JPH06254553A - Apparatus for producing pure water - Google Patents
Apparatus for producing pure waterInfo
- Publication number
- JPH06254553A JPH06254553A JP7077393A JP7077393A JPH06254553A JP H06254553 A JPH06254553 A JP H06254553A JP 7077393 A JP7077393 A JP 7077393A JP 7077393 A JP7077393 A JP 7077393A JP H06254553 A JPH06254553 A JP H06254553A
- Authority
- JP
- Japan
- Prior art keywords
- water
- raw water
- reverse osmosis
- osmosis membrane
- raw
- 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
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Water Treatment By Sorption (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は逆浸透膜装置を利用し，
飲料用，シャワ−用等の生活用水のほか工業用水も含む
広義の純水を製造するための純水製造装置の改良に関す
る。The present invention utilizes a reverse osmosis membrane device,
The present invention relates to improvement of a pure water production apparatus for producing pure water in a broad sense that includes industrial water as well as domestic water for beverages and showers.
【０００２】[0002]
【従来の技術】海水や河川の水から純水を得る方法とし
て，蒸発を利用するもの，凍結を利用するもの，
逆浸透膜装置を利用するものが知られている。この内，
の方法は河川だけでなく，海水を含めた原水から純水
を得る工業的手段として最近注目されている技術であ
る。ところで，逆浸透膜の温度特性は温度（℃）を横軸
に，透過流束補正係数を縦軸にとって表わした場合，図
２に示すような双曲線に類似した減衰状態の特性となっ
ている。同特性から，逆浸透膜は比較的高い温度で使用
する方が透過水量が増大することが示されている。逆浸
透膜装置を利用した従来の純水製造装置としては，たと
えば特公平４−６３７５５号公報に示すものがある。そ
の概略構成は図３に示すように，原水タンク１からポン
プＰ1により供給される原水を，ポンプＰ2により加圧し
て逆浸透膜装置２に供給し，逆浸透膜装置２の膜面を透
過した透過水を送水ポンプＰ3を介して透過水処理設備
３に供給した後，超純水使用設備４に送るようにした逆
浸透膜装置システムにおいて，原水タンク１と逆浸透膜
装置２との間に，原水タンク１からの原水を加熱する熱
交換器５とこの熱交換器５からの原水を加熱するヒ−ト
ポンプ６とを備えた熱回収装置７を設け，逆浸透膜装置
２からの濃縮水及び前記超純水使用設備４からの使用済
生産水を熱交換器５及びヒ−トポンプ６の蒸発器の加熱
側へ供給し，濃縮水及び使用済生産水の有する低温排熱
の回収により２５℃〜３０℃に加熱した原水を逆浸透膜
装置２へ供給するように構成されていた。2. Description of the Related Art As a method for obtaining pure water from seawater or river water, evaporation is used, freezing is used,
Those utilizing a reverse osmosis membrane device are known. Of these,
The method is a technology that has recently been drawing attention as an industrial means for obtaining pure water from not only rivers but also raw water including seawater. By the way, the temperature characteristic of the reverse osmosis membrane is a characteristic of a damping state similar to a hyperbola as shown in FIG. 2 when the temperature (° C.) is plotted on the horizontal axis and the permeation flux correction coefficient is plotted on the vertical axis. From the same characteristics, it is shown that the amount of permeated water increases when the reverse osmosis membrane is used at a relatively high temperature. As a conventional pure water producing apparatus using a reverse osmosis membrane apparatus, there is, for example, one disclosed in Japanese Examined Patent Publication No. 4-63755. Its schematic structure is shown in FIG. 3, the raw water supplied by the pump P 1 from the raw water tank 1, pressurized and supplied to the reverse osmosis membrane device 2 by a pump P 2, the film surface of the reverse osmosis membrane apparatus 2 In the reverse osmosis membrane device system, in which the permeated water that has permeated is supplied to the permeated water treatment equipment 3 via the water feed pump P 3, and then sent to the equipment 4 using ultrapure water, the raw water tank 1 and the reverse osmosis membrane equipment 2 Between the reverse osmosis membrane device 2 is provided a heat recovery device 7 having a heat exchanger 5 for heating the raw water from the raw water tank 1 and a heat pump 6 for heating the raw water from the heat exchanger 5. Concentrated water and the used product water from the ultrapure water using equipment 4 are supplied to the heat exchanger 5 and the heating side of the evaporator of the heat pump 6 to remove the low temperature exhaust heat of the concentrated water and the used product water. Raw water heated to 25 ° C to 30 ° C by recovery is supplied to the reverse osmosis membrane device 2. It has been configured to.
【０００３】[0003]
【発明が解決しようとする課題】従来のものは上記のよ
うに構成されるから，それ以前のものが大掛かりな蒸気
ボイラを熱源としていたものに比べれば，熱回収装置７
を使用しているため優れている。しかしながら，従来の
ものではこの熱回収装置７は熱交換器５とヒ−トポンプ
６により構成されているものであったから，原水の加熱
温度は前記のように３０℃が限度であるため逆浸透膜装
置の温度特性を有効に活用していないという問題点があ
った。この点を詳述すれば次の通りである。即ち，図２
に示すように，逆浸透膜装置は所定圧力で供給される原
水の供給温度が，たとえば１０℃というように基準温度
２５℃以下の温度の場合は透過流束補正係数はほぼ２位
であるが，標準温度の２５℃では前記補正係数は１に，
さらに，３０℃では約０．８５へと低下する。この透過
流束係数は同一の透過水量を得るための膜の面積に相当
するものであるから，原水の温度が２５℃の時の膜の面
積を１とすれば，原水の温度が３０℃なら膜の面積はそ
の０．８５で良いということを意味する。従って，同一
の膜面積のもので，２５℃と３０℃での透過水量で換算
すれば２５℃の透過水量を１とすると３０℃では約１．
１８（１／０．８５）となることを意味する。ところ
で，現在使用されている逆浸透膜装置の最高許容温度は
約４０℃であり，もし，原水を４０℃まで加温できるな
ら透過流束補正係数に従って同一の透過水量を得るため
の膜の面積は０．６３となる。このことは，基準温度の
２５℃のときの透過水量を１とした場合，これと同一の
膜面積での４０℃での透過水量は約１．５９（１／０．
６３）まで増大することを意味する。従って，同一の逆
浸透膜装置を使用し，４０℃まで加温して使用すれば標
準温度（２５℃）の１．５９倍の透過水量で純水を造水
できるのに対し，従来のものでは２５℃〜３０℃の加温
では１〜１．１７でしか使用していないことになり，こ
の点で逆浸透膜装置の温度特性を有効に使用していない
と述べたものである。本発明は従来のものの上記課題
（問題点）を解決するようにした純水製造装置を提供す
ることを目的とする。このため，逆浸透膜をその許容温
度で常に使用すれば効率の良い透過水量が得られるとい
う逆浸透膜の温度特性と，コ−ジェネレ−ション温水生
成装置を利用すれば逆浸透膜の許容温度まで原水を加熱
できるという点に着目し，効率的な純水製造装置を構成
しようとするものである。Since the conventional one is constructed as described above, the heat recovery device 7 is different from the conventional one which used a large-scale steam boiler as a heat source.
Is excellent because it uses. However, in the conventional device, the heat recovery device 7 is composed of the heat exchanger 5 and the heat pump 6, so that the heating temperature of the raw water is limited to 30 ° C. as described above, so that the reverse osmosis membrane is used. There is a problem that the temperature characteristics of the device are not effectively used. This point will be described in detail below. That is, FIG.
As shown in FIG. 5, the reverse osmosis membrane device has a permeation flux correction coefficient of approximately the second place when the supply temperature of raw water supplied at a predetermined pressure is a reference temperature of 25 ° C. or lower, such as 10 ° C. , At the standard temperature of 25 ° C, the correction coefficient is 1.
Furthermore, at 30 ° C., it drops to about 0.85. Since this permeation flux coefficient corresponds to the area of the membrane for obtaining the same amount of permeated water, if the area of the membrane when the temperature of the raw water is 25 ° C is 1, if the temperature of the raw water is 30 ° C, This means that the area of the film is 0.85. Therefore, if the permeated water amounts at 25 ° C and 30 ° C are converted into the permeated water amount at 25 ° C, the permeated water amount at 25 ° C is about 1.
It means that it becomes 18 (1 / 0.85). By the way, the maximum allowable temperature of the reverse osmosis membrane device currently used is about 40 ° C, and if the raw water can be heated up to 40 ° C, the area of the membrane to obtain the same amount of permeated water according to the permeation flux correction coefficient. Is 0.63. This means that when the permeated water amount at the reference temperature of 25 ° C. is 1, the permeated water amount at 40 ° C. in the same membrane area is about 1.59 (1/0.
It means increasing to 63). Therefore, if the same reverse osmosis membrane device is used and heated up to 40 ° C, pure water can be produced with a permeated water amount of 1.59 times the standard temperature (25 ° C). Therefore, it means that it is used only at 1-1.17 when heated at 25 ° C. to 30 ° C., and in this respect, the temperature characteristic of the reverse osmosis membrane device is not effectively used. It is an object of the present invention to provide a pure water producing apparatus that solves the above problems (problems) of the conventional ones. For this reason, the temperature characteristics of the reverse osmosis membrane are such that an efficient amount of permeated water can be obtained if the reverse osmosis membrane is always used at its allowable temperature, and the allowable temperature of the reverse osmosis membrane is increased by using the cogeneration hot water generator. It aims to construct an efficient pure water production system, focusing on the fact that raw water can be heated.
【０００４】[0004]
【課題を解決するための手段】本発明は上記課題を解決
するために，海水，河川水等の被処理用の原水，コ−ジ
ェネレ−ションシステムの発電装置駆動用のガスエンジ
ン等の原動機の排熱回収により水道水等を温水に変えて
循環供給するコ−ジェネレ−ション温水生成装置からの
温水を１次側に供給し，原水を後述する逆浸透膜装置の
許容温度まで加温する第１の熱交換器，この第１の熱交
換器で加温した原水を一旦貯蔵する原水タンク，この原
水タンクからの加温された原水を加圧する圧力ポンプ及
びこの圧力ポンプにより所定圧に加圧された所定温度の
原水を供給され，透過水を生成する逆浸透膜装置を備え
て構成した。この場合，逆浸透膜装置の透過水を，原水
を用いて冷却する第２の熱交換器を備えることが望まし
い。また，上記原水タンクと圧力ポンプの間に重金属以
外の有機物，バクテリア等を濾過するフィルタを設ける
ことが望ましい。さらに，上記逆浸透膜装置の透過水を
第２の熱交換器を経た後，さらにオゾン発生器等を用い
た殺菌装置により殺菌し，飲料水を生成することが望ま
しい。なお，上記純水製造装置の動力源への電源，その
他付帯設備への電源は，全て上記コ−ジェネレ−ション
発電装置から供給し，コ−ジェネレ−ションシステムと
一体的に構成されることが望ましい。In order to solve the above problems, the present invention provides a raw water for treatment such as seawater and river water, and a prime mover such as a gas engine for driving a power generator of a cogeneration system. Hot water from a cogeneration hot water generator is supplied to the primary side to circulate and supply tap water to hot water by recovering exhaust heat, and the raw water is heated to the allowable temperature of the reverse osmosis membrane device described later. No. 1 heat exchanger, raw water tank for temporarily storing raw water heated by the first heat exchanger, pressure pump for pressurizing heated raw water from the raw water tank, and pressurization to a predetermined pressure by this pressure pump The reverse osmosis membrane device which is supplied with the raw water at the predetermined temperature and produces the permeated water is configured. In this case, it is desirable to provide a second heat exchanger that cools the permeated water of the reverse osmosis membrane device using raw water. Further, it is desirable to provide a filter for filtering organic substances other than heavy metals, bacteria, etc. between the raw water tank and the pressure pump. Further, it is desirable that the permeated water of the reverse osmosis membrane device is passed through the second heat exchanger and then further sterilized by a sterilizing device using an ozone generator or the like to produce drinking water. It should be noted that the power source for the power source of the pure water producing apparatus and the power source for other incidental equipment are all supplied from the cogeneration power generation apparatus and may be configured integrally with the cogeneration system. desirable.
【０００５】[0005]
【作用】本発明の純水製造装置では，海水又は河川水等
の原水を，ガスエンジン等の高温の排熱を利用して加温
して得た温水（たとえば８５℃の温水）を熱源として逆
浸透膜装置の許容温度（たとえば４０℃）まで常時加温
した状態で，逆浸透膜装置に対して所定の圧力をかけて
供給するようにしたから，逆浸透膜装置の温度特性が有
効に利用され透過水量は大幅に増大される。また，逆浸
透膜装置より得られた純水は，原水を利用して冷却する
ようにすれば，たとえば２０℃〜２５℃という適正な温
度にまで簡単に冷却され，給水できる。さらに，この給
水を殺菌装置または２次処理装置により飲料水または工
業用水に生成される。なお，逆浸透膜装置に加温された
原水を供給するに当っては，前処理としてのフィルタを
用いれば有機物等が適正に除去される。In the pure water producing apparatus of the present invention, hot water obtained by heating raw water such as seawater or river water using high temperature exhaust heat of a gas engine (for example, hot water at 85 ° C.) is used as a heat source. The temperature characteristic of the reverse osmosis membrane device becomes effective because the reverse osmosis membrane device is supplied with a predetermined pressure while being constantly heated to the allowable temperature of the reverse osmosis membrane device (for example, 40 ° C.). The amount of permeated water used is greatly increased. If pure water obtained from the reverse osmosis membrane device is cooled by using raw water, the pure water can be easily cooled to an appropriate temperature of, for example, 20 ° C to 25 ° C and can be supplied with water. Further, this water supply is generated into drinking water or industrial water by a sterilizer or secondary treatment device. When supplying the heated raw water to the reverse osmosis membrane device, organic matter and the like are properly removed by using a filter as a pretreatment.
【０００６】[0006]
【実施例】以下図１に示す一実施例により本発明を具体
的に説明する。同図において，１０は海水，河川水等の
原水を供給する供給用のポンプ，１１は第２の熱交換器
で，この働きについては後述する。１２は第１の熱交換
器で，この１次側にはコ−ジェネレ−ション温水生成装
置１３からの温水が供給ポンプ１４を介して循環される
ようになっている。コ−ジェネレ−ション温水生成装置
１３は，図示のように，たとえば，交流発電機等のコ−
ジェネレ−ション発電装置１５を駆動するためのガスエ
ンジン，ディ−ゼルエンジン，ガスタ−ビン等の原動機
１６，この原動機１６の排気管１７を通過する排気ガス
の高熱を利用し水道水等を用いて，たとえば８５℃の温
水を得るためのジャケット等の配管１８及び戻り経路に
挿入されるラジェ−タ１９等により構成される。２０は
原水タンクで，第１の熱交換器１２により約４０℃に加
温された原水を貯蔵する。２１は常時開状態の弁，２２
は原水供給用の供給ポンプである。２３はフィルタで，
砂濾過器，活性炭等の濾過層を備え，原水中のＣａ，Ｎ
ａ，Ｍｇ等の重金属以外の有機物，バクテリア等の不純
物を除去する。２４及び２５は夫々加圧前及び加圧後の
圧力を計るための圧力計，２６は加圧用の圧力ポンプ
で，同ポンプ２６により，たとえば５０［ｋｇ／ｃｍ2
Ｇ］程度の所要圧力となるように原水を加圧する。２７
は逆浸透膜装置で，同装置２７を透過して得られた純水
は常時開状態の弁２８を介して第２の熱交換器１１の２
次側に供給され，同交換器１１の１次側を通過する原水
により給水可能な温度（たとえば，２０℃〜２５℃）へ
と冷却し透過水タンク２９にて貯蔵するようにしてい
る。なお，逆浸透膜装置２７で発生する濃縮水は常時開
状態の圧力調整弁３０及び常時開状態の弁３１を介して
外部に放水されるようになっている。３２は圧力調整弁
３０に並列に接続された常時閉状態のバイパス弁，３３
も常時閉状態の弁で，同弁３３の先端は原水タンク２０
に臨んでいる。３４はポンプ２６と原水タンク２０間に
設けられる分岐経路に挿入された所定の開度に調整され
た常時開状態の調整弁である。３５は逆浸透膜装置２７
の透過水側と原水タンク２０とを結ぶ分岐経路中に挿入
された常時閉状態の弁である。３６は透過水タンク２９
に収納された淡水を給水するための供給ポンプである。
３７も供給ポンプで，殺菌装置３８を経て飲料水を供給
するためのものである。３９はオゾン発生器で，プラズ
マ入力を受けて，殺菌装置３８内に導入した導管の先端
部よりオゾンを発生させ，殺菌装置３８に供給された淡
水を殺菌し，飲料に適した良質の水に変換するようにし
ている。４０はオゾン発生後の排ガスを排出するための
排管，４１は供給ポンプ，４２は限界濾過膜装置等の工
業用水となる超純水とするための２次処理装置である。
以上の１０〜４２により本発明の純水製造装置が構成さ
れる。なお，図示しないが，上記純水製造装置の動力源
への電源，その他付帯設備への電源は，全てコ−ジェネ
レ−ション発電装置１５から供給し，コ−ジェネレ−シ
ョンシステムと一体的に構成するのが望ましい。EXAMPLES The present invention will be described in detail with reference to an example shown in FIG. In the figure, 10 is a pump for supplying raw water such as seawater and river water, and 11 is a second heat exchanger, the function of which will be described later. Reference numeral 12 is a first heat exchanger, on the primary side of which hot water from a cogeneration hot water generator 13 is circulated via a supply pump 14. The cogeneration hot water generator 13 is, for example, as shown in the figure, a cogeneration device such as an AC generator.
A prime mover 16 such as a gas engine, a diesel engine, a gas turbine, etc. for driving the generation power generator 15, and the high heat of the exhaust gas passing through the exhaust pipe 17 of the prime mover 16 is used by using tap water or the like. , A pipe 18 such as a jacket for obtaining hot water at 85 ° C. and a radiator 19 inserted in the return path. A raw water tank 20 stores the raw water heated to about 40 ° C. by the first heat exchanger 12. 21 is a normally open valve, 22
Is a supply pump for supplying raw water. 23 is a filter,
Equipped with a sand filter and a filter layer such as activated carbon, Ca, N in raw water
Organic substances other than heavy metals such as a and Mg and impurities such as bacteria are removed. Reference numerals 24 and 25 are pressure gauges for measuring pressures before and after pressurization, and 26 is a pressure pump for pressurization, which is, for example, 50 [kg / cm 2
Pressurize the raw water so that the required pressure is about G]. 27
Is a reverse osmosis membrane device, and the pure water obtained by passing through the device 27 is passed through the valve 28 in the normally open state to
The water supplied to the secondary side and cooled by the raw water passing through the primary side of the exchanger 11 (for example, 20 ° C. to 25 ° C.) is cooled and stored in the permeated water tank 29. It should be noted that the concentrated water generated in the reverse osmosis membrane device 27 is discharged to the outside via the normally open pressure adjusting valve 30 and the normally open valve 31. Reference numeral 32 is a normally-closed bypass valve connected in parallel to the pressure control valve 30, and 33
Is a normally closed valve, and the tip of the valve 33 is the raw water tank 20.
Facing. Reference numeral 34 is a normally open adjustment valve which is inserted into a branch path provided between the pump 26 and the raw water tank 20 and which is adjusted to a predetermined opening degree. 35 is a reverse osmosis membrane device 27
It is a normally closed valve inserted in a branch path connecting the permeated water side and the raw water tank 20. 36 is the permeate tank 29
It is a supply pump for supplying fresh water stored in.
37 is also a supply pump for supplying drinking water through the sterilizer 38. 39 is an ozone generator, which receives plasma input and generates ozone from the tip of the conduit introduced into the sterilizer 38 to sterilize the fresh water supplied to the sterilizer 38 to produce high-quality water suitable for drinking. I'm trying to convert. Reference numeral 40 is a discharge pipe for discharging the exhaust gas after ozone generation, 41 is a supply pump, and 42 is a secondary treatment device for producing ultrapure water that is industrial water such as an ultrafiltration membrane device.
The pure water producing apparatus of the present invention is constituted by the above 10 to 42. Although not shown, the power source for the power source of the pure water producing apparatus and the power source for other incidental equipment are all supplied from the cogeneration system 15 and integrated with the cogeneration system. It is desirable to do.
【０００７】以上の構成において，コ−ジェネレ−ショ
ン温水生成装置１３により第１の熱交換器１２の１次側
に約８５℃の温水が循環されている状態において，海
水，河川水等の原水がポンプ１０により第２の熱交換器
１１を経て第１の熱交換器１２に供給される。従って，
この熱交換器１２を通過した原水は約４０℃に加温さ
れ，原水タンク２０に一旦貯えられた後，弁２１，ポン
プ２２を介してフィルタ２３に供給され，フィルタ２３
により重金属以外の有機物，バクテリア等が濾過され，
圧力ポンプ２６を介して，たとえば５０［ｋｇ／ｃｍ2
Ｇ］等の所定の圧力に加圧されて，逆浸透膜装置２７に
供給される。よって，逆浸透膜装置２７の膜面を透過し
た純水はまだ４０℃程度の温度のものであるが，第２の
熱交換器１１の２次側を通過する際，同交換器１１の１
次側を通過する原水によって２０℃〜２５℃程度の温度
の淡水に冷却されて，透過水タンク２９に一旦貯えられ
る。同タンク２９の淡水は手洗い，シャワ−等の給水の
場合には，ポンプ３６によりそのまま給水され，飲料用
の場合はポンプ３７及び殺菌装置３８を介して殺菌され
た水が給水される。また，工業用水としては，２次処理
装置４２を経た超純水が使用される。なお，逆浸透膜装
置２７で生じた濃縮水は弁３０，３１を介して外部に放
水される。ところで，本発明の純水製造装置では，上記
のように原水を逆浸透膜装置２７に対して加圧して供給
する前に，第１の熱交換器１２により逆浸透膜装置２７
の最高許容温度である４０℃にまで加温するものである
から，逆浸透膜装置２７は図２に示すようにその温度特
性としては基準温度（２５℃）と同一の透過水量を得る
のに，膜面積で６３％で良くなり，膜面積を一定とした
場合には透過水量は基準温度の１．５９倍即ち，５９％
も透過水量を増大できるようにした点に，その構成上の
特徴がある。なお，図１で破線で示した配管ル−トは本
装置の立ち上がり前のテストや設定または保守の時等に
使用するル−トであり，従って同ル−トに配置された弁
３３，３４及び３５は夫々常時閉状態で，そのような使
用状態にのみ開状態となる。In the above-described structure, raw water such as seawater and river water is supplied by the cogeneration hot water generator 13 while hot water of about 85 ° C. is circulated on the primary side of the first heat exchanger 12. Is supplied to the first heat exchanger 12 via the second heat exchanger 11 by the pump 10. Therefore,
The raw water that has passed through the heat exchanger 12 is heated to about 40 ° C., once stored in the raw water tank 20, and then supplied to the filter 23 via the valve 21 and the pump 22, and the filter 23
Filter organic substances other than heavy metals, bacteria, etc.
Via the pressure pump 26, for example, 50 [kg / cm 2
The pressure is increased to a predetermined pressure such as G] and is supplied to the reverse osmosis membrane device 27. Therefore, the pure water that has passed through the membrane surface of the reverse osmosis membrane device 27 is still at a temperature of about 40 ° C., but when passing through the secondary side of the second heat exchanger 11, the pure water of
It is cooled to fresh water having a temperature of about 20 ° C. to 25 ° C. by the raw water passing through the next side and is temporarily stored in the permeated water tank 29. The fresh water in the tank 29 is supplied as it is by the pump 36 in the case of hand washing, water supply such as shower, and in the case of drinking water, the sterilized water is supplied through the pump 37 and the sterilizer 38. Moreover, as the industrial water, ultrapure water that has passed through the secondary treatment device 42 is used. The concentrated water produced in the reverse osmosis membrane device 27 is discharged to the outside via the valves 30 and 31. By the way, in the pure water producing apparatus of the present invention, before the raw water is pressurized and supplied to the reverse osmosis membrane apparatus 27 as described above, the reverse osmosis membrane apparatus 27 is operated by the first heat exchanger 12.
Since it is heated up to 40 ° C. which is the maximum allowable temperature of the reverse osmosis membrane device 27, the reverse osmosis membrane device 27 has the same temperature characteristic as that of the reference temperature (25 ° C.) as shown in FIG. The membrane area is improved to 63%, and when the membrane area is constant, the permeated water amount is 1.59 times the reference temperature, that is, 59%.
Another feature of the system is that it can increase the amount of permeated water. The pipe route shown by the broken line in FIG. 1 is a route used for a test before starting the apparatus, at the time of setting or maintenance, and therefore, the valves 33, 34 arranged in the route are used. Reference numerals 35 and 35 are normally closed, and are opened only in such a usage state.
【０００８】[0008]
【発明の効果】本発明は上記のように逆浸透膜装置に所
定圧力で加圧して供給する海水等の原水をコ−ジェネレ
−ション温水生成装置を熱源に利用して加温し，また上
記装置で透過した水は原水を利用して冷却するようにし
たものであるから，次のような優れた効果を有する。 逆浸透膜装置に供給する原水はコ−ジェネレ−ション
温水生成装置を用いることにより逆浸透膜装置の最高許
容温度（たとえば，４０℃）まで加温するようにしたか
ら，従来のヒ−トポンプ主体の熱回収装置による加温温
度（２５℃〜３０℃）に比べ透過水量を大幅に増大でき
る。即ち，図２の温度特性によれば，従来のもので３０
℃の原水を使用するものに比べて，１．５８７／１．１
７６≒１．３４９即ち，約３４．９％も透過水量が増大
できることが確認された。さらに，図２の温度特性より
判るように，近い将来，逆透過膜装置の最高許容温度が
現在の約４０℃よりさらに増大されることは十分考えら
れるので，この場合には，コ−ジェネレ−ション温水生
成装置では４０℃以上に原水を加温することは十分可能
であるから，この許容温度の上昇に伴い，原水を加温す
れば，さらに，透過水量を増大させることが可能であ
る。 また，本発明のものでは，逆浸透膜装置への供給側の
原水を約４０℃に加温したため，透過水の温度もその分
上昇して約４０℃となったが，この透過水の冷却は原水
を用いて冷却するようにしたため，特別の冷却源を必要
とせず，冷却することができる。 また，逆浸透膜装置に原水を加圧供給する前に，フィ
ルタ２３により重金属以外の有機物，バクテリアを除去
し，逆浸透膜装置２７により重金属成分を除去するよう
に分担したから，原水として河川水は勿論，海水を用い
ても純水を効率良く得ることができる。さらに，透過水
を殺菌装置を通せば飲料水として使用でき，殺菌を行わ
なくても手洗いやシャワ−用の水としては十分に使用が
できる。また，さらに所要の２次処理を行うことにより
工業用水の生成も容易に行うことができる。 本発明で原水の加温に使用されるコ−ジェネレ−ショ
ン温水生成装置は，ガスエンジン等の排熱回収を利用す
るものであり，コ−ジェネレ−ション発電装置の電源設
備の一要素により容易に一体的に構成できるものであ
り，これと図１に示した逆浸透膜装置を主体に本発明を
構成することが容易である。従って，本発明の純水製造
装置は都市における水道水を補充する給水源としては勿
論のこと，海水はあるが水道水の配管設備がされていな
いような僻地における純水製造装置としてもその実益は
大である。As described above, the present invention heats raw water such as seawater supplied to the reverse osmosis membrane device at a predetermined pressure by using the cogeneration hot water generator as a heat source, and Since the water permeated by the device is cooled by using the raw water, it has the following excellent effects. The raw water supplied to the reverse osmosis membrane device is heated to the maximum allowable temperature of the reverse osmosis membrane device (for example, 40 ° C.) by using a cogeneration hot water generator. The permeated water amount can be greatly increased as compared with the heating temperature (25 ° C to 30 ° C) by the heat recovery device. That is, according to the temperature characteristics of FIG.
1.587 / 1.1 compared to the one using raw water at ℃
It was confirmed that the permeated water amount could be increased by 76≈1.349, that is, about 34.9%. Further, as can be seen from the temperature characteristic of FIG. 2, it is fully conceivable that the maximum permissible temperature of the reverse permeable membrane device will be further increased from the present approximately 40 ° C. in the near future. Since it is sufficiently possible to heat the raw water to 40 ° C or higher in the hot water generator, it is possible to further increase the amount of permeated water by warming the raw water as the allowable temperature rises. Further, in the case of the present invention, since the raw water on the supply side to the reverse osmosis membrane device was heated to about 40 ° C, the temperature of the permeated water also increased by that amount to about 40 ° C, but this permeated water was cooled. Since it uses raw water for cooling, it can be cooled without requiring a special cooling source. Further, before the raw water is pressurized and supplied to the reverse osmosis membrane device, the filter 23 removes organic substances other than heavy metals and bacteria, and the reverse osmosis membrane device 27 removes heavy metal components. Of course, pure water can be efficiently obtained by using seawater. Further, the permeated water can be used as drinking water by passing it through a sterilizer, and can be sufficiently used as water for hand washing and shower without sterilization. Further, industrial water can be easily produced by further performing the required secondary treatment. The cogeneration hot water generator used for heating the raw water in the present invention utilizes exhaust heat recovery of a gas engine or the like, and is easily realized by one element of the power supply equipment of the cogeneration power generator. It is easy to configure the present invention mainly with this and the reverse osmosis membrane device shown in FIG. Therefore, the pure water producing apparatus of the present invention is not only used as a water supply source for supplementing tap water in cities, but also as a pure water producing apparatus in a remote area where there is seawater but no plumbing system for tap water is provided. Is large.
【図１】本発明の一実施例を示す配管も含む系統図であ
る。FIG. 1 is a system diagram including piping showing an embodiment of the present invention.
【図２】本発明と従来例を比較するために示した透過流
束補正係数−温度の特性図である。FIG. 2 is a characteristic diagram of permeation flux correction coefficient-temperature shown for comparing the present invention and a conventional example.
【図３】従来例の構成を示す系統図である。FIG. 3 is a system diagram showing a configuration of a conventional example.
１１，１２：熱交換器 １３：コ−ジェネレ−ション温水生成装置 ２０：原水タンク ２３：フィルタ ２６：圧力ポンプ ２７：逆浸透膜装置 ２９：透過水タンク ３８：殺菌装置 ４２：２次処理装置 11, 12: Heat exchanger 13: Co-generation hot water generator 20: Raw water tank 23: Filter 26: Pressure pump 27: Reverse osmosis membrane device 29: Permeate water tank 38: Sterilizer 42: Secondary treatment device
Claims (5)
ジェネレ−ションシステムの発電装置駆動用のガスエン
ジン等の原動機の排熱回収により水道水等を温水に変え
て循環供給するコ−ジェネレ−ション温水生成装置から
の温水を１次側に供給し，原水を後述する逆浸透膜装置
の許容温度まで加温する第１の熱交換器，この第１の熱
交換器で加温した原水を一旦貯蔵する原水タンク，この
原水タンクからの加温された原水を加圧する圧力ポンプ
及びこの圧力ポンプにより所定圧に加圧された所定温度
の原水を供給され，透過水を生成する逆浸透膜装置を備
えたことを特徴とする純水製造装置。1. Raw water or coal for treatment such as seawater and river water
Hot water from a cogeneration hot water generator is supplied to the primary side by circulating wastewater such as tap water to warm water by recovery of exhaust heat from a prime mover such as a gas engine for driving a generation system generator, A first heat exchanger that heats the raw water to an allowable temperature of a reverse osmosis membrane device described later, a raw water tank that temporarily stores the raw water heated by the first heat exchanger, and a warmed water from this raw water tank A pure water production apparatus comprising a pressure pump for pressurizing raw water and a reverse osmosis membrane device for generating permeated water by supplying raw water at a predetermined temperature pressurized to a predetermined pressure by the pressure pump.
いて冷却する第２の熱交換器を備えた請求項１記載の純
水製造装置。2. The pure water producing apparatus according to claim 1, further comprising a second heat exchanger that cools the permeated water of the reverse osmosis membrane apparatus using raw water.
属以外の有機物，バクテリア等を濾過するフィルタを設
けるようにした請求項１又は２のいずれかに記載の純水
製造装置。3. The pure water production apparatus according to claim 1, wherein a filter for filtering organic substances other than heavy metals, bacteria and the like is provided between the raw water tank and the pressure pump.
換器を経た後，さらにオゾン発生器等を用いた殺菌装置
により殺菌し，飲料水を生成するようにした請求項１ま
たは２のいずれかに記載の純水製造装置。4. The permeated water of the reverse osmosis membrane device is passed through a second heat exchanger and then sterilized by a sterilizer using an ozone generator or the like to produce drinking water. 2. The pure water producing device according to any one of 2.
の他付帯設備への電源は全て上記コ−ジェネレ−ション
発電装置から供給し，コ−ジェネレ−ションシステムと
一体的に構成されるようにした請求項１または２のいず
れかに記載の純水製造装置。5. The power source for the power source of the pure water producing apparatus and the power source for other incidental equipment are all supplied from the cogeneration power generation apparatus, and are integrated with the cogeneration system. The pure water production apparatus according to claim 1, wherein the pure water production apparatus is configured as described above.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7077393A JPH06254553A (en) | 1993-03-08 | 1993-03-08 | Apparatus for producing pure water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7077393A JPH06254553A (en) | 1993-03-08 | 1993-03-08 | Apparatus for producing pure water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06254553A true JPH06254553A (en) | 1994-09-13 |
Family
ID=13441182
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7077393A Pending JPH06254553A (en) | 1993-03-08 | 1993-03-08 | Apparatus for producing pure water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06254553A (en) |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002059195A (en) * | 2000-08-21 | 2002-02-26 | Zenkichi Abiko | Water treatment plant of marine deep water |
| JP2005052793A (en) * | 2003-08-07 | 2005-03-03 | Japan Cost Planning:Kk | Purified water feed device having thermoelectric cogeneration apparatus |
| JP2009183800A (en) * | 2008-02-01 | 2009-08-20 | Panasonic Corp | Pure water production method and apparatus |
| CN101844821A (en) * | 2010-05-28 | 2010-09-29 | 济南市琦泉热电有限责任公司 | Equipment and technology for improving reverse osmosis efficiency by waste heat recovery |
| JP2010264385A (en) * | 2009-05-14 | 2010-11-25 | Tohoku Univ | Electrodialysis machine |
| CN102190344A (en) * | 2010-03-08 | 2011-09-21 | 慈溪市龙巍电器有限公司 | Composite type dual-water-supplying reverse osmosis water purifier with brominated resin filter element |
| US8221628B2 (en) | 2010-04-08 | 2012-07-17 | Toyota Motor Engineering & Manufacturing North America, Inc. | Method and system to recover waste heat to preheat feed water for a reverse osmosis unit |
| WO2013031544A1 (en) * | 2011-08-26 | 2013-03-07 | 株式会社日立プラントテクノロジー | Desalinization system and desalinization method |
| US8505324B2 (en) | 2010-10-25 | 2013-08-13 | Toyota Motor Engineering & Manufacturing North America, Inc. | Independent free cooling system |
| WO2013121547A1 (en) * | 2012-02-15 | 2013-08-22 | 三菱重工業株式会社 | Seawater desalination system |
| JP2013193012A (en) * | 2012-03-19 | 2013-09-30 | Toshiba Corp | Seawater desalination device |
| JP2013193013A (en) * | 2012-03-19 | 2013-09-30 | Toshiba Corp | Seawater desalination device |
| US9314742B2 (en) | 2010-03-31 | 2016-04-19 | Toyota Motor Engineering & Manufacturing North America, Inc. | Method and system for reverse osmosis predictive maintenance using normalization data |
| WO2016111371A1 (en) * | 2015-01-09 | 2016-07-14 | 東レ株式会社 | Method for improving inhibition performance of semipermeable membrane, semipermeable membrane, and semipermeable membrane water production device |
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-
1993
- 1993-03-08 JP JP7077393A patent/JPH06254553A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002059195A (en) * | 2000-08-21 | 2002-02-26 | Zenkichi Abiko | Water treatment plant of marine deep water |
| JP2005052793A (en) * | 2003-08-07 | 2005-03-03 | Japan Cost Planning:Kk | Purified water feed device having thermoelectric cogeneration apparatus |
| JP2009183800A (en) * | 2008-02-01 | 2009-08-20 | Panasonic Corp | Pure water production method and apparatus |
| JP2010264385A (en) * | 2009-05-14 | 2010-11-25 | Tohoku Univ | Electrodialysis machine |
| CN102190344A (en) * | 2010-03-08 | 2011-09-21 | 慈溪市龙巍电器有限公司 | Composite type dual-water-supplying reverse osmosis water purifier with brominated resin filter element |
| US9314742B2 (en) | 2010-03-31 | 2016-04-19 | Toyota Motor Engineering & Manufacturing North America, Inc. | Method and system for reverse osmosis predictive maintenance using normalization data |
| US8221628B2 (en) | 2010-04-08 | 2012-07-17 | Toyota Motor Engineering & Manufacturing North America, Inc. | Method and system to recover waste heat to preheat feed water for a reverse osmosis unit |
| CN101844821A (en) * | 2010-05-28 | 2010-09-29 | 济南市琦泉热电有限责任公司 | Equipment and technology for improving reverse osmosis efficiency by waste heat recovery |
| US8505324B2 (en) | 2010-10-25 | 2013-08-13 | Toyota Motor Engineering & Manufacturing North America, Inc. | Independent free cooling system |
| WO2013031544A1 (en) * | 2011-08-26 | 2013-03-07 | 株式会社日立プラントテクノロジー | Desalinization system and desalinization method |
| CN103370279A (en) * | 2012-02-15 | 2013-10-23 | 三菱重工业株式会社 | Seawater desalination system |
| WO2013121547A1 (en) * | 2012-02-15 | 2013-08-22 | 三菱重工業株式会社 | Seawater desalination system |
| JP2013193012A (en) * | 2012-03-19 | 2013-09-30 | Toshiba Corp | Seawater desalination device |
| JP2013193013A (en) * | 2012-03-19 | 2013-09-30 | Toshiba Corp | Seawater desalination device |
| WO2016111371A1 (en) * | 2015-01-09 | 2016-07-14 | 東レ株式会社 | Method for improving inhibition performance of semipermeable membrane, semipermeable membrane, and semipermeable membrane water production device |
| WO2016111372A1 (en) * | 2015-01-09 | 2016-07-14 | 東レ株式会社 | Method for improving blocking capability of semipermeable membrane, semipermeable membrane, and semipermeable-membrane desalination apparatus |
| WO2016111370A1 (en) * | 2015-01-09 | 2016-07-14 | 東レ株式会社 | Water treatment method |
| JPWO2016111371A1 (en) * | 2015-01-09 | 2017-10-19 | 東レ株式会社 | Method of improving semi-permeable membrane blocking performance, semi-permeable membrane, semi-permeable membrane water generator |
| JPWO2016111372A1 (en) * | 2015-01-09 | 2017-10-19 | 東レ株式会社 | Method of improving semi-permeable membrane blocking performance, semi-permeable membrane, semi-permeable membrane water generator |
| CN118139821A (en) * | 2021-10-25 | 2024-06-04 | 奥加诺株式会社 | Water treatment system and water treatment method |
| JP7806183B1 (en) * | 2024-11-15 | 2026-01-26 | 野村マイクロ・サイエンス株式会社 | Temperature control system, temperature control method, sterilization method for medical water production equipment, and secondary pure water production method |
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