JP5974484B2 - Reverse osmosis membrane separation device, its startup method, and permeated water production method - Google Patents

Reverse osmosis membrane separation device, its startup method, and permeated water production method Download PDF

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JP5974484B2
JP5974484B2 JP2011550764A JP2011550764A JP5974484B2 JP 5974484 B2 JP5974484 B2 JP 5974484B2 JP 2011550764 A JP2011550764 A JP 2011550764A JP 2011550764 A JP2011550764 A JP 2011550764A JP 5974484 B2 JP5974484 B2 JP 5974484B2
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reverse osmosis
osmosis membrane
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control valve
pump
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JPWO2012073693A1 (en
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一憲 富岡
一憲 富岡
令嗣 小島
令嗣 小島
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Toray Industries Inc
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/06—Energy recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/12—Controlling or regulating
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/24—Specific pressurizing or depressurizing means
    • B01D2313/246—Energy recovery means

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
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  • Chemical Kinetics & Catalysis (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Description

本発明は、逆浸透膜モジュールを用いて流体中の混合成分または溶解成分を分離する逆浸透膜分離装置に関するものである。  The present invention relates to a reverse osmosis membrane separation device that separates mixed components or dissolved components in a fluid using a reverse osmosis membrane module.

海水淡水化などで使用される逆浸透膜分離装置は、基本的には図１に示すように、被処理液を高圧ポンプ１を介して所定の圧力に高めて逆浸透膜モジュールユニット２に供給し、この逆浸透膜モジュールユニット２の逆浸透作用により被処理液中の溶解成分を分離させ、透過水を得るように構成される。  A reverse osmosis membrane separation apparatus used in seawater desalination or the like basically supplies a liquid to be processed to a predetermined pressure via a high-pressure pump 1 to a reverse osmosis membrane module unit 2 as shown in FIG. The reverse osmosis action of the reverse osmosis membrane module unit 2 separates dissolved components in the liquid to be treated to obtain permeated water.

ところで、逆浸透膜モジュールユニット２は、図２のように、筒状ベッセル２１の中に逆浸透膜（分離膜）から構成した分離膜エレメント２２（例えばスパイラル型の分離膜エレメント）を内挿してなる単位構造体の膜モジュール２０を１本若しくは複数本有したモジュールユニットにより構成される。膜モジュール２０の片端部にある流通口２３に海水などの被処理液を加圧供給すると、各段の分離膜エレメント２２で分離膜を介して溶解成分が分離され、分離後の低圧透過水が中心管２４を経て透過水排出管２５から排出し、また高圧の濃縮水は流通口２３がある端部のもう一方の端部にある濃縮水排出管２６から排出される。  By the way, the reverse osmosis membrane module unit 2 has a separation membrane element 22 (for example, a spiral type separation membrane element) constituted by a reverse osmosis membrane (separation membrane) inserted in a cylindrical vessel 21 as shown in FIG. The unit structure is composed of a module unit having one or a plurality of membrane modules 20. When a liquid to be treated such as seawater is pressurized and supplied to the circulation port 23 at one end of the membrane module 20, the dissolved components are separated through the separation membrane by the separation membrane element 22 at each stage, and the low-pressure permeated water after separation is separated. The concentrated water is discharged from the permeate discharge pipe 25 through the center pipe 24, and the high-pressure concentrated water is discharged from the concentrated water discharge pipe 26 at the other end of the end where the flow port 23 is located.

さて、このような逆浸透膜分離装置においては、装置より排出される高圧の濃縮水のエネルギーを利用し高圧ポンプの所要動力の低減を図ることがある。濃縮水のエネルギー回収方法としては、逆転ポンプ、ターボチャージャーやペルトン水車を使用したりする場合があるが、最近ではエネルギー回収効率が高い圧力交換式のエネルギー回収装置を採用するケースが増加している。  Now, in such a reverse osmosis membrane separation device, the required power of the high-pressure pump may be reduced using the energy of the high-pressure concentrated water discharged from the device. Concentrated water energy recovery methods include the use of reverse pumps, turbochargers, and Pelton turbines. Recently, the use of pressure exchange type energy recovery devices with high energy recovery efficiency is increasing. .

ここで、圧力交換式のエネルギー回収装置を装備した逆浸透膜分離装置の一般的な構成を図３に示す。被処理液は高圧ポンプ１と圧力交換式エネルギー回収装置３に分配供給される。高圧ポンプ１に供給された被処理液は所定の圧力に高められて逆浸透膜モジュールユニット２に供給される。圧力交換式エネルギー回収装置３には、逆浸透膜モジュールユニット２から排出される高圧濃縮水も供給される。圧力交換式エネルギー回収装置３の内部で被処理液は高圧濃縮水のエネルギーを授受されることで昇圧され高圧被処理液として排出される。一方、保有エネルギーを被処理液に授受した高圧濃縮水は、圧力が低下し低圧濃縮水として排出される。圧力交換式エネルギー回収装置３から排出された高圧被処理液は加圧ポンプ４に供給され、高圧ポンプ１で昇圧された被処理液と同じ圧力まで圧力を高められ、高圧ポンプ１から吐出された被処理液と合流後、逆浸透膜モジュールユニット２に供給される。  Here, FIG. 3 shows a general configuration of a reverse osmosis membrane separation device equipped with a pressure exchange type energy recovery device. The liquid to be treated is distributed and supplied to the high pressure pump 1 and the pressure exchange type energy recovery device 3. The liquid to be treated supplied to the high-pressure pump 1 is increased to a predetermined pressure and supplied to the reverse osmosis membrane module unit 2. The pressure exchange type energy recovery device 3 is also supplied with high-pressure concentrated water discharged from the reverse osmosis membrane module unit 2. In the pressure exchange type energy recovery device 3, the liquid to be treated is boosted by receiving the energy of the high-pressure concentrated water and discharged as a high-pressure liquid to be treated. On the other hand, the high-pressure concentrated water that has transferred the stored energy to the liquid to be treated has a reduced pressure and is discharged as low-pressure concentrated water. The high-pressure liquid to be treated discharged from the pressure exchange type energy recovery device 3 is supplied to the pressurizing pump 4, the pressure is increased to the same pressure as the liquid to be treated that has been pressurized by the high-pressure pump 1, and the high-pressure pump 1 discharges the liquid. After merging with the liquid to be treated, it is supplied to the reverse osmosis membrane module unit 2.

このような圧力交換式エネルギー回収装置３を装備した逆浸透膜分離装置の一般的な運転起動手順は、まずは被処理液を圧力交換式エネルギー回収装置３のみに供給する。この被処理液の流量は定常運転時の濃縮水量とほぼ同等となるように圧力交換式エネルギー回収装置３から排出される濃縮水の排出ラインに設けた流量制御弁５で制御される。次に加圧ポンプ４を起動し被処理液の流れが、圧力交換式エネルギー回収装置３、加圧ポンプ４、逆浸透膜モジュールユニット２、圧力交換式エネルギー回収装置３、排出となるようにする。この時、圧力交換式エネルギー回収装置３から排出された被処理液の流量もまた定常運転時の濃縮水量とほぼ同等となるように加圧ポンプ４のモーター回転数を周波数変換装置（インバーター）で制御するのが一般的である。なお、この段階では被処理液の圧力は低圧であり逆浸透膜での溶解成分の分離は行われていない。  In a general operation start-up procedure of a reverse osmosis membrane separation apparatus equipped with such a pressure exchange type energy recovery device 3, first, the liquid to be treated is supplied only to the pressure exchange type energy recovery device 3. The flow rate of the liquid to be treated is controlled by a flow rate control valve 5 provided in the concentrated water discharge line discharged from the pressure exchange type energy recovery device 3 so as to be substantially equal to the amount of concentrated water during steady operation. Next, the pressure pump 4 is started so that the flow of the liquid to be treated becomes the pressure exchange type energy recovery device 3, the pressure pump 4, the reverse osmosis membrane module unit 2, the pressure exchange type energy recovery device 3, and the discharge. . At this time, the rotational speed of the motor of the pressurizing pump 4 is changed by a frequency converter (inverter) so that the flow rate of the liquid to be treated discharged from the pressure exchange type energy recovery device 3 is also substantially equal to the amount of concentrated water during steady operation. It is common to control. At this stage, the pressure of the liquid to be treated is low, and the dissolved components are not separated in the reverse osmosis membrane.

次に高圧ポンプ１を起動する。高圧ポンプ１の起動により被処理液が流れ出すと加圧ポンプ４を介して流れている被処理液と合流し逆浸透膜モジュールユニット２に供給される。加圧ポンプ４を介して流れる被処理液流量は流量調整弁５と加圧ポンプ４のモーター回転数制御により定常運転時の濃縮水量とほぼ同等となるように常に流量制御されているため、高圧ポンプ１を介して吐出された分の被処理液量、すなわち逆浸透膜モジュールユニット２に供給される被処理液量が定常運転時の濃縮水量を超過した分の被処理液量分だけが逆浸透膜を介し溶解成分が分離された透過水として外部に排出されることになる。  Next, the high pressure pump 1 is started. When the liquid to be treated flows by the activation of the high-pressure pump 1, the liquid to be treated flows via the pressure pump 4 and is supplied to the reverse osmosis membrane module unit 2. Since the flow rate of the liquid to be processed flowing through the pressurizing pump 4 is constantly controlled by the motor speed control of the flow rate adjusting valve 5 and the pressurizing pump 4 so as to be almost equal to the amount of concentrated water during steady operation, The amount of liquid to be treated discharged through the pump 1, that is, the amount of liquid to be treated supplied to the reverse osmosis membrane module unit 2 exceeds the amount of concentrated water during normal operation is reversed. The dissolved component is discharged to the outside through the osmosis membrane.

このとき高圧ポンプ１から吐出される被処理液量を少量から流し始め、徐々に増加していくのが一般的であり、図４のように高圧ポンプ１の吐出側に逆浸透膜モジュールユニット２に供給する被処理液流量を調整する流量調整弁６を設けるか、図５のように高圧ポンプのモーター回転数を周波数変換装置（インバーター）７で制御する。  At this time, the amount of liquid to be processed discharged from the high-pressure pump 1 starts to flow from a small amount and gradually increases, and the reverse osmosis membrane module unit 2 is disposed on the discharge side of the high-pressure pump 1 as shown in FIG. A flow rate adjusting valve 6 for adjusting the flow rate of the liquid to be processed supplied to the motor is provided, or the motor rotation speed of the high pressure pump is controlled by a frequency converter (inverter) 7 as shown in FIG.

さて、逆浸透膜を介し透過水が得られるということは、逆浸透膜モジュールユニット２の入口圧力が被処理液の浸透圧以上になることが必要となり、被処理液が例えば海水の場合、逆浸透膜モジュールユニット２の浸透圧は３ＭＰａ程度と高圧である必要がある。  The fact that permeated water is obtained through the reverse osmosis membrane means that the inlet pressure of the reverse osmosis membrane module unit 2 needs to be equal to or higher than the osmotic pressure of the liquid to be treated. The osmotic pressure of the osmotic membrane module unit 2 needs to be as high as about 3 MPa.

このように圧力交換式エネルギー回収装置３を装備した逆浸透膜分離装置の運転開始時は、高圧ポンプ１を起動するまでは、逆浸透膜モジュールユニット２の入口圧力は被処理液の押し込み圧力程度、例えば０．３ＭＰａ程度しかないが、高圧ポンプ１を一旦起動すると、例え流量制御弁６を微開にして被処理液がわずかしか流れないようにしても、前記の通り被処理液の排出先が無いため、逆浸透膜モジュールユニット２の入口圧力は被処理液の浸透圧の３ＭＰａ程度まで高められ、逆浸透膜モジュールユニット２に急激に圧力が掛かることとなる。  Thus, at the start of the operation of the reverse osmosis membrane separation apparatus equipped with the pressure exchange type energy recovery device 3, the inlet pressure of the reverse osmosis membrane module unit 2 is about the pushing pressure of the liquid to be treated until the high pressure pump 1 is started. For example, although it is only about 0.3 MPa, once the high-pressure pump 1 is started, even if the flow control valve 6 is opened slightly so that the liquid to be processed flows only slightly, the discharge destination of the liquid to be processed is as described above. Therefore, the inlet pressure of the reverse osmosis membrane module unit 2 is increased to about 3 MPa of the osmotic pressure of the liquid to be treated, and the reverse osmosis membrane module unit 2 is suddenly pressurized.

高圧の被処理液（海水等）が逆浸透膜モジュールユニット２に対し急激に加えられると、その圧力衝撃によって逆浸透膜の物理的性質が劣化するおそれがあり、また逆浸透膜の物理的性質の劣化は逆浸透膜モジュールユニット２において、例えば脱塩率の低下の要因となり、逆浸透処理能力を低下させることにもなる。  When a high-pressure liquid to be treated (seawater or the like) is suddenly applied to the reverse osmosis membrane module unit 2, the physical properties of the reverse osmosis membrane may be deteriorated by the pressure shock, and the physical properties of the reverse osmosis membrane. The deterioration of the reverse osmosis membrane module unit 2 causes, for example, a decrease in the desalination rate, and also reduces the reverse osmosis treatment capability.

これに対して、特許文献１には高圧ポンプ吐出側に逆浸透膜モジュールユニットに対して、バイパスするバイパス流路とバイパス流量制御弁を用いて入口圧力を徐々に昇圧する方法が提案されているが、圧力交換式エネルギー回収装置を装備した逆浸透膜分離装置の場合、濃縮水量は圧力交換式エネルギー回収装置から排出される濃縮水の排出ラインに設けた流量調整弁により制御され、また圧力交換式エネルギー回収装置から排出された被処理液の流量もまた定常運転時の濃縮水量とほぼ同等となるように加圧ポンプのモーター回転数を周波数変換装置（インバーター）を用いて制御されているため、入口圧力の急激な上昇を抑えるためには高圧ポンプ起動時に高圧ポンプより吐出される被処理液をバイパス流量調節弁より排出させるしかない。  On the other hand, Patent Document 1 proposes a method of gradually increasing the inlet pressure using a bypass flow path and a bypass flow rate control valve that bypass the reverse osmosis membrane module unit on the high-pressure pump discharge side. However, in the case of a reverse osmosis membrane separation device equipped with a pressure exchange type energy recovery device, the amount of concentrated water is controlled by a flow control valve provided in the drain line of the concentrated water discharged from the pressure exchange type energy recovery device, and pressure exchange The flow rate of the liquid to be treated discharged from the energy recovery device is also controlled using a frequency converter (inverter) so that the motor speed of the pressurization pump is approximately equal to the amount of concentrated water during steady operation. In order to suppress a sudden rise in the inlet pressure, the liquid to be treated discharged from the high pressure pump when the high pressure pump is started must be discharged from the bypass flow control valve. There.

高圧ポンプが周波数変換装置により制御されている場合にはこの方法でも起動することは可能であるが、大型の逆浸透膜分離装置の場合、高圧ポンプのモーター容量が大きく周波数変換装置も非常に高額になってしまうため、この周波数変換装置を装備しないことが多い。その様な場合、バイパス流量調節弁を全開とし高圧ポンプを起動すると高圧ポンプが過負荷によりトリップしてしまいこの装置自体を起動することは出来ない。またこの状況を高圧ポンプのトリップを防ぐべくバイパス流量調節弁を高圧ポンプの最低流量を確保するよう弁開度を固定し、高圧ポンプを起動すれば高圧ポンプは起動可能となるが、このとき逆浸透膜モジュールユニットには定常運転値以上の圧力が急激にかかることとなり、入口圧力を徐々に昇圧するのは不可能である。  If the high-pressure pump is controlled by a frequency converter, this method can also be started, but in the case of a large reverse osmosis membrane separator, the motor capacity of the high-pressure pump is large and the frequency converter is very expensive. Therefore, this frequency conversion device is often not equipped. In such a case, if the bypass flow rate control valve is fully opened and the high pressure pump is started, the high pressure pump trips due to overload, and the device itself cannot be started. In order to prevent the trip of the high-pressure pump, the bypass flow rate control valve is fixed so that the minimum flow rate of the high-pressure pump is secured, and the high-pressure pump can be started by starting the high-pressure pump. The osmosis membrane module unit is rapidly applied with a pressure higher than the steady operation value, and it is impossible to gradually increase the inlet pressure.

特開２００１−１１３１３６号公報JP 2001-113136 A

本発明の目的は、エネルギー回収装置を装備した逆浸透膜分離装置において、運転開始時における逆浸透膜モジュールへの急激な圧力変化を防止し、逆浸透膜の物理的性質の劣化を効果的に防ぐことのできる簡易な逆浸透膜分離装置を提供することにある。  The object of the present invention is to prevent a rapid pressure change to the reverse osmosis membrane module at the start of operation in a reverse osmosis membrane separation device equipped with an energy recovery device, effectively reducing the physical properties of the reverse osmosis membrane. An object of the present invention is to provide a simple reverse osmosis membrane separation device that can be prevented.

前記課題を解決するための本発明は、次の（１）から（４）のいずれかを特徴とするものである。  The present invention for solving the above-described problems is characterized by any one of the following (1) to (4).

（１）被処理液の一部を所定の圧力に高めて逆浸透膜モジュールに供給するポンプＡと、残りの被処理液を前記逆浸透膜モジュールより排出される濃縮水の圧力を利用して昇圧するエネルギー回収装置と、前記エネルギー回収装置で昇圧された被処理液を更に所定の圧力に高めて前記逆浸透膜モジュールに供給するポンプＢと、前記ポンプＡから吐出される被処理液の流量を調整する流量制御弁Ａと、前記流量制御弁Ａから前記逆浸透膜モジュールに対してバイパスするバイパス流路と、前記バイパス流路に設けられて前記被処理液のバイパス量を調整する流量制御弁Ｂと、さらに透過水配管上に設けられた透過水流量計と、透過水流量計で計測された透過水量に基づいて流量制御弁Ａを制御する透過水量制御部とを備えることを特徴とする逆浸透膜分離装置。
(1) Utilizing a pump A that raises a part of the liquid to be treated to a predetermined pressure and supplying the liquid to the reverse osmosis membrane module, and the pressure of the concentrated water discharged from the reverse osmosis membrane module An energy recovery device for increasing the pressure, a pump B for further increasing the pressure of the liquid to be processed by the energy recovery device to a predetermined pressure, and supplying the reverse osmosis membrane module, and a flow rate of the liquid to be processed discharged from the pump A A flow rate control valve A for adjusting the flow rate, a bypass flow path for bypassing the reverse osmosis membrane module from the flow rate control valve A, and a flow rate control provided in the bypass flow path for adjusting the bypass amount of the liquid to be treated It comprises a valve B , a permeated water flow meter provided on the permeated water pipe, and a permeated water amount control unit for controlling the flow rate control valve A based on the permeated water amount measured by the permeated water flow meter. Do Osmosis membrane separation device.

（２）さらにポンプＡとエネルギー回収装置に被処理液を供給するポンプＣと、ポンプＣを回転数制御する周波数変換器とを備えることを特徴とする（１）に記載の逆浸透膜分離装置。  (2) The reverse osmosis membrane separation device according to (1), further comprising a pump C for supplying a liquid to be processed to the pump A and the energy recovery device, and a frequency converter for controlling the rotational speed of the pump C. .

（３）（１）に記載の逆浸透膜分離装置を起動する方法であって、ポンプＡの起動前に被処理液がエネルギー回収装置、加圧ポンプ、逆浸透膜モジュール、エネルギー回収装置の順に流れて排出されるように調整した後、流量制御弁Ａ及び流量制御弁Ｂを所定の開度に設定しながらポンプＡを起動し、その後、逆浸透膜モジュールの入口圧力が所定の圧力まで上昇するまで、流量制御弁Ａが開方向、流量制御弁Ｂが閉方向となるように流量制御弁Ａと流量制御弁Ｂを段階的に制御することを特徴とする逆浸透膜分離装置の起動方法。  (3) A method for starting the reverse osmosis membrane separation device according to (1), in which the liquid to be treated is in the order of an energy recovery device, a pressure pump, a reverse osmosis membrane module, and an energy recovery device before the pump A is started. After adjusting to flow and discharge, the pump A is started while the flow rate control valve A and the flow rate control valve B are set to predetermined opening degrees, and then the inlet pressure of the reverse osmosis membrane module rises to the predetermined pressure. The flow control valve A and the flow control valve B are controlled stepwise so that the flow control valve A is in the opening direction and the flow control valve B is in the closing direction until the flow control valve A is activated. .

（４）（３）に記載の逆浸透膜分離装置の起動方法によって逆浸透膜分離装置を起動した後、被処理液を逆浸透膜モジュールに供給して透過水を得る透過水の製造方法。  (4) A method for producing permeated water in which the reverse osmosis membrane separation device is activated by the activation method of the reverse osmosis membrane separation device according to (3), and then the liquid to be treated is supplied to the reverse osmosis membrane module to obtain permeated water.

本発明により、エネルギー回収装置を装備した逆浸透膜分離装置において、バイパス流路に設けられた流量制御弁を用いて、そのバイパス流量を調整することで、高圧ポンプ起動開始時の逆浸透膜モジュールに加えられる被処理液の圧力を徐々に昇圧させることができ、簡易的かつ効果的に逆浸透膜モジュールの物理的性質の劣化を防止することができる。  According to the present invention, in a reverse osmosis membrane separation device equipped with an energy recovery device, a reverse osmosis membrane module at the start of starting a high-pressure pump by adjusting the bypass flow rate using a flow rate control valve provided in the bypass channel It is possible to gradually increase the pressure of the liquid to be treated, which can prevent the deterioration of the physical properties of the reverse osmosis membrane module simply and effectively.

逆浸透膜分離装置の概略構成を示す図である。It is a figure which shows schematic structure of a reverse osmosis membrane separator. 逆浸透膜モジュールユニットの一般的な構造を示す図である。It is a figure which shows the general structure of a reverse osmosis membrane module unit. 圧力交換式エネルギー回収装置を装備した逆浸透膜分離装置の概略構成を示す図である。It is a figure showing a schematic structure of a reverse osmosis membrane separation device equipped with a pressure exchange type energy recovery device. 図３の高圧ポンプ吐出部に流量制御弁を装備した概略構成を示す図である。It is a figure which shows schematic structure which equipped the high-pressure pump discharge part of FIG. 3 with the flow control valve. 図３の高圧ポンプに周波数変換装置を装備した概略構成を示す図である。It is a figure which shows schematic structure which equipped the high-pressure pump of FIG. 3 with the frequency converter. 本発明の実施形態に係る逆浸透膜分離装置の概略構成を示す図である。It is a figure showing a schematic structure of a reverse osmosis membrane separation device concerning an embodiment of the present invention. 本発明の別の実施形態に係る逆浸透膜分離装置の概略構成を示す図である。It is a figure which shows schematic structure of the reverse osmosis membrane separator which concerns on another embodiment of this invention.

本発明の逆浸透膜分離装置を図６を参照しながら説明する。  The reverse osmosis membrane separation apparatus of the present invention will be described with reference to FIG.

図６に示す逆浸透膜分離装置は、流体中の混合または溶解成分を分離する装置の概略構成である。海水などの被処理液は高圧ポンプ１と圧力交換式エネルギー回収装置３に分配供給される。高圧ポンプ１に供給された被処理液は所定の圧力、例えば６．０ＭＰａ程度まで高められて逆浸透膜モジュールユニット２に供給される。圧力交換式エネルギー回収装置３には分配供給される被処理液と逆浸透膜モジュールユニット２から排出される高圧濃縮水が供給される。圧力交換式エネルギー回収装置３の内部で被処理液は高圧濃縮水のエネルギーを授受され圧力が高められ高圧被処理液として排出される。一方保有エネルギーを被処理液に授受した高圧濃縮水は圧力が低下し低圧濃縮水として排出される。圧力交換式エネルギー回収装置３から排出された高圧被処理液は加圧ポンプ４に供給され、高圧ポンプ１で昇圧された被処理液と同じ圧力まで高圧被処理液の圧力が高められ、高圧ポンプ１からの被処理液と合流後、逆浸透膜モジュールユニット２に供給される。逆浸透膜モジュールユニット２は所定の圧力まで高められた被処理液を受けて、逆浸透作用により溶解成分を分離した透過水と濃縮水を得る。  The reverse osmosis membrane separation apparatus shown in FIG. 6 is a schematic configuration of an apparatus for separating mixed or dissolved components in a fluid. The liquid to be treated such as seawater is distributed and supplied to the high pressure pump 1 and the pressure exchange type energy recovery device 3. The liquid to be treated supplied to the high-pressure pump 1 is increased to a predetermined pressure, for example, about 6.0 MPa, and supplied to the reverse osmosis membrane module unit 2. The pressure exchange type energy recovery device 3 is supplied with the liquid to be distributed and the high-pressure concentrated water discharged from the reverse osmosis membrane module unit 2. In the pressure exchange type energy recovery device 3, the liquid to be treated receives the energy of the high-pressure concentrated water, the pressure is increased, and the liquid is discharged as the high-pressure liquid to be treated. On the other hand, the high-pressure concentrated water whose stored energy has been transferred to the liquid to be treated is reduced in pressure and discharged as low-pressure concentrated water. The high-pressure liquid to be treated discharged from the pressure exchange type energy recovery device 3 is supplied to the pressurizing pump 4, and the pressure of the high-pressure liquid to be treated is increased to the same pressure as the liquid to be treated that has been pressurized by the high-pressure pump 1. After merging with the liquid to be treated from 1, it is supplied to the reverse osmosis membrane module unit 2. The reverse osmosis membrane module unit 2 receives the liquid to be treated that has been increased to a predetermined pressure, and obtains permeated water and concentrated water from which dissolved components have been separated by reverse osmosis.

高圧ポンプ１の吐出側には、高圧ポンプ１から吐出された被処理液の流量を制御する流量制御弁６が設置されており、前述の通り高圧ポンプ１から吐出された被処理液の流量は、透過水量とほぼ同量となることから、流量制御弁６は透過水量を制御すべく透過水配管に設置された透過水流量計９をその透過水量制御部１０から流量制御されるのが一般的である。  On the discharge side of the high-pressure pump 1, a flow rate control valve 6 for controlling the flow rate of the liquid to be processed discharged from the high-pressure pump 1 is installed. As described above, the flow rate of the liquid to be processed discharged from the high-pressure pump 1 is Therefore, the flow rate control valve 6 generally controls the flow rate of the permeated water flow meter 9 installed in the permeated water pipe from the permeated water amount control unit 10 in order to control the permeated water amount. Is.

また、流量制御弁６から逆浸透膜モジュールユニット２に対しては、バイパスするバイパス流路と、このバイパス流路に設けられバイパス量を制御する流量制御弁８が設置されており、流量制御弁８は逆浸透膜分離装置の起動時、高圧ポンプ１の最低流量（ミニマムフロー）を確保すべく、高圧ポンプ１の供給側に設置された流量計１１とその高圧ポンプ最低流量制御部１２から流量制御されることを特徴としている。  Further, a bypass flow path for bypassing the reverse osmosis membrane module unit 2 from the flow control valve 6 and a flow control valve 8 for controlling the bypass amount provided in the bypass flow path are installed. 8 is the flow rate from the flow meter 11 installed on the supply side of the high pressure pump 1 and its minimum flow rate control unit 12 to ensure the minimum flow rate (minimum flow) of the high pressure pump 1 when the reverse osmosis membrane separation device is started. It is characterized by being controlled.

この逆浸透膜分離装置における運転操作手順は、まずは被処理液を圧力交換式エネルギー回収装置３のみに供給する。この被処理液の流量は定常運転時の濃縮水量とほぼ同等となるように圧力交換式エネルギー回収装置３から排出される濃縮水の排出ラインに設けた流量調整弁５で制御される。次に加圧ポンプ４を起動し被処理液の流れが、圧力交換式エネルギー回収装置３、加圧ポンプ４、逆浸透膜モジュールユニット２、圧力交換式エネルギー回収装置３、排出となるようにする。この時、圧力交換式エネルギー回収装置３から排出された被処理液の流量もまた定常運転時の濃縮水量とほぼ同等となるように加圧ポンプ４のモーター回転数を周波数変換装置（インバーター）で制御するのが一般的である。なおこの段階では被処理液の圧力は低圧であり逆浸透膜での溶解成分の分離は行われていない。  In the operation procedure in the reverse osmosis membrane separation device, first, the liquid to be treated is supplied only to the pressure exchange type energy recovery device 3. The flow rate of the liquid to be treated is controlled by a flow rate adjusting valve 5 provided in the concentrated water discharge line discharged from the pressure exchange type energy recovery device 3 so as to be substantially equal to the concentrated water amount in the steady operation. Next, the pressure pump 4 is started so that the flow of the liquid to be treated becomes the pressure exchange type energy recovery device 3, the pressure pump 4, the reverse osmosis membrane module unit 2, the pressure exchange type energy recovery device 3, and the discharge. . At this time, the rotational speed of the motor of the pressurizing pump 4 is changed by a frequency converter (inverter) so that the flow rate of the liquid to be treated discharged from the pressure exchange type energy recovery device 3 is also substantially equal to the amount of concentrated water during steady operation. It is common to control. At this stage, the pressure of the liquid to be treated is low, and the separation of dissolved components in the reverse osmosis membrane is not performed.

次に高圧ポンプ１を起動するが、高圧ポンプ１は過大な振動及び加熱損傷を防ぐため起動後直ぐに、高圧ポンプ１の最低流量（ミニマムフロー）まで流量を増加させる必要がある。そのため流量制御弁６及び流量制御弁８を、最低流量を確保出来るように規定の開度にあらかじめ設定し高圧ポンプ１を起動する。具体的には流量制御弁８を全開とした場合の流量制御弁６の２次側の配管圧損及び流量制御弁８の圧力損失を考慮し、流量制御弁６の初期開度を決定する。この状態で高圧ポンプ１を起動すると流量制御弁６の入力側の圧力は高圧ポンプ１の流量特性にも依存するが、定格圧力よりも高圧となり、例えば７．０ＭＰaとなるが、逆浸透膜モジュールユニット２の入口圧力は、流量制御弁８が全開であるので高圧ポンプ１から吐出される被処理液は流量制御弁８からバイパス側に排出されるため、圧力は殆ど上昇せず０．５ＭＰａ程度である。  Next, the high-pressure pump 1 is started. The high-pressure pump 1 needs to increase its flow rate to the minimum flow rate (minimum flow) of the high-pressure pump 1 immediately after the start-up in order to prevent excessive vibration and heating damage. Therefore, the high pressure pump 1 is started by setting the flow rate control valve 6 and the flow rate control valve 8 to a predetermined opening degree in advance so as to ensure the minimum flow rate. Specifically, the initial opening degree of the flow control valve 6 is determined in consideration of the secondary pressure loss of the flow control valve 6 and the pressure loss of the flow control valve 8 when the flow control valve 8 is fully opened. When the high-pressure pump 1 is started in this state, the pressure on the input side of the flow control valve 6 depends on the flow characteristics of the high-pressure pump 1 but is higher than the rated pressure, for example, 7.0 MPa. The inlet pressure of the unit 2 is about 0.5 MPa because the liquid to be treated discharged from the high-pressure pump 1 is discharged from the flow control valve 8 to the bypass side because the flow control valve 8 is fully open, and the pressure hardly rises. It is.

次に透過水を得るために透過水量制御部１０からの指令により流量制御弁６を徐々に開とする。すると高圧ポンプ１の吐出量は瞬間的に増加するが、高圧ポンプ最低流量制御部１２の機能により流量制御弁８にて高圧ポンプ１の最低流量になるよう高圧ポンプ１の吐出量は流量制御されているので、流量制御弁８が閉方向となり高圧ポンプ１の吐出量は最低流量を保持する。この流量制御弁６が開方向、流量制御弁８が閉方向となることにより逆浸透膜モジュールユニット２の入口圧力が上昇する。この２つの制御を同時に段階的に行うことにより、逆浸透膜モジュール入口圧力が徐々に増加し、逆浸透圧モジュールユニット２の入口圧力が例えば３．０ＭＰａに達した時点で透過水が排出され始める。  Next, in order to obtain permeated water, the flow rate control valve 6 is gradually opened according to a command from the permeated water amount control unit 10. Then, although the discharge amount of the high-pressure pump 1 increases instantaneously, the discharge amount of the high-pressure pump 1 is controlled by the flow control valve 8 so that the flow rate of the high-pressure pump 1 becomes the minimum flow rate by the function of the high-pressure pump minimum flow rate control unit 12. Therefore, the flow rate control valve 8 is closed and the discharge amount of the high pressure pump 1 maintains the minimum flow rate. The inlet pressure of the reverse osmosis membrane module unit 2 is increased by the flow control valve 6 being opened and the flow control valve 8 being closed. By performing these two controls stepwise at the same time, the reverse osmosis membrane module inlet pressure gradually increases, and the permeate begins to be discharged when the reverse osmosis pressure module unit 2 inlet pressure reaches, for example, 3.0 MPa. .

透過水が排出され始めても高圧ポンプ最低流量制御部１２では高圧ポンプ１の最低流量制御が継続されているので、流量制御弁８よりバイパス側に排出される被処理水量が徐々に減少し、その減少水量と同等の透過水が逆浸透膜モジュールユニット２より排出されることになる。そして最終的には流量制御弁８は全閉となる。  Even if the permeated water starts to be discharged, the minimum flow rate control of the high pressure pump 1 is continued in the high pressure pump minimum flow rate control unit 12, so that the amount of treated water discharged from the flow rate control valve 8 to the bypass side gradually decreases. Permeated water equivalent to the reduced water amount is discharged from the reverse osmosis membrane module unit 2. Finally, the flow control valve 8 is fully closed.

この時から高圧ポンプ１の吐出量が逆浸透膜モジュールユニット２の透過水量と同量となり、その後も透過水量制御部１０により透過水流量計９が定格流量になるまで、流量制御弁６を徐々に開とする制御が継続され、透過水量が定格流量に至った時点で本装置の起動は終了する。  From this time, the discharge rate of the high-pressure pump 1 becomes the same as the permeate flow rate of the reverse osmosis membrane module unit 2, and thereafter the flow rate control valve 6 is gradually turned until the permeate flow rate meter 9 reaches the rated flow rate by the permeate flow rate control unit 10. When the control to open is continued, and the permeated water amount reaches the rated flow rate, the start-up of this apparatus is finished.

具体的には、高圧ポンプ１を起動してから透過水が定格水量に達するまでの時間を約３００秒以上とするのが最良である。そのためには透過水量制御部１０の流量設定値を３００秒かけて定格水量まで徐々に上昇させるプログラム制御及び極端な圧力及び流量変動を防止するために操作端である流量制御弁６の変化率制限を設けるのが良い。  Specifically, it is best to set the time from when the high-pressure pump 1 is started until the permeated water reaches the rated water amount to about 300 seconds or more. For this purpose, program control for gradually increasing the flow rate setting value of the permeate flow rate control unit 10 to the rated water amount over 300 seconds, and limiting the rate of change of the flow rate control valve 6 that is the operating end in order to prevent extreme pressure and flow rate fluctuations. It is good to provide.

このような装置構成において、高圧ポンプ１および加圧ポンプ４は渦巻きポンプまたはプランジャーポンプからなり、流量制御弁６及び流量制御弁８はグローブ弁、ケージ弁またはニードル弁からなる。バイパスされた被処理液は系外に排水しても良いが、被処理液を貯留している槽等に戻し再度被処理液として利用しても良い。  In such an apparatus configuration, the high-pressure pump 1 and the pressure pump 4 are vortex pumps or plunger pumps, and the flow rate control valve 6 and the flow rate control valve 8 are globe valves, cage valves, or needle valves. The bypassed liquid to be processed may be drained out of the system, but may be returned to the tank or the like storing the liquid to be processed and used again as the liquid to be processed.

さらに、上記方法ではある設定した時間を掛けて透過水量制御部１０及び高圧ポンプ最低流量制御部１２により逆浸透膜モジュールユニット２の入口圧力を上昇させていくが、図７の様に逆浸透膜モジュールユニット２の入口に設けた圧力伝送器１３により得られる被処理液の圧力値に基づき入口圧力制御部１４より透過水量制御部１０にカスケード制御を行い流量制御弁６の弁開度を制御するのも良い。  Furthermore, in the above method, the inlet pressure of the reverse osmosis membrane module unit 2 is increased by the permeated water amount control unit 10 and the high pressure pump minimum flow rate control unit 12 over a set time, but the reverse osmosis membrane as shown in FIG. Based on the pressure value of the liquid to be treated obtained by the pressure transmitter 13 provided at the inlet of the module unit 2, cascade control is performed from the inlet pressure controller 14 to the permeate flow rate controller 10 to control the valve opening degree of the flow control valve 6. Also good.

また逆浸透膜モジュールユニット２の入口必要圧力は、被処理液の水質、水温により変化する。通常運転においては、この変化分に対し透過水水量制御部１０からの指令で、流量制御弁６への入口必要圧力が高い場合は、流量制御弁６が開方向、逆に流量制御弁６への入口必要圧力が低い場合は、流量制御弁６が閉方向となるよう調整し、逆浸透膜モジュールユニット２の入口必要圧力の増減に対応している。  The required pressure at the inlet of the reverse osmosis membrane module unit 2 varies depending on the quality of the liquid to be treated and the water temperature. In normal operation, if the required pressure at the inlet to the flow rate control valve 6 is high in response to a command from the permeate flow rate control unit 10 for this change, the flow rate control valve 6 opens, and conversely to the flow rate control valve 6. When the required pressure at the inlet is low, the flow control valve 6 is adjusted so as to be in the closing direction, corresponding to the increase or decrease in the required pressure at the inlet of the reverse osmosis membrane module unit 2.

動力エネルギー消費の観点からは、流量制御弁６の弁開度が全開に近い場合は無駄な動力エネルギー消費が無いことになるが、流量制御弁６の弁開度が全開よりも閉まっている時は、高圧ポンプ１のエネルギーを流量制御弁６で消費していることになり、高圧ポンプ１で無駄な動力エネルギー消費が発生していることになる。この動力エネルギーとは、高圧ポンプ１等の機器を作動させるのは電力であるので、「動力エネルギー＝電力エネルギー」となり、海水淡水化装置においては電力エネルギーの低減も大きな要素となっているため、このような無駄な電力エネルギー消費を削減するために、図７に示すように被処理液の供給ポンプ１５に周波数変換装置（インバーター）７を設置することが好ましい。  From the viewpoint of power energy consumption, when the valve opening degree of the flow control valve 6 is close to full open, there is no useless power energy consumption, but when the valve opening degree of the flow control valve 6 is closed rather than full open. This means that the energy of the high-pressure pump 1 is consumed by the flow control valve 6, and unnecessary power energy consumption is generated in the high-pressure pump 1. This power energy is electric power that operates the equipment such as the high-pressure pump 1, so “power energy = power energy”, and in the seawater desalination device, reduction of power energy is also a major factor. In order to reduce such wasteful energy consumption, it is preferable to install a frequency converter (inverter) 7 in the supply pump 15 for the liquid to be treated as shown in FIG.

逆浸透膜モジュール２の入口必要圧力は、微少な配管圧損などを考慮しなければ、供給ポンプ１５の吐出圧に高圧ポンプ１の吐出圧を加算し、そこから流量制御弁６での動力エネルギー損失分を減算すれば求めることができる。ここで、例えば供給ポンプ１５の定格吐出圧が１．０ＭＰａで、高圧ポンプ１の定格吐出圧が７．０ＭＰａである時、逆浸透膜モジュール２の入口必要圧力が７．５ＭＰａであるとすると、流量制御弁６で０．５ＭＰａの動力エネルギーを損失しなければいけなくなる。この時、供給ポンプ１５に周波数変換装置（インバーター）７が設置されていれば、供給ポンプ１５への供給電源周波数を変換することで、供給ポンプ１５の出力回転数を調整し、供給ポンプ１５の吐出圧力を定格の１．０ＭＰａから０．５ＭＰａに減少することで、無駄な電力エネルギーの消費も無くすことが可能となる。この方法を実施することで、流量制御弁６で動力エネルギーを無駄に消費する必要はなくなる。このように被処理水の供給ポンプ１５に周波数変換装置（インバーター）７を設置し、無駄な動力エネルギー消費を抑えようする場合があるが、このような場合においても上記した流量制御弁６およびバイパスラインに設けられた流量制御弁５を用いた起動方法、運転方法は有効である。  The required pressure at the inlet of the reverse osmosis membrane module 2 is obtained by adding the discharge pressure of the high-pressure pump 1 to the discharge pressure of the supply pump 15 and taking into account the motive energy loss at the flow rate control valve 6 unless the slight pressure loss of the piping is taken into consideration. It can be obtained by subtracting the minutes. Here, for example, when the rated discharge pressure of the supply pump 15 is 1.0 MPa and the rated discharge pressure of the high-pressure pump 1 is 7.0 MPa, the required inlet pressure of the reverse osmosis membrane module 2 is 7.5 MPa. The flow rate control valve 6 must lose 0.5 MPa of motive energy. If the frequency converter (inverter) 7 is installed in the supply pump 15 at this time, the output rotation speed of the supply pump 15 is adjusted by converting the supply power frequency to the supply pump 15, and the supply pump 15 By reducing the discharge pressure from the rated 1.0 MPa to 0.5 MPa, it is possible to eliminate wasteful consumption of electric power energy. By implementing this method, there is no need to waste power energy by the flow control valve 6. As described above, the frequency converter (inverter) 7 may be installed in the supply pump 15 for the water to be treated to suppress wasteful power energy consumption. In such a case, the flow control valve 6 and the bypass described above may be used. A starting method and an operating method using the flow control valve 5 provided in the line are effective.

１：高圧ポンプ（ポンプＡ）
２：逆浸透膜モジュールユニット
３：圧力交換式エネルギー回収装置
４：加圧ポンプ（ポンプＢ）
５：流量制御弁
６：流量制御弁（流量制御弁Ａ）
７：周波数変換装置（インバーター）
８：流量制御弁（流量制御弁Ｂ）
９：透過水流量計
１０：透過水量制御部
１１：流量計
１２：高圧ポンプ最低流量制御部
１３：圧力伝送器
１４：入口圧力制御部
１５：供給ポンプ（ポンプＣ）
２０：膜モジュール
２１：筒状ベッセル
２２：分離膜エレメント
２３：流通口
２４：中心管
２５：透過水排出管
２６：濃縮水排出管1: High-pressure pump (Pump A)
2: Reverse osmosis membrane module unit 3: Pressure exchange type energy recovery device 4: Pressure pump (pump B)
5: Flow control valve 6: Flow control valve (flow control valve A)
7: Frequency converter (inverter)
8: Flow control valve (flow control valve B)
9: Permeate flow meter 10: Permeate flow control unit 11: Flow meter 12: High pressure pump minimum flow control unit 13: Pressure transmitter 14: Inlet pressure control unit 15: Supply pump (pump C)
20: Membrane module 21: Cylindrical vessel 22: Separation membrane element 23: Distribution port 24: Center pipe 25: Permeate discharge pipe 26: Concentrated water discharge pipe

Claims (4)

被処理液の一部を所定の圧力に高めて逆浸透膜モジュールに供給するポンプＡと、残りの被処理液を逆浸透膜モジュールより排出される濃縮水の圧力を利用して昇圧するエネルギー回収装置と、エネルギー回収装置で昇圧された被処理液を更に所定の圧力に高めて逆浸透膜モジュールに供給するポンプＢと、ポンプＡから吐出される被処理液の流量を調整する流量制御弁Ａと、流量制御弁Ａから逆浸透膜モジュールに対してバイパスするバイパス流路と、バイパス流路に設けられて被処理液のバイパス量を調整する流量制御弁Ｂと、さらに透過水配管上に設けられた透過水流量計と、透過水流量計で計測された透過水量に基づいて流量制御弁Ａを制御する透過水量制御部とを備えることを特徴とする逆浸透膜分離装置。 Energy recovery for boosting a part of the liquid to be treated to a predetermined pressure by using the pressure of concentrated water discharged from the reverse osmosis membrane module and a pump A for supplying the liquid to the reverse osmosis membrane module Apparatus, pump B to which the liquid to be processed whose pressure has been increased by the energy recovery apparatus is further increased to a predetermined pressure and supplied to the reverse osmosis membrane module, and flow control valve A for adjusting the flow rate of the liquid to be processed discharged from pump A A bypass flow path that bypasses the reverse osmosis membrane module from the flow control valve A, a flow control valve B that is provided in the bypass flow path and adjusts the bypass amount of the liquid to be treated , and further provided on the permeate pipe A reverse osmosis membrane separation device comprising: a permeated water flow meter; and a permeated water amount control unit that controls the flow rate control valve A based on the permeated water amount measured by the permeated water flow meter . さらにポンプＡとエネルギー回収装置に被処理液を供給するポンプＣと、ポンプＣを回転数制御する周波数変換器とを備えることを特徴とする請求項１に記載の逆浸透膜分離装置。 The reverse osmosis membrane separation device according to claim 1, further comprising a pump C for supplying a liquid to be treated to the pump A and the energy recovery device, and a frequency converter for controlling the rotation speed of the pump C. 請求項１に記載の逆浸透膜分離装置を起動する方法であって、ポンプＡの起動前に被処理液がエネルギー回収装置、加圧ポンプ、逆浸透膜モジュール、エネルギー回収装置の順に流れて排出されるように調整した後、流量制御弁Ａ及び流量制御弁Ｂを所定の開度に設定しながらポンプＡを起動し、その後、逆浸透膜モジュールの入口圧力が所定の圧力まで上昇するまで、流量制御弁Ａが開方向、流量制御弁Ｂが閉方向となるように流量制御弁Ａと流量制御弁Ｂを段階的に制御することを特徴とする逆浸透膜分離装置の起動方法。 It is a method of starting the reverse osmosis membrane separation apparatus of Claim 1, Comprising: Before starting the pump A, to-be-processed liquid flows and discharges in order of an energy recovery device, a pressurization pump, a reverse osmosis membrane module, and an energy recovery device. After adjusting so that the flow rate control valve A and the flow rate control valve B are set to a predetermined opening, the pump A is started, and then, until the inlet pressure of the reverse osmosis membrane module rises to a predetermined pressure, A method for starting a reverse osmosis membrane separation device, wherein the flow rate control valve A and the flow rate control valve B are controlled stepwise so that the flow rate control valve A is in an open direction and the flow rate control valve B is in a closed direction. 請求項３に記載の逆浸透膜分離装置の起動方法によって逆浸透膜分離装置を起動した後、被処理液を逆浸透膜モジュールに供給して透過水を得る透過水の製造方法。 The manufacturing method of the permeated water which starts a reverse osmosis membrane separator by the starting method of the reverse osmosis membrane separator of Claim 3, and supplies a to-be-processed liquid to a reverse osmosis membrane module, and obtains permeated water.
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