JPH09220563A - Reverse osomosis membrane seawater desalting apparatus and method therefor - Google Patents
Reverse osomosis membrane seawater desalting apparatus and method thereforInfo
- Publication number
- JPH09220563A JPH09220563A JP8030717A JP3071796A JPH09220563A JP H09220563 A JPH09220563 A JP H09220563A JP 8030717 A JP8030717 A JP 8030717A JP 3071796 A JP3071796 A JP 3071796A JP H09220563 A JPH09220563 A JP H09220563A
- Authority
- JP
- Japan
- Prior art keywords
- preheater
- reverse osmosis
- membrane
- osmosis membrane
- temp
- 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
- Y02A20/131—Reverse-osmosis
-
- 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
- Y02A20/138—Water desalination using renewable energy
- Y02A20/144—Wave energy
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、逆浸透膜脱塩法に
よる海水の淡水化装置およびその方法に関するものであ
る。TECHNICAL FIELD The present invention relates to a desalination apparatus for seawater by a reverse osmosis membrane desalination method and a method thereof.
【０００２】[0002]
【従来の技術】逆浸透膜を利用した海水の淡水化技術は
種々開発されているが、その多くは原海水を砂等の濾過
材で濾過して清澄化するものである（化学工業便覧改訂
四版，９３８頁、丸善，昭和５３年，日本の科学と技
術，２６巻，２３５号，８５頁，１９８５年）。2. Description of the Related Art Various seawater desalination technologies using reverse osmosis membranes have been developed, but most of them are for clarifying raw seawater by filtering with a filter material such as sand (Chemical Industry Handbook, revised) Fourth edition, p. 938, Maruzen, 1978, Japanese Science and Technology, 26, 235, p. 85, 1985).
【０００３】一方、逆浸透膜を用いた海水の淡水化装置
において、逆浸透膜の水透過速度が供給海水温度に大き
く左右されること、これを海水の予熱によって改善する
ことは知られている（特開昭５２−２７０５７号公
報）。On the other hand, in a seawater desalination apparatus using a reverse osmosis membrane, it is known that the water permeation rate of the reverse osmosis membrane is greatly influenced by the temperature of the supplied seawater and that it is improved by preheating the seawater. (JP-A-52-27057).
【０００４】[0004]
【発明が解決しようとする課題】原海水の温度は季節に
より変動するため、従来技術では逆浸透膜装置の水透過
速度は供給原海水温度に大きく左右され、そのため、夏
期と冬期において同量の生産水量を確保しようとした場
合、使用する逆浸透膜のエレメント数を冬期の方が夏期
よりも多くしなければならず、運転維持管理が複雑にな
るという問題があった。Since the temperature of raw seawater varies depending on the season, the water permeation rate of a reverse osmosis membrane device in the prior art is greatly influenced by the temperature of the raw raw seawater supplied, and therefore, the same amount is obtained in summer and winter. In order to secure the amount of produced water, the number of elements of the reverse osmosis membrane to be used must be larger in winter than in summer, which causes a problem that operation and maintenance becomes complicated.
【０００５】特開昭５２−２７０５７号公報に開示され
た技術はこの問題点を解決するべくなされたものである
が、この技術では、膜の薬品洗浄間隔が短くなり薬品洗
浄の操作のための費用や労力がかかりコスト高につなが
る、という問題があった。The technique disclosed in Japanese Unexamined Patent Publication No. 52-27057 has been made to solve this problem. However, in this technique, the chemical cleaning interval of the membrane is shortened and the chemical cleaning operation is performed. There is a problem that it costs money and labor and leads to high cost.
【０００６】本発明は、上記の従来技術の欠点を克服す
べくなされたものであって、運転維持管理が容易でかつ
水透過性能の高い逆浸透膜脱塩法による海水淡水化装置
およびその方法を提供することを目的としている。The present invention has been made to overcome the above-mentioned drawbacks of the prior art, and is an apparatus and method for desalinating seawater by the reverse osmosis membrane desalination method, which is easy to maintain and manage and has high water permeability. Is intended to provide.
【０００７】[0007]
【課題を解決するための手段】上記課題を解決するため
に、本発明の逆浸透膜脱塩法海水淡水化装置は、逆浸透
膜装置の前処理として限外濾過膜又は精密濾過膜分離装
置を用いて、該濾過膜分離装置に供給する原海水を予め
加温するための予熱設備を有することを特徴として構成
されたものである。In order to solve the above problems, a reverse osmosis membrane desalination seawater desalination apparatus according to the present invention is an ultrafiltration membrane or microfiltration membrane separation apparatus as a pretreatment for a reverse osmosis membrane apparatus. Is used to preheat the raw seawater supplied to the filtration membrane separation device.
【０００８】すなわち、本発明は、原海水を予熱する予
熱器、限外濾過膜又は精密濾過膜装置、及び逆浸透膜装
置がこの順に配設され、該予熱器の出口側に温計検出器
が、逆浸透膜装置の入口側に圧力検出器が備えられ、該
温度検出器の検出温度又は圧力検出器の検出圧力に応じ
て予熱器の熱量を調節する調節機構を有していることを
特徴とする逆浸透膜脱塩法海水淡水化装置と、原海水を
２０〜３０℃に予熱してから限外濾過又は精密濾過し、
その後逆浸透膜によって脱塩することを特徴とする逆浸
透膜脱塩法海水淡水化方法を提供するものである。That is, according to the present invention, a preheater for preheating raw seawater, an ultrafiltration membrane or microfiltration membrane device, and a reverse osmosis membrane device are arranged in this order, and a thermometer detector is provided on the outlet side of the preheater. However, a pressure detector is provided on the inlet side of the reverse osmosis membrane device, and it has an adjusting mechanism for adjusting the heat quantity of the preheater according to the temperature detected by the temperature detector or the pressure detected by the pressure detector. Reverse osmosis membrane desalination seawater desalination equipment that features, and raw seawater is preheated to 20 to 30 ° C. and then subjected to ultrafiltration or microfiltration,
Then, a reverse osmosis membrane desalination method is provided for desalination by a reverse osmosis membrane.
【０００９】上記構成において、予熱設備で原海水を２
０〜３０℃程度に加温することにより、逆浸透膜装置の
前処理の膜分離装置においては、平均ろ過圧力あるいは
有効膜間差圧の急激な上昇はなく安定して連続通水する
ことを可能にし、さらに、逆浸透膜装置においても一定
数のエレメントで一定量の生産水量を得ることを可能に
している。In the above structure, the raw seawater is heated to 2 by the preheating facility.
By heating to about 0 to 30 ° C, in the membrane separator for pretreatment of the reverse osmosis membrane device, there is no sudden increase in the average filtration pressure or the effective transmembrane pressure difference, and stable continuous water flow is possible. In addition, even in the reverse osmosis membrane device, it is possible to obtain a fixed amount of produced water with a fixed number of elements.
【００１０】[0010]
【発明の実施の形態】予熱器は例えば５℃程度の原海水
を２０〜３０℃程度に加温できる能力を有するものであ
ればよく、通常は各現場で取得できる安価な熱源と熱交
換させる熱交換器が用いられる。BEST MODE FOR CARRYING OUT THE INVENTION The preheater may be any one that has the ability to heat raw seawater at about 5 ° C. to about 20 to 30 ° C., and normally exchanges heat with an inexpensive heat source that can be obtained at each site. A heat exchanger is used.
【００１１】限外濾過膜は、孔径が０．０１〜０．１μ
ｍ程度で、分画分子量が１０００以上、通常１千〜１０
万程度である。本発明に好ましいものは分画分子量が１
万〜１０万程度のものである。材質は酢酸セルロース
系、ポリアクリロニトリル系、ポリアミド−イミド系、
ポリアミド系、ポリスルホン系、ポリフッ化ビニリデン
系、ポリオレフィン系のものなどがあってそのいずれで
もよいが、好ましいものはポリアクリロニトリル系、ポ
リオレフィン系等である。The ultrafiltration membrane has a pore size of 0.01 to 0.1 μm.
m, the molecular weight cut-off is 1000 or more, usually 1,000 to 10
It is about ten thousand. Preferred in the present invention are those having a molecular weight cut off of 1
It is about 100,000 to 100,000. The material is cellulose acetate, polyacrylonitrile, polyamide-imide,
There are polyamide-based, polysulfone-based, polyvinylidene fluoride-based, and polyolefin-based ones, and any of them may be used. Preferred are polyacrylonitrile-based and polyolefin-based ones.
【００１２】精密濾過膜は、孔径が０．１〜１μｍ程度
のものである。材質は酢酸セルロース系、ニトロセルロ
ース系、ポリ塩化ビニル系、ポリスルホン系、ポリアミ
ド系ポリカーボネート系、ポリプロピレン系、ポリテト
ラフルオロエチレン系のものなどがあって、そのいずれ
も使用しうるが、好ましいものは、ポリプロピレン系、
ポリスルホン系等である。精密ろ過膜あるいは限外ろ過
膜のモジュールの形状は管型あるいは浸潰槽型のいずれ
であってもよい。The microfiltration membrane has a pore size of about 0.1 to 1 μm. The material is cellulose acetate, nitrocellulose, polyvinyl chloride, polysulfone, polyamide polycarbonate, polypropylene, polytetrafluoroethylene, etc., and any of them may be used. Polypropylene,
Polysulfone type and the like. The shape of the module of the microfiltration membrane or the ultrafiltration membrane may be either a tube type or a immersion tank type.
【００１３】また、これらの濾過膜を装着した装置は複
数を直列あるいは並列に設けてもよい。A plurality of devices equipped with these filtration membranes may be provided in series or in parallel.
【００１４】逆浸透膜は合成紙などで作られた膜支持体
の内面にポリアミド系、ポリエチレンイミン系、ポリエ
チレンオキサイド系、酢酸セルロース系、ポリスルホン
系、ポリフラン系のものなどの膜を接着したものであ
る。好ましいものは酢酸セルロース系、ポリアミド系等
である。膜の形状としては平膜型、チューブラー型、ス
パイラル型、中空糸型等各種のものがある。逆浸透膜を
装着した装置も複数を直列あるいは並列に設けてもよ
い。The reverse osmosis membrane is formed by adhering a membrane such as a polyamide-based, polyethyleneimine-based, polyethylene oxide-based, cellulose acetate-based, polysulfone-based or polyfuran-based membrane to the inner surface of a membrane support made of synthetic paper or the like. is there. Preferred are cellulose acetates, polyamides and the like. As the shape of the membrane, there are various types such as a flat membrane type, a tubular type, a spiral type, and a hollow fiber type. A plurality of devices equipped with reverse osmosis membranes may be provided in series or in parallel.
【００１５】予熱器の出口側には温度検出器が、そして
逆浸透膜装置の入口側には圧力検出器がそれぞれ備えら
れる。そして、これらによって検出された温度あるいは
圧力に応じて予熱器に供給される熱量を調節する調節機
構がさらに設けられる。この調節機構は原海水の温度の
ほか懸濁物質や溶解高分子の濃度等による濾過、透過速
度の低下を減少させて、濾過、透過速度を定常状態に維
持しうるよう原海水温度を制御するものである。A temperature detector is provided on the outlet side of the preheater, and a pressure detector is provided on the inlet side of the reverse osmosis membrane device. Further, an adjusting mechanism for adjusting the amount of heat supplied to the preheater according to the temperature or pressure detected by these is further provided. This regulation mechanism controls the temperature of raw seawater so that the filtration and permeation rate can be maintained in a steady state by reducing the decrease in filtration and permeation rate due to the concentration of suspended solids and dissolved polymers in addition to the temperature of raw seawater. It is a thing.
【００１６】本発明の装置には、そのほか貯槽、送液ポ
ンプ、薬剤供給管、流量計、各種検出器等が適宜設けら
れる。薬液注入の下流側にラインミキサー等を設けるこ
とも好ましい。The apparatus of the present invention is appropriately provided with a storage tank, a liquid feed pump, a drug supply pipe, a flow meter, various detectors and the like. It is also preferable to provide a line mixer or the like on the downstream side of the chemical solution injection.
【００１７】上記装置を利用して海水を淡水化するに
は、原海水に必要により殺菌剤、凝集剤、ｐＨ調整剤等
を加えてから予熱器で２０〜３０℃程度の範囲で濾過、
透過速度を定常状態に維持しうるよう加熱される。そし
て、逆浸透膜装置で分離された淡水は製造水として用途
に供する。一方、濃縮水は塩分等の回収原料としてもよ
く、海へ投入してもよい。To desalinate seawater using the above-mentioned apparatus, if necessary, a bactericidal agent, a coagulant, a pH adjusting agent, etc. are added to the raw seawater, and then filtered with a preheater in the range of about 20 to 30 ° C.
It is heated to keep the permeation rate steady. Then, the fresh water separated by the reverse osmosis membrane device is provided for use as production water. On the other hand, the concentrated water may be used as a raw material for recovering salt or the like, or may be put into the sea.
【００１８】[0018]
【実施例】以下に実施例を挙げて本発明をより具体的に
説明する。The present invention will be described more specifically with reference to the following examples.
【００１９】（実施例１）図１に示す装置を使用した。
この装置は予熱器６、濾過膜分離装置９、貯留槽１１、
逆浸透膜装置１３及び生産水槽１６よりなっている。予
熱器６の入口側には原海水供給配管１がポンプ２を介し
て接続されている。この配管１の途中には殺菌剤供給配
管３、ｐＨ調整剤供給配管４および凝集剤供給配管５が
それぞれ接続されている。予熱器６の出口側配管７は濾
過膜分離装置９に接続されており、該配管７の途中には
温度検出器が取付けられている。予熱器６から排出され
る原海水の温度がこの温度検出器で検出され、この検出
温度によって温度制御器８が予熱器６に供給される熱量
を調整する。濾過膜分離装置９の出口側配管１０は貯留
槽１１に接続され、貯留槽１１からは高圧ポンプ１２を
介して逆浸透膜装置１３に配管接続されている。逆浸透
膜装置１３の出口には濃縮水配管１５と淡水配管１４が
接続されている。淡水配管１４は生産水槽１６に接続さ
れており、そこから淡水が製造水として取り出される。Example 1 The apparatus shown in FIG. 1 was used.
This device includes a preheater 6, a filtration membrane separation device 9, a storage tank 11,
It comprises a reverse osmosis membrane device 13 and a production water tank 16. The raw seawater supply pipe 1 is connected via a pump 2 to the inlet side of the preheater 6. In the middle of the pipe 1, a disinfectant supply pipe 3, a pH adjusting agent supply pipe 4, and a coagulant supply pipe 5 are connected. The outlet side pipe 7 of the preheater 6 is connected to the filtration membrane separation device 9, and a temperature detector is attached in the middle of the pipe 7. The temperature of the raw seawater discharged from the preheater 6 is detected by this temperature detector, and the temperature controller 8 adjusts the amount of heat supplied to the preheater 6 by this detected temperature. The outlet side pipe 10 of the filtration membrane separation device 9 is connected to a storage tank 11, and the storage tank 11 is connected to a reverse osmosis membrane device 13 via a high-pressure pump 12. A concentrated water pipe 15 and a fresh water pipe 14 are connected to the outlet of the reverse osmosis membrane device 13. The fresh water pipe 14 is connected to a production water tank 16 from which fresh water is taken out as production water.
【００２０】この装置を用い、次のようにして海水を淡
水化した。まず、原海水を配管１よりポンプ２で濾過膜
分離装置９に供給する過程において、予め殺菌剤、ｐＨ
調整剤および凝集剤をそれぞれ配管３、４、５より添加
した。殺菌剤には次亜塩素酸ナトリウムを、ｐＨ調整剤
には硫酸を、そして凝集剤には塩化第二鉄を用い、それ
ぞれ５ｍｇ／ｌ、２ｍｇ／ｌ、３ｍｇ／ｌとなるように
添加した。次いで、原海水は予熱器６により２５℃まで
加温されながら配管内において充分に攪拌させた後、濾
過膜分離装置９により不溶性沈殿物および懸濁物質を除
去した。次いで、膜濾過水は貯留槽１１に導入され、高
圧ポンプ１２によって加圧され、逆浸透膜装置１３に供
給された。濃縮水は配管１５より回収され、淡水は配管
１４より回収された。淡水は生産水槽１６に導入され製
造水を得た。Using this device, seawater was desalinated as follows. First, in the process of supplying raw seawater from the pipe 1 to the filtration membrane separation device 9 with the pump 2, the sterilizing agent and pH
A regulator and a coagulant were added through pipes 3, 4, and 5, respectively. Sodium hypochlorite was used as a bactericide, sulfuric acid was used as a pH adjuster, and ferric chloride was used as a flocculant, and added at 5 mg / l, 2 mg / l, and 3 mg / l, respectively. Next, the raw seawater was sufficiently stirred in the pipe while being heated to 25 ° C. by the preheater 6, and then the insoluble precipitate and the suspended substance were removed by the filtration membrane separation device 9. Next, the membrane filtered water was introduced into the storage tank 11, pressurized by the high pressure pump 12, and supplied to the reverse osmosis membrane device 13. The concentrated water was collected through the pipe 15, and the fresh water was collected through the pipe 14. Fresh water was introduced into the production water tank 16 to obtain production water.
【００２１】表１に示した膜モジュールおよび表２に示
した運転条件によって通水実験を行い、図２に●で示す
ような結果を得た。ここで、膜間差圧とは精密ろ過膜装
置における膜入口圧力から膜出口圧力を差し引いた圧力
を表している。Water-passing experiments were conducted under the membrane modules shown in Table 1 and the operating conditions shown in Table 2, and the results shown by ● in FIG. 2 were obtained. Here, the transmembrane pressure difference represents a pressure obtained by subtracting the membrane outlet pressure from the membrane inlet pressure in the microfiltration membrane device.
【００２２】[0022]
【表１】 [Table 1]
【００２３】[0023]
【表２】 [Table 2]
【００２４】図３より明らかなように、本発明の方法に
よれば、精密ろ過膜装置の膜間差圧の上昇は見られず安
定して通水することができる。As is apparent from FIG. 3, according to the method of the present invention, the transmembrane pressure of the microfiltration membrane device is not increased and stable water can be passed.
【００２５】（比較例１）供給原海水の温度が５〜７℃
で推移し、逆浸透膜装置のエレメント数を６本にしたこ
と以外は実施例１と同様の処理を行い、図２に○で示す
ような結果を得た。(Comparative Example 1) The temperature of the raw seawater supplied is 5 to 7 ° C.
The same treatment as in Example 1 was carried out except that the number of elements of the reverse osmosis membrane device was changed to 6, and the results shown by ◯ in FIG. 2 were obtained.
【００２６】（実施例２）供給原海水の温度を２５℃で
一定とし、前処理の濾過膜分離装置として限外ろ過膜装
置を用いて、表３に示した膜モジュールおよび表４に示
した運転条件によって通水実験を行い、図３に示すよう
な結果を得た。ここで、平均ろ過圧とは限外ろ過膜装置
における膜入口圧力と循環水圧力の平均から膜出口圧力
を差し引いた圧力を表している。Example 2 The membrane module shown in Table 3 and Table 4 were prepared by using the ultrafiltration membrane device as a pretreatment filtration membrane separation device while keeping the temperature of the raw seawater supply constant at 25 ° C. A water flow experiment was conducted under operating conditions, and the results shown in FIG. 3 were obtained. Here, the average filtration pressure represents a pressure obtained by subtracting the membrane outlet pressure from the average of the membrane inlet pressure and the circulating water pressure in the ultrafiltration membrane device.
【００２７】[0027]
【表３】 [Table 3]
【００２８】[0028]
【表４】 [Table 4]
【００２９】図３より明らかなように、本発明の方法に
よれば、限外ろ過膜装置の平均ろ過圧の上昇は見られず
安定して通水することができる。As is clear from FIG. 3, according to the method of the present invention, stable increase in the average filtration pressure of the ultrafiltration membrane device is not observed and stable water can be passed.
【００３０】（比較例２）供給原海水の温度が５〜７℃
で推移し、逆浸透膜装置のエレメント数を６本にしたこ
と以外は実施例２と同様の処理を行い、図３に示すよう
な結果を得た。(Comparative Example 2) The temperature of the raw seawater supplied is 5 to 7 ° C.
The same treatment as in Example 2 was performed except that the number of elements of the reverse osmosis membrane device was changed to 6, and the results shown in FIG. 3 were obtained.
【００３１】[0031]
【発明の効果】以上述べたように、本発明によれば、逆
浸透膜装置の前処理として濾過膜分離装置を用いて、膜
分離装置に供給する原海水を予め加温するための予熱設
備を有し、予熱設備で原海水を２０〜３０℃程度に加温
することにより、濾過膜分離装置においては、平均ろ過
圧力あるいは有効膜間差圧の急激な上昇はなく安定して
連続通水することができる。さらに、逆浸透膜装置にお
いてもエレメント数を削減できることにより、生産水の
コトス低下につながる。また、運転維持管理が容易にな
り、特に前処理の濾過膜分離装置における薬品洗浄の間
隔が長くなることから、薬品洗浄操作のための費用や労
力が削減できる等の効果を有する。As described above, according to the present invention, the preheating equipment for preheating the raw seawater supplied to the membrane separation device by using the filtration membrane separation device as the pretreatment of the reverse osmosis membrane device. In addition, by heating the raw seawater to about 20 to 30 ° C. in the preheating equipment, the filtration membrane separation device does not have a rapid increase in the average filtration pressure or the effective transmembrane pressure difference, and stable continuous water flow is achieved. can do. Furthermore, the number of elements can be reduced even in the reverse osmosis membrane device, which leads to a reduction in the amount of product water. Further, the operation and maintenance are facilitated, and particularly, the interval of chemical cleaning in the pretreatment filtration membrane separation device is lengthened, so that the cost and labor for the chemical cleaning operation can be reduced.
【図１】 本発明の一実施例における逆浸透膜脱塩法海
水淡水化装置の全体構成図である。FIG. 1 is an overall configuration diagram of a reverse osmosis membrane desalination seawater desalination apparatus according to an embodiment of the present invention.
【図２】 実施例１及び比較例１の運転結果を示すグラ
フである。FIG. 2 is a graph showing the operation results of Example 1 and Comparative Example 1.
【図３】 実施例２及び比較例２の運転結果を示すグラ
フである。FIG. 3 is a graph showing the operation results of Example 2 and Comparative Example 2.
６…予熱器 ８…温度制御器 ９…濾過膜分離装置 １１…貯留槽 １３…逆浸透膜装置 １６…生産水槽 6 ... Preheater 8 ... Temperature controller 9 ... Filtration membrane separation device 11 ... Storage tank 13 ... Reverse osmosis membrane device 16 ... Production water tank
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 庁内整理番号 ＦＩ 技術表示箇所 Ｂ０１Ｄ 61/18 Ｂ０１Ｄ 61/18 61/20 61/20 61/58 61/58 ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 6 Identification number Office reference number FI technical display location B01D 61/18 B01D 61/18 61/20 61/20 61/58 61/58
Claims (2)
は精密濾過膜装置、及び逆浸透膜装置がこの順に配設さ
れ、該予熱器の出口側に温計検出器が、逆浸透膜装置の
入口側に圧力検出器が備えられ、該温度検出器の検出温
度又は圧力検出器の検出圧力に応じて予熱器の熱量を調
節する調節機構を有していることを特徴とする逆浸透膜
脱塩法海水淡水化装置1. A preheater for preheating raw seawater, an ultrafiltration membrane or microfiltration membrane device, and a reverse osmosis membrane device are arranged in this order, and a thermometer detector is provided on the outlet side of the preheater, and a reverse osmosis device is provided. A pressure detector is provided on the inlet side of the membrane device, and the pressure detector has an adjusting mechanism for adjusting the heat quantity of the preheater according to the temperature detected by the temperature detector or the pressure detected by the pressure detector. Permeation membrane desalination seawater desalination equipment
外濾過又は精密濾過し、その後逆浸透膜によって脱塩す
ることを特徴とする逆浸透膜脱塩法海水淡水化方法2. A reverse osmosis membrane desalination seawater desalination method, which comprises preheating raw seawater to 20 to 30 ° C., performing ultrafiltration or microfiltration, and then desalting with a reverse osmosis membrane.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8030717A JPH09220563A (en) | 1996-02-19 | 1996-02-19 | Reverse osomosis membrane seawater desalting apparatus and method therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP8030717A JPH09220563A (en) | 1996-02-19 | 1996-02-19 | Reverse osomosis membrane seawater desalting apparatus and method therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09220563A true JPH09220563A (en) | 1997-08-26 |
Family
ID=12311406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP8030717A Pending JPH09220563A (en) | 1996-02-19 | 1996-02-19 | Reverse osomosis membrane seawater desalting apparatus and method therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09220563A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2009113178A1 (en) * | 2008-03-14 | 2009-09-17 | 三菱重工業株式会社 | Dehydration system and method of dehydration |
| CN102583861A (en) * | 2012-02-22 | 2012-07-18 | 中国海洋大学 | Method for preheating inflow water of membrane method seawater softening device |
| US8496731B2 (en) | 2007-03-15 | 2013-07-30 | Mitsubishi Heavy Industries, Ltd. | Method for transporting fluid |
| US9149769B2 (en) | 2007-03-15 | 2015-10-06 | Mitsubishi Heavy Industries, Ltd. | Dehydration system and dehydration method |
-
1996
- 1996-02-19 JP JP8030717A patent/JPH09220563A/en active Pending
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8858798B2 (en) | 2006-10-05 | 2014-10-14 | Mitsubishi Heavy Industries, Ltd. | Dehydration method |
| US8496731B2 (en) | 2007-03-15 | 2013-07-30 | Mitsubishi Heavy Industries, Ltd. | Method for transporting fluid |
| US9149769B2 (en) | 2007-03-15 | 2015-10-06 | Mitsubishi Heavy Industries, Ltd. | Dehydration system and dehydration method |
| WO2009113178A1 (en) * | 2008-03-14 | 2009-09-17 | 三菱重工業株式会社 | Dehydration system and method of dehydration |
| US8585904B2 (en) | 2008-03-14 | 2013-11-19 | Mitsubishi Heavy Industries, Ltd. | Dehydration system and dehydration method |
| CN102583861A (en) * | 2012-02-22 | 2012-07-18 | 中国海洋大学 | Method for preheating inflow water of membrane method seawater softening device |
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