem of doing.
【０００５】また、上記濃縮排水を再脱塩して濃縮し、
濃縮排水量を少なくするとともに、その脱塩水は精製水
として利用することも考えられるが、前記のように、水
中には、硫酸カルシウムなどの難溶性塩が含有されてい
るため、これらが濃縮されることにより、電気透析膜に
沈析して目詰まりを起こし、運転ができなくなる。この
ため、難溶性塩が析出しない濃度に抑えながら電気透析
を行わなければならず、更に濃縮することは困難であっ
た。Further, the concentrated waste water is desalted and concentrated,
It is possible to reduce the amount of concentrated wastewater and use the demineralized water as purified water.However, as described above, since water contains poorly soluble salts such as calcium sulfate, these are concentrated. As a result, the electrodialysis membrane is deposited and clogged, and the operation cannot be performed. For this reason, electrodialysis must be performed while controlling the concentration so that the sparingly soluble salt does not precipitate, and further concentration is difficult.
【０００６】そこで、本発明の目的は、脱塩プロセスか
ら排出される濃縮排水を、難溶性塩の析出を防止しつつ
再脱塩して、更に高濃度に濃縮することができるように
した脱塩プロセスより排出される濃縮排水の再脱塩方法
を提供することにある。Therefore, an object of the present invention is to reconcentrate the concentrated wastewater discharged from the desalination process while preventing the precipitation of the hardly soluble salt, so that it can be concentrated to a higher concentration. It is to provide a method for re-desalinating concentrated wastewater discharged from a salt process.
【０００７】[0007]
【課題を解決するための手段】上記目的を達成するた
め、本発明による脱塩プロセスより排出される濃縮排水
の再脱塩方法は、脱塩プロセスより排出される濃縮排水
を、一価イオン選択透過膜を組み込んだ電気透析槽で透
析して再脱塩するに際して、前記電気透析槽の濃縮室へ
の供給水として、脱塩処理された水を使用することを特
徴とする。In order to achieve the above object, the method for re-desalinating concentrated wastewater discharged from a desalination process according to the present invention, selects concentrated monovalent ion from the concentrated wastewater discharged from the desalination process. When dialysis is performed in an electrodialysis tank incorporating a permeable membrane for re-desalting, desalted water is used as the water supplied to the concentration chamber of the electrodialysis tank.
【０００８】以下、本発明について更に詳細に説明す
る。本発明の処理対象とする脱塩プロセスより排出され
る濃縮排水は、地下水、湖水、海水、河川水などを飲料
水又は工業水として利用するために、蒸留法、逆浸透
法、電気透析法等により脱塩精製したときに排出され
る、濃縮された塩類を含む排水を意味する。The present invention will be described in more detail below. The concentrated wastewater discharged from the desalination process to be treated according to the present invention is a distillation method, a reverse osmosis method, an electrodialysis method, etc. for utilizing groundwater, lake water, seawater, river water, etc. as drinking water or industrial water. Means wastewater containing concentrated salts, which is discharged when desalinated and purified by
【０００９】本発明の方法では、一価陰イオン選択透過
膜と、陽イオン選択透過膜とを、電極間にそれぞれ複数
枚交互に配列し、希釈室と濃縮室とを交互に形成した電
気透析槽又は、一価陽イオン選択透過膜と、陰イオン選
択透過膜とを、電極間にそれぞれ複数枚交互に配列し、
稀釈室と濃縮室とを交互に形成した電気透析槽のいずれ
かが用いられる。In the method of the present invention, a monovalent anion-selective permeable membrane and a cation-selective permeable membrane are alternately arranged between electrodes, and electrodialysis is performed by alternately forming a diluting chamber and a concentrating chamber. A tank or a monovalent cation selective permeable membrane and an anion selective permeable membrane are alternately arranged between the electrodes,
Either an electrodialysis tank in which a diluting chamber and a concentrating chamber are alternately formed is used.
【００１０】一価陰イオン選択透過膜としては、好まし
くは、四級アンモニウム基を陰イオン交換基として有す
る陰イオン交換膜で、硝酸イオン、フッ素イオンなどの
一価陰イオンを、硫酸イオンなどの多価陰イオンに比べ
て選択的に透過させる性質を有するものが使用される。
また、一価陽イオン選択透過膜としては、スルホン酸基
を陽イオン交換基として有する陽イオン交換膜で、ナト
リウムイオン、カリウムイオンなどの一価陽イオンを、
カルシウムイオン、マグネシウムイオンなどの多価陽イ
オンに比べて選択的に透過させる性質を有するものが使
用される。これらの一価イオン選択透過膜において、一
価イオン／多価イオンの選択性は、好ましくは２倍以
上、特には５倍以上が適切である。イオン交換容量は
０．５〜１０ミリ当量／ｇ乾燥樹脂が好ましく、厚さは
５〜５００μｍが好ましい。これら一価イオン選択透過
膜は、均一系、不均一系のいずれも使用できるが、均一
系のものでスチレン−ジビニルベンゼン共重合体を母体
する膜が好ましく使用される。The monovalent anion selective permeation membrane is preferably an anion exchange membrane having a quaternary ammonium group as an anion exchange group, and monovalent anions such as nitrate ion and fluorine ion are converted into sulfate ion and the like. Those having the property of selectively permeating compared with polyvalent anions are used.
Further, the monovalent cation selective permeation membrane is a cation exchange membrane having a sulfonic acid group as a cation exchange group, and monovalent cations such as sodium ion and potassium ion,
Those having a property of selectively permeating compared with polyvalent cations such as calcium ions and magnesium ions are used. In these monovalent ion selective permeable membranes, the monovalent ion / multivalent ion selectivity is preferably 2 times or more, particularly 5 times or more. The ion exchange capacity is preferably 0.5 to 10 meq / g dry resin, and the thickness is preferably 5 to 500 μm. These monovalent ion selective permeation membranes may be either homogeneous or heterogeneous, and homogeneous membranes having a styrene-divinylbenzene copolymer as a matrix are preferably used.
【００１１】また、陽イオン選択透過膜としては、好ま
しくはスルホン酸基を陽イオン交換基とするもので、ま
た、陰イオン選択透過膜としては、四級アンモニウム基
を陰イオン交換基とするもので、いずれも一価イオンに
対して特に大きい選択透過性を有しないものが使用さ
れ、それらのイオン交換容量が０．５〜１０ミリ当量／
ｇ乾燥樹脂、厚さが５〜５００μｍのものが好ましい。
これらの陽又は陰の選択透過膜は、均一系、不均一系の
いずれも使用できるが、均一系のものでスチレン−ジビ
ニルベンゼン共重合体を母体する膜が好ましく使用さ
れ、必要に応じて、ポリオレフィン、ポリ塩化ビニル、
ポリエステルなどの織布又は不織布で補強されたものも
使用できる。Further, the cation selective permeable membrane preferably has a sulfonic acid group as a cation exchange group, and the anion selective permeable membrane has a quaternary ammonium group as an anion exchange group. However, none of them has particularly high selective permeability for monovalent ions, and their ion exchange capacities are 0.5 to 10 meq /
A dry resin having a thickness of 5 to 500 μm is preferable.
These positive or negative permselective membranes can be either homogeneous or heterogeneous, but homogeneous membranes having a styrene-divinylbenzene copolymer as a matrix are preferably used, and if necessary, Polyolefin, polyvinyl chloride,
Those reinforced with a woven or non-woven fabric such as polyester can also be used.
【００１２】上記一価陰イオン又は一価陽イオン選択透
過膜及び陽イオン又は陰イオン選択透過膜を、それぞれ
１０〜６００枚電極間に交互に配列して、希釈室及び濃
縮室を十分に形成した電気透析槽が好ましく用いられ
る。この組み立て構造は、特開昭５５−２４５３８号、
特公昭５１−４７６６３号などに開示された構造を適宜
採用することができるが、このうち締付型（フィルター
プレス型）装置が好ましく使用される。The monovalent anion or monovalent cation selective permeable membrane and the cation or anion selective permeable membrane are alternately arranged between 10 to 600 sheets of electrodes to sufficiently form a diluting chamber and a concentrating chamber. The electrodialysis tank described above is preferably used. This assembly structure is disclosed in JP-A-55-24538,
The structure disclosed in Japanese Examined Patent Publication No. 51-47663 and the like can be appropriately adopted, and of these, a tightening type (filter press type) device is preferably used.
【００１３】脱塩プロセスより排出される濃縮排水は、
上記電気透析槽の希釈室に、好ましくは５〜５０ｃｍ／
ｓｅｃで供給される。電気透析槽の濃縮室には、電気透
析槽の運転を開始すれば、順次希釈室から陽イオン及び
陰イオンが水の移動に伴って移行してくるが、少なくと
も当初は０．５〜５ｃｍ／ｓｅｃで水を供給する。電気
透析槽の両端部にある陽極及び陰極が収容されるそれぞ
れの陽極室及び陰極室には、常法に従って、適宜の電解
質水溶液が供給される。The concentrated wastewater discharged from the desalination process is
In the dilution chamber of the electrodialysis tank, preferably 5 to 50 cm /
It is supplied in sec. When the operation of the electrodialysis tank is started, the cations and anions move from the dilution room to the concentration room of the electrodialysis tank along with the movement of water, but at least initially 0.5 to 5 cm / Water is supplied in sec. Appropriate electrolyte aqueous solutions are supplied to the respective anode chambers and cathode chambers at both ends of the electrodialysis tank, which accommodate the anodes and cathodes, according to a conventional method.
【００１４】本発明の最大の特徴は、上記濃縮室への供
給水として、脱塩処理された水を使用することにある。
ここで、脱塩処理された水とは、例えばイオン交換樹脂
等を通して脱塩した水や、蒸留水や、あるいは上記脱塩
プロセスにより精製された水などを意味する。ただし、
別途脱塩設備を設ける必要がないという理由から、上記
脱塩プロセスにより精製された水を使用することが好ま
しい。The greatest feature of the present invention is that desalted water is used as the feed water to the concentrating chamber.
Here, the desalted water means, for example, water desalted through an ion exchange resin or the like, distilled water, or water purified by the desalting process. However,
It is preferable to use water purified by the desalting process, because it is not necessary to provide a separate desalting facility.
【００１５】こうして、電気透析槽にて限界電流密度以
下の、好ましくは０．１〜１０Ａ／ｄｍ2 の電流密度で
通電を行い、希釈室に供給される水の陰イオン及び陽イ
オンを、それぞれ陰イオン選択透過膜及び陽イオン選択
透過膜を通して濃縮室に移行させることにより脱塩を行
う。本発明では、この脱塩において、一価陰イオン又は
一価陽イオン選択透過膜を用いているため、例えばＳＯ
4 などの二価以上の多価陰イオン又はＣａなどの二価以
上の多価陽イオンが、好ましくは５０％以上、特には９
５％以上希釈室に保持され、硝酸イオン、亜硝酸イオン
などの一価の陰イオン又は、ナトリウムイオン、カリウ
ムイオンなどの一価の陽イオンのみが、ほぼ選択的に濃
縮室に移行する。In this way, electricity is supplied in the electrodialysis tank at a current density below the limit current density, preferably 0.1 to 10 A / dm 2 , and anions and cations of the water supplied to the dilution chamber are respectively supplied. Desalination is carried out by transferring to the concentration chamber through the anion selective permeable membrane and the cation selective permeable membrane. In the present invention, since a monovalent anion or monovalent cation selective permeable membrane is used in this desalting, for example, SO
A divalent or higher polyvalent anion such as 4 or a divalent or higher polyvalent cation such as Ca is preferably 50% or more, and particularly 9
The monovalent anion such as nitrate ion and nitrite ion, or the monovalent cation such as sodium ion and potassium ion is retained in the diluting chamber at 5% or more, and almost selectively migrates to the concentrating chamber.
【００１６】また、濃縮室に供給される水が、上記のよ
うに脱塩処理された水であるため、濃縮室では、難溶性
塩を形成する原因となる、硫酸イオン、リン酸イオンな
どの多価陰イオン又はカルシウム、マグネシウムなどの
多価陽イオンのいずれか一方のイオンの濃度が極めて低
く維持され、硫酸カルシウム、硫酸マグネシウムなどの
難溶性塩の電気透析膜への沈析が防止される。このた
め、従来の電気透析法に比べて、排水中に含まれる塩分
を更に高濃度に濃縮することが可能となる。Further, since the water supplied to the concentrating chamber is the water desalted as described above, in the concentrating chamber, the sulfate ion, the phosphate ion, etc., which cause formation of a sparingly soluble salt, are generated. The concentration of either one of polyvalent anions or polyvalent cations such as calcium and magnesium is maintained at an extremely low level, and the precipitation of sparingly soluble salts such as calcium sulfate and magnesium sulfate on the electrodialysis membrane is prevented. . Therefore, it becomes possible to concentrate the salt content in the waste water to a higher concentration than in the conventional electrodialysis method.
【００１７】更に、本発明の好ましい態様では、こうし
て得られた高濃度の濃縮水を蒸発乾固させる。これによ
って、濃縮水中に含まれる塩類を固形化して廃棄するこ
とが可能となり、下水配管等の排水設備費を大幅に軽減
させることができる。Further, in a preferred embodiment of the present invention, the high-concentration concentrated water thus obtained is evaporated to dryness. As a result, the salts contained in the concentrated water can be solidified and discarded, and the cost of drainage equipment such as sewer pipes can be significantly reduced.
【００１８】[0018]
【作用】本発明では、脱塩プロセスより排出される濃縮
排水を、一価陰イオン又は一価陽イオン選択透過膜を組
み込んだ電気透析槽で透析するので、それぞれＳＯ4 な
どの多価陰イオン又はＣａなどの多価陽イオンが希釈室
に保持され、硝酸イオン、亜硝酸イオンなどの一価の陰
イオン又はナトリウムなどの一価の陽イオンのみがほぼ
選択的に濃縮室に移行して濃縮される。また、電気透析
の際に濃縮室に供給される水も脱塩処理された水である
ため、濃縮室におけるＳＯ4 などの多価陰イオン又はＣ
ａなどの多価陽イオンの濃度は、極めて低く維持され
る。その結果、硫酸カルシウム、硫酸マグネシウムなど
の難溶性塩の電気透析膜への沈析が防止され、排水中に
含まれる塩分を更に高濃度に濃縮することが可能とな
る。In the present invention, the concentrated waste water discharged from the desalting process is dialyzed in an electrodialysis tank incorporating a monovalent anion or monovalent cation selective permeation membrane, and therefore, polyvalent anions such as SO 4 are used. Alternatively, polyvalent cations such as Ca are retained in the dilution chamber, and only monovalent anions such as nitrate ions and nitrite ions or monovalent cations such as sodium are almost selectively transferred to the concentration chamber and concentrated. To be done. In addition, since the water supplied to the concentration chamber during electrodialysis is also desalted water, polyvalent anions such as SO 4 or C in the concentration chamber are used.
The concentration of polyvalent cations such as a is kept very low. As a result, precipitation of sparingly soluble salts such as calcium sulfate and magnesium sulfate on the electrodialysis membrane is prevented, and the salt content in the waste water can be concentrated to a higher concentration.
【００１９】[0019]
【実施例】図１には、本発明の脱塩プロセスより排出さ
れる濃縮排水の再脱塩方法の一実施例が示されている。EXAMPLE FIG. 1 shows an example of a method for re-desalting concentrated waste water discharged from the desalination process of the present invention.
【００２０】ＴＤＳ（総溶解塩分、Total Dissolve Sol
id）１２００ｐｐｍの原水を、１０００ｍ3 ／日の量
で、逆浸透法からなる脱塩設備に供給した。その結果、
ＴＤＳ４００ｐｐｍの精製水が７００ｍ3 ／日の量で得
られ、ＴＤＳ３０６６ｐｐｍの濃縮排水が３００ｍ3 ／
日の量で排出された。TDS (Total Dissolve Sol
the raw water of the id) 1200ppm, in the amount of 1000m 3 / day, was fed to the desalination facility consisting of a reverse osmosis method. as a result,
Purified water with TDS of 400 ppm was obtained in an amount of 700 m 3 / day, and concentrated waste water with TDS of 3066 ppm was 300 m 3 / day.
Emitted in the amount of days.
【００２１】この濃縮排水を、一価陰イオン選択透過膜
を組み込んだ電気透析槽で透析し、再脱塩した。使用し
た電気透析槽は、旭硝子株式会社製、陽イオン交換膜、
商品名「セレミオンＣＭＶ」及び一価陰イオン選択透過
膜、商品名「セレミオンＡＭＶ」を３００対、を組込ん
だ旭硝子株式会社製の電気透析槽、商品名「ＤＷ−４型
槽」（膜面積０．８ｍ2 ）である。電気透析槽に供給さ
れた直流電流は５０Ａ、電圧は２００Ｖであった。The concentrated waste water was dialyzed in an electrodialysis tank incorporating a monovalent anion selective permeable membrane, and desalted again. The electrodialysis tank used was a cation exchange membrane manufactured by Asahi Glass Co., Ltd.
An electrodialysis tank manufactured by Asahi Glass Co., Ltd. incorporating a trade name "Selemion CMV" and a monovalent anion selective permeable membrane, and a trade name "Selemion AMV" 300 pairs, a trade name "DW-4 type tank" (membrane area 0.8 m 2 ). The direct current supplied to the electrodialysis tank was 50 A and the voltage was 200 V.
【００２２】電気透析槽の希釈室には上記濃縮排水を供
給し、濃縮室には上記脱塩設備からの精製水を供給し
た。The concentrated waste water was supplied to the dilution chamber of the electrodialysis tank, and the purified water from the desalination facility was supplied to the concentration chamber.
【００２３】その結果、電気透析槽の希釈室からは、Ｔ
ＤＳ１００ｐｐｍの精製水が２７０ｍ3 ／日の量で流出
し、これは上記脱塩設備からの精製水に合流して、飲料
水として利用することができた。As a result, from the dilution chamber of the electrodialysis tank, T
Purified water of 100 ppm DS flowed out in an amount of 270 m 3 / day, which could be combined with the purified water from the desalination facility and used as drinking water.
【００２４】また、電気透析槽の濃縮室からは、ＴＤＳ
２１０００ｐｐｍの再濃縮水が３０ｍ3 ／日の量で排出
された。これは、最初の濃縮排水の約７倍のＴＤＳ濃度
を有し、その量は約１／１０である。したがって、排水
処理の対象となる濃縮水の量が極めて少なくなり、例え
ば蒸発乾固して廃棄することも可能となる。From the concentration chamber of the electrodialysis tank, TDS
21000 ppm of reconcentrated water was discharged in an amount of 30 m 3 / day. It has a TDS concentration of about 7 times that of the first concentrated effluent, which is about 1/10. Therefore, the amount of concentrated water that is the target of wastewater treatment is extremely small, and it is possible to evaporate to dryness and discard it.
【００２５】[0025]
【発明の効果】以上説明したように、本発明によれば、
濃縮室におけるＳＯ4 などの多価陰イオン又はＣａなど
の多価陽イオンの濃度を極めて低く維持することがで
き、硫酸カルシウム、硫酸マグネシウムなどの難溶性塩
の電気透析膜への沈析が防止して、排水中に含まれる塩
分を更に高濃度に濃縮することが可能となる。その結
果、排水処理の対象となる濃縮水の量を極めて少なくす
ることができ、例えば蒸発乾固して廃棄することも可能
となる。As described above, according to the present invention,
The concentration of polyvalent anions such as SO 4 or polyvalent cations such as Ca in the concentration chamber can be kept extremely low, and the precipitation of sparingly soluble salts such as calcium sulfate and magnesium sulfate on the electrodialysis membrane is prevented. Then, it becomes possible to concentrate the salt content contained in the waste water to a higher concentration. As a result, the amount of concentrated water that is the target of wastewater treatment can be extremely reduced, and it is possible to evaporate to dryness and dispose of it.
【図１】本発明の一実施例を示す工程図FIG. 1 is a process chart showing an embodiment of the present invention.
Claims (3)
一価イオン選択透過膜を組み込んだ電気透析槽で透析し
て再脱塩するに際して、前記電気透析槽の濃縮室への供
給水として、脱塩処理された水を使用することを特徴と
する脱塩プロセスより排出される濃縮排水の再脱塩方
法。1. Concentrated wastewater discharged from the desalination process,
When performing desalting by dialysis in an electrodialysis tank incorporating a monovalent ion selective permeable membrane, desalted water is used as feed water to the concentration chamber of the electrodialysis tank. Re-desalination method of concentrated wastewater discharged from salt process.
ロセスにより精製された水を使用する請求項１記載の脱
塩プロセスより排出される濃縮排水の再脱塩方法。2. The method of re-desalting concentrated wastewater discharged from the desalination process according to claim 1, wherein water purified by the desalination process is used as the desalted water.
発乾固させる請求項１又は２記載の脱塩プロセスより排
出される濃縮排水の再脱塩方法。3. The method for re-desalinating concentrated waste water discharged from the desalination process according to claim 1, wherein the concentrated water re-concentrated in the electrodialysis tank is evaporated to dryness.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5319825A JPH07171351A (en) | 1993-12-20 | 1993-12-20 | Redesalting of concentrated drained water discharged from desulfurization process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5319825A JPH07171351A (en) | 1993-12-20 | 1993-12-20 | Redesalting of concentrated drained water discharged from desulfurization process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH07171351A true JPH07171351A (en) | 1995-07-11 |
Family
ID=18114633
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5319825A Pending JPH07171351A (en) | 1993-12-20 | 1993-12-20 | Redesalting of concentrated drained water discharged from desulfurization process |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH07171351A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109133440A (en) * | 2017-06-28 | 2019-01-04 | 北京朗新明环保科技有限公司 | A kind of desulfurization wastewater zero-discharge treatment system and technique |
-
1993
- 1993-12-20 JP JP5319825A patent/JPH07171351A/en active Pending
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109133440A (en) * | 2017-06-28 | 2019-01-04 | 北京朗新明环保科技有限公司 | A kind of desulfurization wastewater zero-discharge treatment system and technique |
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