JPS6369507A - Reverse-osmosis membrane concentrator - Google Patents
Reverse-osmosis membrane concentratorInfo
- Publication number
- JPS6369507A JPS6369507A JP21464886A JP21464886A JPS6369507A JP S6369507 A JPS6369507 A JP S6369507A JP 21464886 A JP21464886 A JP 21464886A JP 21464886 A JP21464886 A JP 21464886A JP S6369507 A JPS6369507 A JP S6369507A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- concentrated
- osmosis membrane
- liquid
- liq
- 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
- 239000012528 membrane Substances 0.000 title claims abstract description 60
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 56
- 239000007788 liquid Substances 0.000 claims description 84
- 239000002994 raw material Substances 0.000 claims description 16
- 239000012466 permeate Substances 0.000 claims description 13
- 238000000605 extraction Methods 0.000 claims description 10
- 238000007599 discharging Methods 0.000 claims description 3
- 239000012141 concentrate Substances 0.000 abstract description 17
- 238000002347 injection Methods 0.000 description 10
- 239000007924 injection Substances 0.000 description 10
- 238000010586 diagram Methods 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 239000010720 hydraulic oil Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000003204 osmotic effect Effects 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 206010011224 Cough Diseases 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、被濃縮液を高圧で逆浸透膜に供給して、当該
逆浸透膜を透過する透過液と透過しない濃縮液とに分離
する逆浸透膜濃縮装置に関するものである。[Detailed Description of the Invention] [Industrial Application Field] The present invention supplies a liquid to be concentrated to a reverse osmosis membrane under high pressure and separates it into a permeated liquid that passes through the reverse osmosis membrane and a concentrated liquid that does not pass through the membrane. This invention relates to a reverse osmosis membrane concentrator.
従来この種の逆浸透膜濃縮装置は、第５図に示すように
逆浸透膜槽１と被濃縮液の循環ポンプ２との間を閉ルー
プの循環管路３に構成し、この閉ループ循環管路３に、
加圧ポンプ４付き原料被濃縮液注入管路５にて被濃縮液
を高圧（５０〜６０ｋｇ ／ ｃＩりにして供給するこ
とにより、前記逆浸透膜槽１における逆浸透膜を通過し
た透過液を透過液取出管路６より機外に取り出す一方、
濃縮液を定圧排水弁７付き濃縮液取出管路８から系外に
排出するようにしたものであった。Conventionally, this type of reverse osmosis membrane concentration device has a closed loop circulation pipe 3 between the reverse osmosis membrane tank 1 and the circulation pump 2 for the liquid to be concentrated, as shown in FIG. 3,
By supplying the liquid to be concentrated at high pressure (50 to 60 kg/cI) through the raw material liquid to be concentrated injection line 5 equipped with the pressure pump 4, the permeate that has passed through the reverse osmosis membrane in the reverse osmosis membrane tank 1 is While the permeated liquid is taken out of the machine from the permeate extraction pipe 6,
The concentrated liquid was discharged out of the system from a concentrated liquid extraction pipe line 8 equipped with a constant pressure drain valve 7.
そして、このものは濃縮液と透過液との分離が連続運転
にてできる利点を有する反面、加圧ポンプ４は、透過液
量と濃縮液量との合計量の原料被濃縮液を高圧に加圧し
て供給しなければならないから、該加圧ポンプ４におけ
る動力消費が大きくて、運転経費が著しく嵩む点に問題
があった。While this device has the advantage of being able to separate the concentrate and permeate in continuous operation, the pressurizing pump 4 applies the total amount of the raw material to be concentrated, the amount of the permeate and the concentrate, to high pressure. Since it has to be supplied under pressure, the pressure pump 4 consumes a large amount of power, resulting in a significant increase in operating costs.
そこで先行技術としての特公昭５９−４８１２２号公報
は、その公報における第４図に記載され、且つ、本明細
書に添付した第６図に示すように、逆浸透膜槽ｌと被濃
縮液の循環ポンプ２との間を閉ループの管路に形成した
閉ループ循環管路３の途中に密閉タンク９を設ける一方
、加圧ポンプ４をバイパスして前記循環ポンプ２の吸込
側に接続したバイパス管路１０を設け、更に、前記閉ル
ープ循環管路３に、前記バイパス管路１０からの流れ及
び濃縮液取出管路８への流れを阻止し閉ループ循環管路
３における循環流れを許容する状態と、バイパス管路１
０からの流れ及び濃縮液排出管路８への流れを許容し閉
ループ循環管路３の濃縮液排出管路８の接続部より下流
側への流れを阻止する状態とに切換可能な流路切換弁１
１．１２を設けて成る回分式の逆浸透膜濃縮装置を提案
している。Therefore, Japanese Patent Publication No. 59-48122 as a prior art is described in FIG. 4 in that publication, and as shown in FIG. A closed-loop circulation line 3 is formed as a closed-loop line with the circulation pump 2, and a sealed tank 9 is provided in the middle, while a bypass line is connected to the suction side of the circulation pump 2 by bypassing the pressurizing pump 4. 10 is provided in the closed-loop circulation line 3, and further includes a state in which the flow from the bypass line 10 and the flow to the concentrate extraction line 8 is blocked and circulation flow in the closed-loop circulation line 3 is allowed; Conduit 1
Flow path switching that allows the flow from 0 and the flow to the concentrate discharge pipe 8 and blocks the flow downstream from the connection part of the concentrate discharge pipe 8 of the closed loop circulation pipe 3. Valve 1
We have proposed a batch type reverse osmosis membrane concentrator equipped with 1.12.
しかして、この先行技術の逆浸透膜濃縮装置は、逆浸透
膜槽ｌ、循環ポンプ２及び密閉タンク９を含む閉ループ
循環管路３の圧力を、加圧ポンプ４にて高圧にすること
によって、透過液取出管路６から透過液を取り出し、前
記閉ループ循環管路３における被濃縮液濃度が高くなる
と、前記の運転を中断して原料被濃縮液注入管路５から
原料被濃縮液を注入する一方、濃縮液排出管路８から濃
縮液を排出することによって、閉ループ循環管路３内に
おける濃縮液を新しい原料被濃縮液と総入れ替えするよ
うにしたもので、閉ループ循環管路３中に密閉タンク９
を設けたことにより、運転時間を前記密閉タンクの内容
積の分だけ延長でき、また、こ＼における加圧ポンプ４
は、原料被濃縮液を透過液の量だけ高圧に加圧して供給
するだけで良いから、前記従来のものよりも動力の消費
を少なくできる。Therefore, in this prior art reverse osmosis membrane concentrator, the pressure in the closed loop circulation line 3 including the reverse osmosis membrane tank 1, the circulation pump 2, and the closed tank 9 is made high by the pressure pump 4. The permeate is taken out from the permeate extraction pipe 6, and when the concentration of the liquid to be concentrated in the closed loop circulation pipe 3 becomes high, the operation is interrupted and the raw material to be concentrated is injected from the raw material to be concentrated liquid injection pipe 5. On the other hand, by discharging the concentrate from the concentrate discharge pipe 8, the concentrate in the closed loop circulation pipe 3 is completely replaced with a new raw material to be concentrated. tank 9
By providing this, the operating time can be extended by the internal volume of the sealed tank, and the pressurizing pump 4 in this
Since it is sufficient to pressurize and supply the raw material to be concentrated by the amount of the permeate, power consumption can be reduced compared to the conventional method.
しかし、この先行技術の逆浸透膜濃縮装置は、閉ループ
循環管路３中に設けた密閉タンク９を水平横型にして、
該密閉タンク９への閉ループ循環管路３の入口９ａと、
当該密閉タンク９から閉ループ循環管路３への出口９ｂ
と略同じ高さ位置に設けた構成にしているので、加圧ポ
ンプ４の駆動に要する動力の低減、つまり、運転経費の
低減が未だ十分でない点に問題がある。However, in this prior art reverse osmosis membrane concentrator, the closed tank 9 provided in the closed loop circulation pipe 3 is of a horizontal type.
an inlet 9a of the closed loop circulation line 3 to the closed tank 9;
Outlet 9b from the closed tank 9 to the closed loop circulation pipe 3
Since the pressure pump 4 is provided at substantially the same height as the pressure pump 4, there is a problem in that the power required to drive the pressure pump 4, that is, the operating cost, is still not sufficiently reduced.
すなわち、密閉タンク９が水平横型で、その人口９ａと
出口９ｂとが略同じ高さ位置になっていることにより、
被濃縮液の分離運転中において密閉タンク９内にその人
口９ａから流入した濃縮液は、当該密閉タンク９内に溜
っている被濃縮液の全体と逐次混合し、被濃縮液濃度の
高い被濃縮液になったのち、循環ポンプ３により逆浸透
膜槽１に供給されることになり、換言すれば、逆浸透膜
槽１に供給される被濃縮液の濃度は、運転時間の経過に
比例して濃くなるもので、加圧ポンプ４による圧力も、
前記被濃縮液の濃度が運転時間の経過に比例して濃（な
ることに応じて上昇するようにしなければならないから
、加圧ポンプ４を駆動するのに要する動力が増大するの
である。That is, since the closed tank 9 is of a horizontal type, and its population 9a and outlet 9b are at approximately the same height,
During the separation operation of the liquid to be concentrated, the concentrated liquid flowing into the closed tank 9 from its population 9a is successively mixed with the entire liquid to be concentrated stored in the sealed tank 9, and the liquid to be concentrated with a high concentration of the liquid to be concentrated is After becoming a liquid, it is supplied to the reverse osmosis membrane tank 1 by the circulation pump 3. In other words, the concentration of the concentrated liquid supplied to the reverse osmosis membrane tank 1 is proportional to the elapse of the operating time. The pressure from the pressurizing pump 4 also increases.
Since the concentration of the liquid to be concentrated must increase in proportion to the passage of operating time, the power required to drive the pressurizing pump 4 increases.
本発明は、この先行技術の問題を解消することを目的と
するものである。The present invention aims to solve this problem of the prior art.
この目的を達成するために本発明は、透過液取出管路を
備えた逆浸透膜槽と循環ポンプとの間を閉ループ循環管
路に構成し、この閉ループ循環管路の途中に密閉タンク
を設ける一方、前記閉ループ循環管路又は密閉タンクに
、被濃縮液を加圧するための手段、原料被濃縮液の注入
手段及び濃縮液の排出手段を設けて成る逆浸透膜濃縮装
置において、前記密閉タンクを竪型にして、これを前記
閉ループ循環管路のうち前記逆浸透膜槽から循環ポンプ
の吸込側への循環管路中に設けると共に、前記逆浸透膜
槽から密閉タンクへの濃縮液の入口を当該密閉タンクの
下部に、該密閉タンクから循環ポンプへの被濃縮液の出
口を当該密閉タンクの上部に各々設けた構成にしたもの
である。In order to achieve this object, the present invention configures a closed loop circulation line between a reverse osmosis membrane tank equipped with a permeate extraction line and a circulation pump, and provides a sealed tank in the middle of this closed loop circulation line. On the other hand, in the reverse osmosis membrane concentrator, the closed loop circulation pipe or the sealed tank is provided with a means for pressurizing the liquid to be concentrated, a means for injecting the raw material liquid to be concentrated, and a means for discharging the concentrated liquid. It is vertically shaped and is installed in the closed loop circulation pipe from the reverse osmosis membrane tank to the suction side of the circulation pump, and an inlet for concentrated liquid from the reverse osmosis membrane tank to the closed tank. The configuration is such that an outlet for the liquid to be concentrated from the sealed tank to the circulation pump is provided at the bottom of the sealed tank, and an outlet for the liquid to be concentrated from the sealed tank to the circulation pump is provided at the top of the sealed tank.
この構成において閉ループ循環管路における被濃縮液は
、密閉タンクに設けた加圧手段にて高圧に保持された状
態のもとで、当該閉ループ循環管路中の循環ポンプにて
、逆浸透膜槽と密閉タンクとの間を循環し、逆浸透膜槽
における浸透膜を透過した透過液は、当該逆浸透膜槽に
おける透過液取出管路を介して機外に取り出される。In this configuration, the liquid to be concentrated in the closed loop circulation pipe is maintained at a high pressure by the pressurizing means provided in the closed tank, and then transported to the reverse osmosis membrane tank by the circulation pump in the closed loop circulation pipe. The permeated liquid that circulates between the reverse osmosis membrane tank and the closed tank and permeates the osmotic membrane in the reverse osmosis membrane tank is taken out of the machine via the permeated liquid extraction pipe in the reverse osmosis membrane tank.
この場合において、前記密閉タンクを竪型に構成すると
共に、該密閉タンクの下部に前記逆浸透膜槽からの濃縮
液の入口を、密閉タンクの上部に循環ポンプへの被濃縮
液の出口を設けた構成にしたことにより、逆浸透膜槽か
ら密閉タンク内に入る濃縮液は、密閉タンク内の下部に
溜る一方、密閉タンク内における被濃縮液は循環ポンプ
によって汲み出されるが、密閉タンクの下部に流入する
濃縮液と、密閉タンク内における被濃縮液とは、濃度差
、延いては比重差のために相互に混合することが殆どな
く層状に分かれた状態のもとで、密閉タンクの下部に流
入する濃縮液によって、密閉タンク内における被濃縮液
を押し上げる形態を採ることになるから、密閉タンクか
ら逆浸透膜槽に送られる被濃縮液は、前記先行技術のよ
うに密閉タンク内に流入する濃縮液との混合によって濃
度が直ちに濃くなることはなく、前記密閉タンク内にお
ける被濃縮液が出て行くまで低濃度に維持できる。In this case, the sealed tank is configured in a vertical shape, and an inlet for the concentrated liquid from the reverse osmosis membrane tank is provided at the bottom of the sealed tank, and an outlet for the concentrated liquid to the circulation pump is provided at the top of the sealed tank. With this configuration, the concentrated liquid entering the sealed tank from the reverse osmosis membrane tank accumulates at the bottom of the sealed tank, while the liquid to be concentrated in the sealed tank is pumped out by the circulation pump, but the concentrated liquid enters the sealed tank from the bottom of the sealed tank. The concentrated liquid flowing into the tank and the liquid to be concentrated in the closed tank hardly mix with each other due to the difference in concentration and specific gravity, and are separated into layers. The concentrated liquid flowing into the tank pushes up the concentrated liquid in the closed tank, so the concentrated liquid sent from the closed tank to the reverse osmosis membrane tank does not flow into the closed tank as in the prior art. The concentration does not increase immediately upon mixing with the concentrated liquid, and can be maintained at a low concentration until the concentrated liquid in the closed tank leaves.
これにより、閉ループ循環管路における被濃縮液の圧力
は、逆浸透膜槽に送られる被濃縮液の濃度を前記のよう
に低濃度に維持できる間は、当初における圧力のままで
良く、前記先行技術のように運転時間の経過に伴って次
第に高くする必要がないから、閉ループ循環管路におけ
る被濃縮液を高圧にすることに要する動力を低減するこ
とができる。As a result, the pressure of the liquid to be concentrated in the closed loop circulation pipe can remain at the initial pressure as long as the concentration of the liquid to be concentrated sent to the reverse osmosis membrane tank can be maintained at a low concentration as described above. Since there is no need to gradually increase the pressure as the operating time elapses as in the conventional technology, the power required to increase the pressure of the liquid to be concentrated in the closed loop circulation pipe can be reduced.
また、濃縮液の濃度が所定の限界値になると、濃縮液を
その排出手段から系外に排出する一方、新しい原料被濃
縮液を注入手段から注入することによって、濃縮液を新
しい原料被濃縮液に総入れ替えするのである。When the concentration of the concentrate reaches a predetermined limit value, the concentrate is discharged from the system through the discharge means, and a new raw material concentrate is injected from the injection means. It will be completely replaced.
すなわち本発明によると、回分式の逆浸透膜濃縮装置に
おいて、その閉ループ循環管路を高圧に維持することに
要する動力を低減できるから、運転経費を節減できる効
果を有する。That is, according to the present invention, in a batch type reverse osmosis membrane concentrator, the power required to maintain the closed loop circulation line at a high pressure can be reduced, so that the operating cost can be reduced.
以下本発明の実施例を図面（第１図）について説明する
に、図において符号１は逆浸透膜槽、２は循環ポンプ、
９は密閉タンクを各々示し、これら逆浸透膜槽１、循環
ポンプ２及び密閉タンク９の相互間は、密閉タンク９内
の被濃縮液が循環ポンプ２にて逆浸透膜槽ｌに送られた
のち逆浸透膜槽１から密閉タンク９内に戻るように閉ル
ープ循環管路３にて接続されており、前記逆浸透膜槽１
には、透過液取出管路６が接続されている。Embodiments of the present invention will be described below with reference to the drawings (Fig. 1). In the drawing, numeral 1 is a reverse osmosis membrane tank, 2 is a circulation pump,
9 indicates a sealed tank, and between the reverse osmosis membrane tank 1, the circulation pump 2, and the sealed tank 9, the liquid to be concentrated in the sealed tank 9 was sent to the reverse osmosis membrane tank L by the circulation pump 2. The reverse osmosis membrane tank 1 is then connected through a closed loop circulation pipe 3 so as to return to the closed tank 9, and the reverse osmosis membrane tank 1
A permeate extraction conduit 6 is connected to.
前記密閉タンク９は竪型に構成され、その下部には前記
逆浸透膜槽からの濃縮液の入口９ａが、その上部には前
記循環ポンプ２への被濃縮液の出口９ｂが各々設けられ
ている。The hermetic tank 9 has a vertical structure, and its lower part is provided with an inlet 9a for the concentrated liquid from the reverse osmosis membrane tank, and its upper part is provided with an outlet 9b for the concentrated liquid to the circulation pump 2. There is.
また、前記密閉タンク９の底部には、濃縮液の排出管路
８が接続され、この濃縮液の排出管路８には、密閉タン
ク９内に挿入した濃度検出計１３に連動し、密閉タンク
９内における被濃縮液濃度が所定の限界値以上になると
自動的に開くようにした排出弁１４が設けられている。Further, a concentrated liquid discharge pipe 8 is connected to the bottom of the sealed tank 9, and a concentration detector 13 inserted into the sealed tank 9 is connected to the concentrated liquid discharge pipe 8. A discharge valve 14 is provided which automatically opens when the concentration of the liquid to be concentrated in the container 9 exceeds a predetermined limit value.
更に、前記密閉タンク９の上部には、原料被濃縮液の注
入管路５が接続され、この原料被濃縮液注入管路５には
、原料被濃縮液の注入ポンプ１５が設けられていると共
に、該注入ポンプ１５に対してバイパスをなすバイパス
管路１６が接続され、このバイパス管路１６中には、前
記閉ループ循環管路３を高圧に維持するための加圧ポン
プ４が設けられている。Furthermore, an injection pipe 5 for the raw material to be concentrated is connected to the upper part of the sealed tank 9, and an injection pump 15 for the raw material to be concentrated is provided in the raw material to be concentrated liquid injection pipe 5. A bypass line 16 is connected to the injection pump 15, and a pressurizing pump 4 for maintaining the closed loop circulation line 3 at a high pressure is provided in the bypass line 16. .
なお、図中符号１７はフィルター、図中符号１８．１９
．２０は逆止弁を各々示す。Note that the reference numeral 17 in the figure is a filter, and the reference numerals 18 and 19 in the figure are filters.
．． 20 each indicates a check valve.
この構成において、密閉タンク９内における塩水は、加
圧ポンプ４にて所定の高圧に保持された状態のもとで、
当該閉ループ循環管路３中の循環ポンプ２にて、逆浸透
膜槽１と密閉タンク９との間を循環し、逆浸透膜槽１に
おける透過膜を透過した透過液は、当該逆浸透膜槽１に
おける透過液取出管路６を介して機外に取り出される一
方、前記逆浸透膜槽１において濃縮された濃縮液は、前
記密閉タンク９内に戻ることになる。In this configuration, the salt water in the closed tank 9 is maintained at a predetermined high pressure by the pressure pump 4, and
The circulation pump 2 in the closed loop circulation pipe 3 circulates between the reverse osmosis membrane tank 1 and the closed tank 9, and the permeated liquid that has permeated the permeation membrane in the reverse osmosis membrane tank 1 is sent to the reverse osmosis membrane tank. The concentrated liquid concentrated in the reverse osmosis membrane tank 1 returns to the closed tank 9 while being taken out of the machine via the permeate extraction pipe 6 in the reverse osmosis membrane tank 1 .
そして、前記密閉タンク９内において、当該密閉タンク
９内に戻る濃縮液と密閉タンク９内における被濃縮液と
が、前記先行技術のように逐次混合するときには、この
密閉タンク９から前記′ｆ！浸透膜槽１に送られる被濃
縮液の濃度は、第２図に二点鎖線の曲線Ｂで示すように
運転時間の経過と共に次第に上昇することになるから、
加圧ポンプ４にて高圧に維持する圧力も、前記曲線Ｂに
沿って高くなるようにしなければならないことになる。In the sealed tank 9, when the concentrated liquid returning to the sealed tank 9 and the liquid to be concentrated in the sealed tank 9 are successively mixed as in the prior art, the 'f! The concentration of the liquid to be concentrated sent to the osmotic membrane tank 1 gradually increases as the operating time passes, as shown by the two-dot chain curve B in FIG.
The pressure maintained at a high level by the pressurizing pump 4 must also increase along the curve B.
これに対して本発明は、前記のように密閉タンク９を竪
型に構成すると共に、該密閉タンク９の底部に前記逆浸
透膜槽１からの濃縮液の入口９ａを、密閉タンク９の上
部に循環ポンプ３への被濃縮液の出口９ｂを設けた構成
にしたものである。In contrast, in the present invention, the sealed tank 9 is configured in a vertical shape as described above, and the inlet 9a for the concentrated liquid from the reverse osmosis membrane tank 1 is connected to the bottom of the sealed tank 9, and the inlet 9a is connected to the upper part of the sealed tank 9. The structure is such that an outlet 9b for the concentrated liquid to the circulation pump 3 is provided.
このように構成すると、逆浸透膜［１から密閉タンク９
内に入る濃縮液は、当該密閉タンク９内の底部に溜る一
方、密閉タンク９内における被濃縮液は循環ポンプ３に
よって汲み出されるが、密閉タンク９の底部に流入する
濃縮液と、密閉タンク９内における被濃縮液とは、濃度
差、延いては比重差のために相互に混合することが殆ど
なく屑状に分かれた状態のもとで、密閉タンク９の下部
に流入する濃縮液によって、密閉タンク９内におけるｗ
＜濃縮液を押し上げる形態を採ることになるから、密閉
タンク９から逆浸透膜槽１に送られる被濃縮液は、前記
先行技術のように密閉タンク内に流入する濃縮液との混
合によって濃度が直ちに濃くなることはなく、前記密閉
タンク内における被濃縮液が出て行＜ＴＩの時間まで低
濃度ＡＩに維持でき、最初に密閉タンク９に入った濃縮
液が密閉タンク９から出て行くようになって初めて逆浸
透膜槽１に送られる被濃縮液の濃度がＡ２に高くなり、
そして、Ａ２の濃度の被濃縮液が密閉タンク９から出て
行くようになるまでの時間Ｔ２だけ、前記Ａ２の濃度を
維持できることになり、逆浸透膜槽１に送られる被濃縮
液の濃度は、前記の繰り返しによって、Ａ１からＡ２に
、Ａ２からＡ３へと階段的に高くなることになる。With this configuration, the reverse osmosis membrane [1 to the closed tank 9
The concentrated liquid that enters the tank 9 accumulates at the bottom of the sealed tank 9, while the liquid to be concentrated in the sealed tank 9 is pumped out by the circulation pump 3. The liquid to be concentrated in the tank 9 is separated into scraps that hardly mix with each other due to the difference in concentration and, furthermore, the difference in specific gravity. , w in the sealed tank 9
<Since the concentrated liquid is pushed up, the concentrated liquid sent from the closed tank 9 to the reverse osmosis membrane tank 1 is mixed with the concentrated liquid flowing into the closed tank to increase its concentration, as in the prior art. It does not become concentrated immediately, and the concentration AI can be maintained at a low concentration until the time when the concentrated liquid in the sealed tank exits < TI, and the concentrated liquid that first entered the sealed tank 9 flows out from the sealed tank 9. Only then does the concentration of the liquid to be concentrated sent to the reverse osmosis membrane tank 1 increase to A2,
Then, the concentration of A2 can be maintained for the time T2 until the liquid to be concentrated with the concentration of A2 comes out of the closed tank 9, and the concentration of the liquid to be concentrated sent to the reverse osmosis membrane tank 1 is , by repeating the above steps, the height increases stepwise from A1 to A2 and from A2 to A3.
従って、加圧ポンプ４にて高圧に維持する圧力も、前記
階段状の線Ａｌ、Ａ２．Ａ３に沿って高くなるようにす
ることで良いから、加圧ポンプ４にて高圧に維持する圧
力を、前記曲線Ｂに沿って高くする場合よりも、高圧に
維持するのに必要な動力を低減することができるのであ
る。Therefore, the pressure maintained at high pressure by the pressurizing pump 4 is also the same as the stepped lines Al, A2. Since it is sufficient to increase the pressure along the curve A3, the power required to maintain the high pressure with the pressurizing pump 4 is lower than when increasing the pressure along the curve B. It is possible.
そして、密閉タンク９内における濃縮液の濃度が所定の
限界値になると、当該密閉タンク９の底部に接続した濃
縮液排出管路中の排出弁１４が開くことにより、密閉タ
ンク９内の濃縮液を排出する一方、密閉タンク９内には
、注入ポンプ１５にて新しい原料被濃縮液を注入管路５
より注入することにより、密閉タンク９内及び閉ループ
循環管路３における濃縮液を新しい原料被濃縮液に総入
れ替えするのである。When the concentration of the concentrated liquid in the sealed tank 9 reaches a predetermined limit value, the discharge valve 14 in the concentrated liquid discharge pipe connected to the bottom of the sealed tank 9 opens, and the concentrated liquid in the sealed tank 9 is opened. At the same time, a new raw material to be concentrated liquid is injected into the sealed tank 9 using an injection pump 15 through a conduit 5.
By injecting more, the concentrated liquid in the closed tank 9 and the closed loop circulation pipe 3 is completely replaced with a new raw material to be concentrated liquid.
なお、前記実施例は、密閉タンク９、循環ポンプ３及び
逆浸透膜槽１を含む閉ループ循環管路３における圧力を
高圧にするための加圧手段として、加圧ポンプ４を使用
し、この加圧ポンプ４を、密閉タンク９の上部への塩水
供給管路５に接続した場合であったが、該加圧ポンプ４
は、前記密閉タンク９又は閉ループ循環管路３に対して
直接的に接続しても良く、また、この加圧ポンプ４に代
えて、第３図に示すように密閉タンク９内に、蛇腹式の
隔膜筒２１を設け、該隔膜筒２１内に、作動油等の液体
を高圧ポンプ２２及び切換弁２３を介して供給するよう
にした加圧手段にしても良く、更にまた、第４図に示す
ように密閉タンク９内に、その内面に沿わせた袋体２４
を設け、咳袋体２４の外側と密閉タンク９の内面との間
に、作動油等の液体を高圧ポンプ２５及び切換弁２６を
介して供給するようにした加圧手段にしても良いのであ
り、この第４図のようにした場合には、密閉タンク９の
内面に被濃縮液が接触することがないから、密閉タンク
を安価な材料にて製作できる利点を有する。In addition, in the above embodiment, the pressurizing pump 4 is used as pressurizing means for increasing the pressure in the closed loop circulation pipe 3 including the closed tank 9, the circulation pump 3, and the reverse osmosis membrane tank 1. In this case, the pressure pump 4 was connected to the salt water supply pipe 5 to the upper part of the closed tank 9.
may be directly connected to the sealed tank 9 or the closed loop circulation pipe 3, and instead of the pressurizing pump 4, a bellows-type pump may be installed in the sealed tank 9 as shown in FIG. A diaphragm cylinder 21 may be provided, and a pressurizing means may be used to supply liquid such as hydraulic oil into the diaphragm cylinder 21 via a high-pressure pump 22 and a switching valve 23. Furthermore, as shown in FIG. As shown, a bag body 24 is placed inside the sealed tank 9 along its inner surface.
A pressurizing means may be provided in which a liquid such as hydraulic oil is supplied between the outside of the cough bag body 24 and the inside of the sealed tank 9 via the high-pressure pump 25 and the switching valve 26. In the case shown in FIG. 4, since the liquid to be concentrated does not come into contact with the inner surface of the closed tank 9, there is an advantage that the closed tank can be manufactured from inexpensive materials.
第１図は本発明の第一実施例を示す図、第２図は運転時
間と被濃縮液濃度との関係を示す図、第３図は第二実施
例を示す図、第４図は第三実施例を示す図、第５図は従
来の逆浸透膜濃縮装置を示す図、第６図は先行技術の逆
浸透膜濃縮装置を示す図である。
１・・・・逆浸透膜槽、２・・・・循環ポンプ、３・・
・・閉ループ循環管路、４・・・・加圧ポンプ、５・・
・・原料被濃縮液の注入管路、６・・・・透過液取出管
路、８・・・・濃縮液の排出管路、９・・・・密閉タン
ク、９ａ・・・・密閉タンクへの入口、９ｂ・・・・密
閉タンクからの出口、１４・・・・排出弁、１５・・・
・原料被濃縮液の注入ポンプ。
特許出願人 株式会社 笹倉機械製作所ｊ！＄１：Ｒ
ｆｓ７FIG. 1 is a diagram showing the first embodiment of the present invention, FIG. 2 is a diagram showing the relationship between operating time and concentrated liquid concentration, FIG. 3 is a diagram showing the second embodiment, and FIG. FIG. 5 is a diagram showing a conventional reverse osmosis membrane concentrator, and FIG. 6 is a diagram showing a prior art reverse osmosis membrane concentrator. 1...Reverse osmosis membrane tank, 2...Circulation pump, 3...
...Closed loop circulation pipe, 4...Pressure pump, 5...
・・Injection pipe for raw material to be concentrated, 6: Permeate extraction pipe, 8: Discharge pipe for concentrated liquid, 9: Sealed tank, 9a: To sealed tank Inlet, 9b... Outlet from sealed tank, 14... Discharge valve, 15...
- Injection pump for raw material concentrate. Patent applicant: Sasakura Machinery Co., Ltd. $1:R
fs7
Claims (1)
プとの間を閉ループ循環管路に構成し、この閉ループ循
環管路の途中に密閉タンクを設ける一方、前記閉ループ
循環管路又は密閉タンクに、被濃縮液を加圧するための
手段、原料被濃縮液の注入手段及び濃縮液の排出手段を
設けて成る逆浸透膜濃縮装置において、前記密閉タンク
を竪型にして、これを前記閉ループ循環管路のうち前記
逆浸透膜槽から循環ポンプの吸込側への循環管路中に設
けると共に、前記逆浸透膜槽から密閉タンクへの濃縮液
の入口を当該密閉タンクの下部に、該密閉タンクから循
環ポンプへの被濃縮液の出口を当該密閉タンクの上部に
各々設けたことを特徴とする逆浸透膜濃縮装置。(1) A closed loop circulation line is constructed between the reverse osmosis membrane tank having a permeate extraction line and the circulation pump, and a sealed tank is provided in the middle of this closed loop circulation line, while the closed loop circulation line is Alternatively, in a reverse osmosis membrane concentrator comprising a closed tank provided with a means for pressurizing the liquid to be concentrated, a means for injecting the raw material liquid to be concentrated, and a means for discharging the concentrated liquid, the sealed tank is made vertical and the Provided in the closed loop circulation pipeline from the reverse osmosis membrane tank to the suction side of the circulation pump, and an inlet for the concentrated liquid from the reverse osmosis membrane tank to the closed tank at the bottom of the closed tank, A reverse osmosis membrane concentrating device characterized in that an outlet for a liquid to be concentrated from the sealed tank to a circulation pump is provided at the upper part of the sealed tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21464886A JPS6369507A (en) | 1986-09-11 | 1986-09-11 | Reverse-osmosis membrane concentrator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP21464886A JPS6369507A (en) | 1986-09-11 | 1986-09-11 | Reverse-osmosis membrane concentrator |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6369507A true JPS6369507A (en) | 1988-03-29 |
Family
ID=16659240
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP21464886A Pending JPS6369507A (en) | 1986-09-11 | 1986-09-11 | Reverse-osmosis membrane concentrator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6369507A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005046846A1 (en) * | 2003-11-05 | 2005-05-26 | Council Of Scientific And Industrial Research | An improvised device for concentrating the aqueous solution and a process thereof |
| JP2007061781A (en) * | 2005-09-02 | 2007-03-15 | Horyo Corp | Sediment removing device |
-
1986
- 1986-09-11 JP JP21464886A patent/JPS6369507A/en active Pending
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2005046846A1 (en) * | 2003-11-05 | 2005-05-26 | Council Of Scientific And Industrial Research | An improvised device for concentrating the aqueous solution and a process thereof |
| EP1682251A1 (en) * | 2003-11-05 | 2006-07-26 | Council of Scientific and Industrial Research | An improvised device for concentrating the aqueous solution and a process thereof |
| JP2007516057A (en) * | 2003-11-05 | 2007-06-21 | カウンセル オブ サイエンティフィック アンド インダストリアル リサーチ | Improved device for concentrating aqueous solutions and process therefor |
| JP2007061781A (en) * | 2005-09-02 | 2007-03-15 | Horyo Corp | Sediment removing device |
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