JP3100504B2 - Demineralized water production equipment - Google Patents
Demineralized water production equipmentInfo
- Publication number
- JP3100504B2 JP3100504B2 JP06081082A JP8108294A JP3100504B2 JP 3100504 B2 JP3100504 B2 JP 3100504B2 JP 06081082 A JP06081082 A JP 06081082A JP 8108294 A JP8108294 A JP 8108294A JP 3100504 B2 JP3100504 B2 JP 3100504B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- storage tank
- return pipe
- concentrated
- raw water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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)
- Degasification And Air Bubble Elimination (AREA)
- Physical Water Treatments (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は逆浸透膜装置を用いて被
処理水を濃縮水と透過水とに分離するようにした脱塩水
製造装置に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a desalinated water producing apparatus for separating treated water into concentrated water and permeated water using a reverse osmosis membrane device.
【０００２】[0002]
【従来の技術】逆浸透膜を利用して被処理水を濃縮水と
透過水とに分離する脱塩水製造装置が知られている。こ
の逆浸透膜を利用した脱塩水製造装置によった場合、被
処理水中に含まれるナトリウム、カルシウム、マグネシ
ウム、塩化物、硫酸根、硝酸根などのイオンは有効に除
去することができるが、被処理水に溶解している遊離二
酸化炭素は逆浸透膜を透過してしまい、透過水の水質が
悪化するという問題がある。そのため、工業的には逆浸
透膜装置の前段に脱炭酸塔を付設して、被処理水中の遊
離二酸化炭素を除去して、炭酸ガスの取り除かれた被処
理水を逆浸透膜装置に送るようにしている。2. Description of the Related Art There is known an apparatus for producing desalinated water in which water to be treated is separated into concentrated water and permeated water using a reverse osmosis membrane. According to the apparatus for producing desalinated water using this reverse osmosis membrane, ions such as sodium, calcium, magnesium, chloride, sulfate and nitrate contained in the water to be treated can be effectively removed. There is a problem that free carbon dioxide dissolved in the treated water permeates the reverse osmosis membrane and the quality of the permeated water deteriorates. For this reason, industrially, a decarbonation tower is provided in front of the reverse osmosis membrane device to remove free carbon dioxide in the water to be treated and to send the water to be treated with carbon dioxide removed to the reverse osmosis membrane device. I have to.
【０００３】[0003]
【発明が解決しようとする課題】上記したように、工業
的には逆浸透膜装置の前段に脱炭酸塔を設備して、被処
理水中の遊離二酸化炭素を除去するようにしている。し
かしながら、前記脱炭酸塔は周知のように設備全体が可
成り大型であり、工業的には設置上何ら問題はないにし
ても、研究室や実験室規模等の比較的小規模の脱塩水製
造装置にはスペース的に設置することができない。その
ため、これまでの研究室規模の脱塩水製造装置において
は、逆浸透膜を透過した透過水中に遊離二酸化炭素が含
まれたままであり、そのため後段にイオン交換塔が接続
されている場合は遊離二酸化炭素の除去されていない透
過水がそのまま後段のイオン交換塔に送られることとな
り、その結果、イオン交換塔内に充填されている陰イオ
ン交換樹脂の負荷が増大して、イオン交換塔の通水ライ
フが短縮されるという問題点があった。As described above, a decarbonation tower is industrially provided in front of a reverse osmosis membrane apparatus to remove free carbon dioxide in the water to be treated. However, as is well known, the entire decarbonation tower is quite large, and even if there is no problem in industrial installation, relatively small scale production of desalinated water such as a laboratory or a laboratory is required. The device cannot be installed in space. Therefore, in a conventional laboratory-scale desalinated water production apparatus, free carbon dioxide is still contained in the permeated water permeated through the reverse osmosis membrane. The permeated water from which carbon has not been removed is sent to the subsequent ion exchange tower as it is, and as a result, the load on the anion exchange resin filled in the ion exchange tower increases, and the water flowing through the ion exchange tower is increased. There was a problem that life was shortened.
【０００４】そこで、本発明は逆浸透膜装置によって分
離された濃縮水の戻し管中にエゼクタを付設し、当該エ
ゼクタより空気を吸引して、戻し管を通じて流れる濃縮
水中に空気を混合させ、気液接触により遊離二酸化炭素
を除去するようにして、逆浸透膜装置の前段に脱炭酸塔
を設備しなくても遊離二酸化炭素量の低減された透過水
を得ることができ、したがって、後段にイオン交換塔が
接続されている場合には、当該イオン交換塔内に充填さ
れている陰イオン交換樹脂の負荷を大幅に軽減できるよ
うになした脱塩水製造装置を提供することを目的とする
ものである。Accordingly, the present invention provides an ejector in the return pipe of the concentrated water separated by the reverse osmosis membrane device, sucks air from the ejector, mixes the air with the concentrated water flowing through the return pipe, and removes the air. By removing free carbon dioxide by liquid contact, it is possible to obtain permeated water having a reduced amount of free carbon dioxide without installing a decarbonation tower in the preceding stage of the reverse osmosis membrane device, and therefore, in the latter stage, When an exchange tower is connected, an object of the present invention is to provide a desalinated water production apparatus capable of greatly reducing the load of the anion exchange resin charged in the ion exchange tower. is there.
【０００５】[0005]
【課題を解決するための手段】前記目的を達成するため
の本発明の構成を詳述すれば、請求項１に係る発明は、
原水貯槽内の被処理水をポンプによって逆浸透膜装置に
送り、逆浸透膜によって被処理水を透過水と濃縮水とに
分離し、濃縮水を戻し管を通じて原水貯槽内に戻すよう
になした脱塩水製造装置において、前記濃縮水の戻し管
の管路中にエゼクタを付設し、戻し管を流れる濃縮水の
流速を利用して当該エゼクタより空気を吸引し、気液接
触により濃縮水中の遊離二酸化炭素を除去するようにな
したことを特徴とする脱塩水製造装置であり、また、請
求項２に係る発明は、原水貯槽内の上部にスプレーノズ
ルを配設し、戻し管を通じて原水貯槽内に戻される濃縮
水を、当該スプレーノズルを介して原水貯槽内に散水す
るようになした請求項１記載の脱塩水製造装置である。The structure of the present invention for achieving the above object will be described in detail.
The water to be treated in the raw water storage tank is sent to the reverse osmosis membrane device by a pump, the water to be treated is separated into permeated water and concentrated water by the reverse osmosis membrane, and the concentrated water is returned to the raw water storage tank through the return pipe. In the desalinated water production device, an ejector is provided in the conduit of the return pipe of the concentrated water, air is sucked from the ejector using the flow rate of the concentrated water flowing through the return pipe, and liberation of the concentrated water is performed by gas-liquid contact. A desalinated water producing apparatus characterized in that carbon dioxide is removed, and the invention according to claim 2 is arranged such that a spray nozzle is disposed in an upper part of the raw water storage tank, and the inside of the raw water storage tank is returned through a return pipe. The desalinated water producing apparatus according to claim 1, wherein the concentrated water returned to the water is sprayed into the raw water storage tank through the spray nozzle.
【０００６】[0006]
【作用】このように、本発明脱塩水製造装置において
は、濃縮水の戻し管の管路中にエゼクタを付設してある
ので、逆浸透膜を透過しなかった比較的高圧の濃縮水が
エゼクタを通過するときに当該エゼクタによって空気が
吸引され、戻し管を流れる濃縮水の中に当該吸引空気が
混合される。そして、気液接触により濃縮水中の遊離二
酸化炭素が濃縮水中より分離され、分離された遊離二酸
化炭素は、濃縮水が戻し管の先端から原水貯槽内に戻さ
れた時に、炭酸ガスとして原水貯槽の上部に設けてある
排気管を通じて外部に排出されるものである。また、原
水貯槽内の上部にスプレーノズルを配設し、濃縮水を当
該スプレーノズルによって噴霧状あるいは微細な水滴状
にして下方に降らせるようにすると、気液接触効果が一
層向上し、きわめて良好に遊離二酸化炭素を除去するこ
とができるものである。なお、スプレーノズルを配設し
ない場合は、原水貯槽内に濃縮水を戻すための戻し管の
先端部は、必ずしも原水貯槽内の上部位置に設定する必
要はなく、たとえば原水貯槽内に貯溜されている被処理
水の水面下に戻し管の先端部を位置させるようにしても
よいものである。As described above, in the apparatus for producing desalinated water of the present invention, since the ejector is provided in the conduit of the return pipe of the concentrated water, the relatively high-pressure concentrated water that has not passed through the reverse osmosis membrane is ejected. The air is sucked by the ejector as it passes through, and the sucked air is mixed with the concentrated water flowing through the return pipe. Then, free carbon dioxide in the concentrated water is separated from the concentrated water by gas-liquid contact, and the separated free carbon dioxide is converted into carbon dioxide gas in the raw water storage tank when the concentrated water is returned into the raw water storage tank from the end of the return pipe. It is discharged to the outside through an exhaust pipe provided at the top. In addition, when a spray nozzle is arranged at the upper part in the raw water storage tank, and the concentrated water is made to fall down in the form of a spray or fine water droplets by the spray nozzle, the gas-liquid contact effect is further improved, and it is extremely favorable. Free carbon dioxide can be removed. When the spray nozzle is not provided, the end of the return pipe for returning the concentrated water into the raw water storage tank does not necessarily need to be set at the upper position in the raw water storage tank, and is, for example, stored in the raw water storage tank. Alternatively, the tip of the return pipe may be located below the surface of the water to be treated.
【０００７】本発明脱塩水製造装置によった場合は、従
来のような大型の脱炭酸塔を逆浸透膜装置の前段に設備
しなくても、良好に被処理水中の遊離二酸化炭素を軽減
することができて純度の高い透過水を得ることができる
と共に、当該逆浸透膜装置の後段にイオン交換塔を接続
した場合には、後段のイオン交換塔内に充填されている
陰イオン交換樹脂に掛かる負荷を大幅に軽減することが
でき、当該イオン交換塔の通水ライフを延ばすことが可
能となる。[0007] According to the apparatus for producing desalinated water of the present invention, free carbon dioxide in the water to be treated can be satisfactorily reduced without having to install a conventional large-scale decarbonation tower in front of the reverse osmosis membrane apparatus. It is possible to obtain high-purity permeated water and, when an ion exchange column is connected to the subsequent stage of the reverse osmosis membrane device, to the anion exchange resin filled in the subsequent ion exchange column. The applied load can be greatly reduced, and the water flow life of the ion exchange tower can be extended.
【０００８】[0008]
【実施例】以下、本発明脱塩水製造装置の具体的構成を
図示の実施例に基づいて詳細に説明する。図１は本発明
脱塩水製造装置の一実施例を示す概略図、図２は本発明
脱塩水製造装置の他の実施例を示す概略図である。BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a block diagram showing an embodiment of a desalinated water producing apparatus according to the present invention. FIG. 1 is a schematic view showing an embodiment of the desalinated water producing apparatus of the present invention, and FIG. 2 is a schematic view showing another embodiment of the desalinated water producing apparatus of the present invention.
【０００９】図中１は原水貯槽、２は当該原水貯槽１に
被処理水を供給する原水供給管、３は原水貯槽１内の被
処理水を逆浸透膜装置４に送る送水管、５は当該送水管
３の管路中に付設したポンプ、６は前記逆浸透膜装置４
の内部に付設された逆浸透膜、７は当該逆浸透膜６を透
過しなかった濃縮水を前記原水貯槽１内に戻すための戻
し管である。なお、戻し管７を通じて濃縮水の全てが原
水貯槽１内に戻されるものではなく、通常は濃縮水の約
７０％前後を原水貯槽１内に戻し、残りの濃縮水は戻し
管７に接続された排水管８を通じてブローするようにし
ている。In the figure, 1 is a raw water storage tank, 2 is a raw water supply pipe for supplying the raw water to the raw water storage tank 1, 3 is a water feed pipe for sending the raw water in the raw water storage tank 1 to the reverse osmosis membrane device 4, and 5 is A pump provided in the pipe of the water supply pipe 3, 6 is the reverse osmosis membrane device 4
Is a return pipe for returning the concentrated water that has not passed through the reverse osmosis membrane 6 into the raw water storage tank 1. Note that not all of the concentrated water is returned to the raw water storage tank 1 through the return pipe 7. Normally, about 70% of the concentrated water is returned to the raw water storage tank 1, and the remaining concentrated water is connected to the return pipe 7. The water is blown through the drain pipe 8.
【００１０】次に、９は前記濃縮水の戻し管７の管路中
に付設したエゼクタであり、ポンプ５によって付勢され
た濃縮水がエゼクタ９を通過するときに、当該エゼクタ
９内に外部の空気が吸引され、戻し管７を流れる濃縮水
中に当該空気が攪拌混合される。１０は原水貯槽１内の
上部に配設したスプレーノズルであり、戻し管７の先端
部は当該スプレーノズル１０に接続されている。なお、
本発明装置においては戻し管７の先端部に必ずしもスプ
レーノズルを接続する必要はなく、特に図示しないが、
戻し管７の先端部を単純に原水貯槽１内の下方に向けて
突出させるようにしてもよいし、あるいは、図２に示す
実施例のように戻し管７の先端部１１を原水貯槽１内の
被処理水の水面下に位置させるようにしてもよいもので
ある。さらに、特に図示していないが、原水供給管２を
原水貯槽１に直接連通せずに、原水供給管２の先端をエ
ゼクタ９の下流側の戻し管７に連通させ、原水を戻し管
７を介して濃縮水と混合して原水貯槽１内に供給するよ
うにしてもよい。Reference numeral 9 denotes an ejector provided in the conduit of the return pipe 7 of the concentrated water. When the concentrated water urged by the pump 5 passes through the ejector 9, the ejector 9 is provided inside the ejector 9. Is sucked, and the air is stirred and mixed into the concentrated water flowing through the return pipe 7. Reference numeral 10 denotes a spray nozzle disposed at an upper portion in the raw water storage tank 1, and a tip of the return pipe 7 is connected to the spray nozzle 10. In addition,
In the device of the present invention, it is not always necessary to connect the spray nozzle to the tip of the return pipe 7, and although not particularly shown,
The distal end of the return pipe 7 may simply protrude downward in the raw water storage tank 1, or the distal end 11 of the return pipe 7 may be connected to the raw water storage tank 1 as in the embodiment shown in FIG. May be located below the surface of the water to be treated. Further, although not particularly shown, the raw water supply pipe 2 is not directly connected to the raw water storage tank 1, but the distal end of the raw water supply pipe 2 is connected to a return pipe 7 downstream of the ejector 9, and the raw water is returned to the return pipe 7. Alternatively, the raw water may be mixed with the concentrated water and supplied into the raw water storage tank 1.
【００１１】その他、図中の１２は原水貯槽１の上部に
付設した排気管である。１３は逆浸透膜装置４の透過水
側に接続した透過水の出口管であり、当該出口管１３の
先端部は図示しないたとえばイオン交換塔の上部に接続
される。１４は前記エゼクタ９の手前の戻し管７の管路
中に付設したバルブ、１５は前記排水管８の管路中に付
設したバルブである。なお、当該バルブ１４および１５
の開度を調節することにより、戻し管７を通じて原水貯
槽１内に戻される濃縮水の分量が決定される。In addition, reference numeral 12 in the drawing denotes an exhaust pipe provided above the raw water storage tank 1. Reference numeral 13 denotes an outlet pipe of permeated water connected to the permeated water side of the reverse osmosis membrane device 4, and a distal end of the outlet pipe 13 is connected to, for example, an upper part of an ion exchange tower (not shown). Reference numeral 14 denotes a valve provided in the conduit of the return pipe 7 in front of the ejector 9, and reference numeral 15 denotes a valve provided in the pipe of the drain pipe 8. The valves 14 and 15
The amount of concentrated water returned into the raw water storage tank 1 through the return pipe 7 is determined by adjusting the opening degree of the concentrated water.
【００１２】図１に示す実施例の場合、原水貯槽１内の
被処理水はポンプ５によって吸引され、送水管３を通じ
て逆浸透膜装置４内に送られる。そして、逆浸透膜６を
透過し、逆浸透膜６によってナトリウムやカルシウムな
どのイオンが取り除かれた透過水は出口管１３を通じて
後段の図示しない処理設備に送られる。In the embodiment shown in FIG. 1, the water to be treated in the raw water storage tank 1 is sucked by the pump 5 and sent to the reverse osmosis membrane device 4 through the water pipe 3. Then, the permeated water that has passed through the reverse osmosis membrane 6 and from which ions such as sodium and calcium have been removed by the reverse osmosis membrane 6 is sent through an outlet pipe 13 to processing equipment (not shown) at the subsequent stage.
【００１３】一方、逆浸透膜６を透過しなかった非透過
水はイオン濃度の高い濃縮水となって戻し管７を通じて
原水貯槽１内に戻されるが、当該戻し管７の管路中にエ
ゼクタ９が付設されているので、エゼクタ９より吸引さ
れる空気が戻し管７を流れる濃縮水中に激しく攪拌状態
で混合され、気液接触状態でスプレーノズル１０より噴
霧状あるいは微細な水滴状となって散布され、原水貯槽
１内に戻される。この際、濃縮水から遊離二酸化炭素が
炭酸ガスとして分離され、分離された炭酸ガスは原水貯
槽１の上部に設けてある排気管１２を通じて外部に排気
される。また、この実施例においては、前記したように
原水貯槽１内に戻される濃縮水はスプレーノズル１０に
よって細かく分散されるようになっているので被処理水
の水面に到達するまでの間においても気液接触が行わ
れ、炭酸ガスの分離が一層促進されることとなる。この
循環が継続されることにより被処理水中の遊離二酸化炭
素濃度は次第に低減され、透過水中に含まれる遊離二酸
化炭素濃度も大幅に軽減されるものである。On the other hand, the non-permeated water that has not passed through the reverse osmosis membrane 6 becomes concentrated water having a high ion concentration and is returned to the raw water storage tank 1 through the return pipe 7. Since the nozzle 9 is attached, the air sucked from the ejector 9 is mixed with the concentrated water flowing through the return pipe 7 in a vigorous stirring state, and becomes a spray or fine water droplet from the spray nozzle 10 in a gas-liquid contact state. Sprayed and returned into the raw water storage tank 1. At this time, free carbon dioxide is separated from the concentrated water as carbon dioxide, and the separated carbon dioxide is exhausted to the outside through an exhaust pipe 12 provided at an upper part of the raw water storage tank 1. Further, in this embodiment, since the concentrated water returned into the raw water storage tank 1 is finely dispersed by the spray nozzle 10 as described above, the concentrated water returns to the surface of the water to be treated. Liquid contact is performed, and the separation of carbon dioxide gas is further promoted. By continuing this circulation, the concentration of free carbon dioxide in the water to be treated is gradually reduced, and the concentration of free carbon dioxide contained in the permeated water is also significantly reduced.
【００１４】図２に示す実施例は、戻し管７の先端部１
１を原水貯槽１内の被処理水の水面下に没するようにし
たものであるが、このようにした場合、戻し管７の先端
部１１から戻される濃縮水中には多量の空気が含まれて
いるため、原水貯槽１内の被処理水中で気泡化して良好
な気液接触効果が得られるものである。なお、前記いず
れの実施例においても、エゼクタ９によって吸引する空
気の量は、原水貯槽１内に戻される濃縮水の量と同等
か、あるいはそれ以上の量とするのが好ましい。The embodiment shown in FIG.
1 is submerged under the surface of the water to be treated in the raw water storage tank 1. In such a case, the concentrated water returned from the distal end 11 of the return pipe 7 contains a large amount of air. Therefore, bubbles are formed in the water to be treated in the raw water storage tank 1 and a good gas-liquid contact effect can be obtained. In any of the above embodiments, the amount of air sucked by the ejector 9 is preferably equal to or larger than the amount of concentrated water returned into the raw water storage tank 1.
【００１５】次に、水温が２０℃、ＴＡ（トータルアニ
オン）が１リットル当たり１４０ｍｇＣａＣＯ3 で、そ
のうちＣＯ2 の含有量が７ｍｇＣａＣＯ3 の一般市水を
被処理水に設定し、当該被処理水を原水貯槽１内からポ
ンプ５によって１２Ｋｇ／ｃｍ2 の圧力で逆浸透膜装置
４内に、１時間当たり７００リットル供給し、透過水８
０リットルを除いた濃縮水のうち４５０リットルを、管
路中にエゼクタ９を具えた戻し管７の通常の先端部、す
なわちスプレーノズルを用いないで戻し管７の先端口か
ら原水貯槽１内に普通に戻すようにした実験例（Ａ）
と、同じくエゼクタ９を具えた戻し管７の先端部にスプ
レーノズル１０を接続して、当該スプレーノズル１０か
ら濃縮水を微細な粒子状（３５００μｍ程度）にして戻
すようにした実験例（Ｂ）を、戻し管の管路中にエゼク
タを具えない従来の脱塩水製造装置による比較例と併せ
て表１に実験の結果を示す。なお、上記実験例（Ａ）お
よび（Ｂ）のいずれもエゼクタで供給する空気量は、空
気量／戻し濃縮水＝１／１（容量比）の割合とした。Next, general city water having a water temperature of 20 ° C., a TA (total anion) of 140 mg CaCO 3 per liter and a CO 2 content of 7 mg CaCO 3 is set as the water to be treated, and the water to be treated is 700 liters per hour are supplied from the raw water storage tank 1 into the reverse osmosis membrane device 4 by the pump 5 at a pressure of 12 kg / cm 2 , and the permeated water 8
450 liters of the concentrated water excluding 0 liters is introduced into the raw water storage tank 1 from the normal end of the return pipe 7 having an ejector 9 in the pipeline, that is, from the distal end of the return pipe 7 without using a spray nozzle. Experimental example (A)
An experimental example (B) in which a spray nozzle 10 is connected to the tip of a return pipe 7 also equipped with an ejector 9 and the concentrated water is returned from the spray nozzle 10 into fine particles (about 3500 μm). Table 1 shows the results of the experiment together with a comparative example using a conventional desalinated water producing apparatus having no ejector in the return pipe. In each of the experimental examples (A) and (B), the amount of air supplied by the ejector was a ratio of air amount / concentrated return water = 1/1 (volume ratio).
【表１】 [Table 1]
【００１６】この表１により明らかなとおり、実験例
（Ｂ）によった場合、逆浸透膜６を透過した透過水中の
ＣＯ2 量は、透過水１リットル当たり３．８ｍｇＣａＣ
Ｏ3 に低減されており、比較例の場合の７ｍｇＣａＣＯ
3 に較べ大幅に改善されていることが実証された。ま
た、戻し管の先端部にスプレーノズルを接続しない実験
例（Ａ）によった場合でも、透過水中のＣＯ2 量は、透
過水１リットル当たり４．５ｍｇＣａＣＯ3 に低減して
いた。なお、比較例の場合のＴＡ量は透過水１リットル
当たり１２ｍｇＣａＣＯ3 であるのに対し、実験例
（Ｂ）の場合のＴＡ量は８．８ｍｇＣａＣＯ3 であるの
で、ＴＡ量の比は１２／８．８＝１．３６倍となる。し
たがって、逆浸透膜装置の透過水を更にイオン交換塔で
脱塩処理する場合は、本発明装置を使用した場合の方
が、当該割合でイオン交換塔内の陰イオン交換樹脂の通
水ライフが延びることとなる。As apparent from Table 1, according to the experimental example (B), the amount of CO 2 in the permeated water permeated through the reverse osmosis membrane 6 was 3.8 mg CaC per liter of permeated water.
O 3 , 7 mg CaCO 2 for the comparative example
It was proved that it was significantly improved compared to 3 . Further, even in the case of Experimental Example (A) in which the spray nozzle was not connected to the end of the return pipe, the amount of CO 2 in the permeated water was reduced to 4.5 mg CaCO 3 per liter of permeated water. The TA amount in the comparative example was 12 mg CaCO 3 per liter of permeated water, whereas the TA amount in the experimental example (B) was 8.8 mg CaCO 3 , so the ratio of the TA amount was 12/8. .8 = 1.36 times. Therefore, in the case where the permeated water of the reverse osmosis membrane device is further desalted in the ion exchange tower, the water flow life of the anion exchange resin in the ion exchange tower is higher in the case where the device of the present invention is used. Will be extended.
【００１７】[0017]
【発明の効果】以上のように、本発明脱塩水製造装置に
よった場合は、従来のような大型の脱炭酸塔を逆浸透膜
装置の前段に設備しなくても、良好に被処理水中の遊離
二酸化炭素を軽減することができ、そのため、後段にイ
オン交換塔が接続されている場合は、当該イオン交換塔
内に充填されている陰イオン交換樹脂に掛かる負荷を大
幅に軽減することができ、当該イオン交換樹塔の通水ラ
イフを延ばすことが可能となった。したがって、研究室
や実験室規模等の比較的小規模で行われる脱塩水製造プ
ロセスに最適の装置を提供することができるものであ
る。As described above, in the case of using the desalinated water production apparatus of the present invention, it is possible to satisfactorily treat the water to be treated without using a conventional large-sized decarbonation tower in front of the reverse osmosis membrane apparatus. Free carbon dioxide can be reduced, and therefore, when an ion exchange tower is connected at the subsequent stage, the load on the anion exchange resin filled in the ion exchange tower can be significantly reduced. As a result, the water flow life of the ion exchange tower can be extended. Therefore, it is possible to provide an apparatus optimal for a desalinated water production process performed on a relatively small scale such as a laboratory or a laboratory.
【図１】本発明脱塩水製造装置の一実施例を示す概略図
である。FIG. 1 is a schematic view showing one embodiment of a desalinated water producing apparatus of the present invention.
【図２】本発明脱塩水製造装置の他の実施例を示す概略
図である。FIG. 2 is a schematic diagram showing another embodiment of the desalinated water producing apparatus of the present invention.
１：原水貯槽 ２：原水供給管 ３：送水管 ４：逆浸透膜装置 ５：ポンプ ６：逆浸透膜 ７：戻し管 ８：排水管 ９：エゼクタ １０：スプレーノズル １１：先端部 １２：排気管 １３：出口管 １４：バルブ １５：バルブ 1: Raw water storage tank 2: Raw water supply pipe 3: Water supply pipe 4: Reverse osmosis membrane device 5: Pump 6: Reverse osmosis membrane 7: Return pipe 8: Drain pipe 9: Ejector 10: Spray nozzle 11: Tip 12: Exhaust pipe 13: Outlet pipe 14: Valve 15: Valve
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平２−52088（ＪＰ，Ａ) 特開 昭58−186490（ＪＰ，Ａ) 特開 平５−220480（ＪＰ，Ａ) 特開 昭59−32990（ＪＰ，Ａ) 特開 平２−290287（ＪＰ，Ａ) 特開 昭63−77588（ＪＰ，Ａ) 特開 昭62−91204（ＪＰ，Ａ) 特開 昭62−273095（ＪＰ，Ａ) 特開 昭60−102906（ＪＰ，Ａ) 特開 平６−178971（ＪＰ，Ａ) 特開 平６−79144（ＪＰ，Ａ) 特開 平５−192658（ＪＰ，Ａ) 実開 平４−53494（ＪＰ，Ｕ) 実開 平３−66697（ＪＰ，Ｕ) 実開 昭61−8494（ＪＰ，Ｕ) (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 1/44 B01D 61/00 - 61/58 C02F 1/20 ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-2-52088 (JP, A) JP-A-58-186490 (JP, A) JP-A-5-220480 (JP, A) JP-A-59-186 32990 (JP, A) JP-A-2-290287 (JP, A) JP-A-63-77588 (JP, A) JP-A-62-91204 (JP, A) JP-A-62-273095 (JP, A) JP-A-60-102906 (JP, A) JP-A-6-178971 (JP, A) JP-A-6-79144 (JP, A) JP-A-5-192658 (JP, A) (JP, U) JP-A 3-66697 (JP, U) JP-A 61-8494 (JP, U) (58) Fields investigated (Int. Cl. 7 , DB name) C02F 1/44 B01D 61 / 00-61/58 C02F 1/20
Claims (2)
逆浸透膜装置に送り、逆浸透膜によって被処理水を透過
水と濃縮水とに分離し、濃縮水を戻し管を通じて原水貯
槽内に戻すようになした脱塩水製造装置において、前記
濃縮水の戻し管の管路中にエゼクタを付設し、戻し管を
流れる濃縮水の流速を利用して当該エゼクタより空気を
吸引し、気液接触により濃縮水中の遊離二酸化炭素を除
去するようになしたことを特徴とする脱塩水製造装置。1. The water to be treated in a raw water storage tank is sent to a reverse osmosis membrane device by a pump, the water to be treated is separated into permeated water and concentrated water by a reverse osmosis membrane, and the concentrated water is returned into the raw water storage tank through a return pipe. In the desalinated water producing apparatus adapted to return, an ejector is provided in the conduit of the return pipe of the concentrated water, air is sucked from the ejector using the flow rate of the concentrated water flowing through the return pipe, and gas-liquid contact is performed. A desalinated water producing apparatus characterized in that free carbon dioxide in concentrated water is removed by the method.
設し、戻し管を通じて原水貯槽内に戻される濃縮水を、
当該スプレーノズルを介して原水貯槽内に散水するよう
になした請求項１記載の脱塩水製造装置。2. A spray nozzle is provided at an upper portion of the raw water storage tank, and the concentrated water returned to the raw water storage tank through a return pipe is provided.
2. The desalinated water producing apparatus according to claim 1, wherein water is sprinkled into the raw water storage tank via the spray nozzle.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP06081082A JP3100504B2 (en) | 1994-03-29 | 1994-03-29 | Demineralized water production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP06081082A JP3100504B2 (en) | 1994-03-29 | 1994-03-29 | Demineralized water production equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07265854A JPH07265854A (en) | 1995-10-17 |
| JP3100504B2 true JP3100504B2 (en) | 2000-10-16 |
Family
ID=13736474
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP06081082A Expired - Fee Related JP3100504B2 (en) | 1994-03-29 | 1994-03-29 | Demineralized water production equipment |
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| Country | Link |
|---|---|
| JP (1) | JP3100504B2 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4923266B2 (en) * | 2007-06-08 | 2012-04-25 | 株式会社松村組 | Contaminated water treatment equipment |
| JP5910675B2 (en) * | 2014-07-03 | 2016-04-27 | 栗田工業株式会社 | Pure water production apparatus and pure water production method |
| JP2020089803A (en) * | 2018-12-03 | 2020-06-11 | オルガノ株式会社 | Carbonic acid removing system, pure water producing apparatus, and method of removing carbonic acid |
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1994
- 1994-03-29 JP JP06081082A patent/JP3100504B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH07265854A (en) | 1995-10-17 |
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