WO2019180789A1 - Water treatment device and water treatment method - Google Patents

Water treatment device and water treatment method Download PDF

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WO2019180789A1
WO2019180789A1 PCT/JP2018/010872 JP2018010872W WO2019180789A1 WO 2019180789 A1 WO2019180789 A1 WO 2019180789A1 JP 2018010872 W JP2018010872 W JP 2018010872W WO 2019180789 A1 WO2019180789 A1 WO 2019180789A1
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water
membrane
unit
separation
treatment
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PCT/JP2018/010872
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French (fr)
Japanese (ja)
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嘉晃 伊藤
英正 垣上
英夫 鈴木
英夫 岩橋
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三菱重工エンジニアリング株式会社
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Publication of WO2019180789A1 publication Critical patent/WO2019180789A1/en

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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
    • B01D61/08—Apparatus therefor
    • 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
    • B01D61/58—Multistep processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Abstract

This water treatment device 1A is provided with: a first membrane treatment section 111 provided with a plurality of membrane separation sections each comprising a first separation membrane 111a that performs membrane separation of water to be treated W1 into first permeate water W2 and first concentrated water; and a second membrane treatment section 112 provided with a plurality of membrane separation sections each comprising a second separation membrane 112a that has a lower desalination rate than the first separation membranes 111a and that performs membrane separation of the first concentrated water into second permeate water W3 and second concentrated water W4. The first membrane treatment section 111 discharges at least part of the first permeate water W2 to the exterior of the first membrane treatment section 111 and supplies the first concentrated water subjected to membrane separation from the water to be treated W1 to the second membrane treatment section 112. The second membrane treatment section 112 supplies at least part of the second permeate water W3 to the water to be treated W1 supplied to the first membrane treatment section 111 and discharges the second concentrated water W4 subjected to membrane separation from the first concentrated water.

Description

水処理装置及び水処理方法Water treatment apparatus and water treatment method
　本発明は、水処理装置及び水処理方法に関し、例えば、分離膜により被処理水を膜分離する水処理装置及び水処理方法に関する。 The present invention relates to a water treatment apparatus and a water treatment method, and for example, relates to a water treatment apparatus and a water treatment method in which water to be treated is separated by a separation membrane.
　従来、第１分離膜モジュール、第２分離膜モジュール及び第３分離膜モジュールが直列に配置された純水製造システムが提案されている（例えば、特許文献１参照）。特許文献１に記載の純水製造システムでは、第３分離膜モジュールの透過水を第１分離膜モジュールの供給水として循環させることにより、被処理水の水回収率を高めて有効利用している。 Conventionally, a pure water production system in which a first separation membrane module, a second separation membrane module, and a third separation membrane module are arranged in series has been proposed (for example, see Patent Document 1). In the pure water production system described in Patent Document 1, the permeated water of the third separation membrane module is circulated as the supply water of the first separation membrane module, so that the water recovery rate of the treated water is increased and effectively used. .
特開２０１１－１８９３０２号公報JP 2011-189302 A
　ところで、複数の分離膜モジュールが直列に配設された水処理装置では、分離膜により膜分離した濃縮水を高濃度に濃縮することが求められる。しかしながら、従来の水処理装置では、濃縮水の濃縮には限界があり、必ずしも十分に濃縮水を高濃縮できない場合がある。 By the way, in a water treatment apparatus in which a plurality of separation membrane modules are arranged in series, it is required to concentrate the concentrated water separated by the separation membrane to a high concentration. However, in the conventional water treatment apparatus, there is a limit to the concentration of the concentrated water, and there is a case where the concentrated water cannot be sufficiently highly concentrated.
　本発明は、膜分離後の濃縮水を高濃縮可能な水処理装置及び水処理方法を提供することを目的とする。 An object of the present invention is to provide a water treatment apparatus and a water treatment method capable of highly concentrating concentrated water after membrane separation.
　本発明の第１の態様によると、被処理水を第１濃縮水と第１透過水とに膜分離する第１分離膜を有する少なくとも一つの膜分離部を備えた第１膜処理部と、前記第１濃縮水を第２透過水と第２濃縮水とに膜分離する前記第１分離膜より相対的に脱塩率が低い第２分離膜を有する少なくとも一つの膜分離部を備えた第２膜処理部と、を具備し、前記第１膜処理部は、前記第１透過水の少なくとも一部を当該第１膜処理部の外部に排出する一方、前記被処理水から膜分離された前記第１濃縮水を前記第２膜処理部に供給し、前記第２膜処理部は、前記第２透過水の少なくとも一部を前記第１膜処理部に供給される前記被処理水に供給する一方、前記第１濃縮水から膜分離された前記第２濃縮水を排出することを特徴とする。 According to the first aspect of the present invention, a first membrane treatment unit comprising at least one membrane separation unit having a first separation membrane for membrane separation of treated water into first concentrated water and first permeated water; A first separation unit having a second separation membrane having a lower desalination rate than the first separation membrane for separating the first concentrated water into a second permeated water and a second concentrated water; Two membrane treatment units, wherein the first membrane treatment unit discharges at least part of the first permeated water to the outside of the first membrane treatment unit, and is membrane-separated from the treated water. The first concentrated water is supplied to the second membrane treatment unit, and the second membrane treatment unit supplies at least a part of the second permeated water to the treated water supplied to the first membrane treatment unit. On the other hand, the second concentrated water separated from the first concentrated water is discharged.
　本発明の第２の態様によると、第１分離膜を備えた少なくとも一つの膜分離部により被処理水を第１透過水と第１濃縮水とに膜分離する第１膜処理工程と、前記第１分離膜より相対的に脱塩率が低い第２分離膜を備えた少なくとも一つの膜分離部により前記第１濃縮水を第２透過水と第２濃縮水とに膜分離する第２膜処理工程とを含み、前記第１膜処理工程では、前記第１透過水の少なくとも一部を排出する一方、前記被処理水から膜分離された前記第１濃縮水を前記膜分離部に供給し、前記第２膜処理工程では、前記第２透過水の少なくとも一部を前記膜分離部に供給される前記被処理水に供給する一方、前記第１濃縮水から膜分離された前記第２濃縮水を排出することを特徴とする。 According to the second aspect of the present invention, the first membrane treatment step of membrane-separating the water to be treated into the first permeated water and the first concentrated water by the at least one membrane separation unit provided with the first separation membrane; A second membrane that membrane-separates the first concentrated water into second permeated water and second concentrated water by at least one membrane separation section having a second separation membrane having a lower desalination rate than the first separation membrane. In the first membrane treatment step, at least a part of the first permeate is discharged, and the first concentrated water separated from the treated water is supplied to the membrane separation unit. In the second membrane treatment step, at least a part of the second permeated water is supplied to the treated water supplied to the membrane separation unit, while the second concentration is membrane-separated from the first concentrated water. It is characterized by draining water.
　本発明によれば、膜分離後の濃縮水を高濃縮可能な水処理装置及び水処理方法を実現できる。 According to the present invention, a water treatment apparatus and a water treatment method capable of highly concentrating concentrated water after membrane separation can be realized.
図１Ａは、第１の実施の形態に係る水処理装置の一例を示す模式図である。 Drawing 1A is a mimetic diagram showing an example of the water treatment equipment concerning a 1st embodiment. 図１Ｂは、第１の実施の形態に係る水処理装置の他の例を示す模式図である。FIG. 1B is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. 図２Ａは、第１の実施の形態に係る水処理装置の別の例を示す模式図である。FIG. 2A is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. 図２Ｂは、第１の実施の形態に係る水処理装置の別の例を示す模式図である。FIG. 2B is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. 図３Ａは、第２の実施の形態に係る水処理装置の一例を示す模式図である。FIG. 3A is a schematic diagram illustrating an example of a water treatment device according to the second embodiment. 図３Ｂは、第２の実施の形態に係る水処理装置の他の例を示す模式図である。FIG. 3B is a schematic diagram illustrating another example of the water treatment device according to the second embodiment. 図４Ａは、第３の実施の形態に係る水処理装置の一例を示す模式図である。FIG. 4A is a schematic diagram illustrating an example of a water treatment device according to the third embodiment. 図４Ｂは、第３の実施の形態に係る水処理装置の他の例を示す模式図である。FIG. 4B is a schematic diagram illustrating another example of the water treatment device according to the third embodiment.
　以下、本発明の実施の形態について、添付図面を参照して詳細に説明する。なお、本発明は、以下の各実施の形態に限定されるものではなく、適宜変更して実施可能である。また、以下の各実施の形態は適宜組み合わせて実施可能である。 Hereinafter, embodiments of the present invention will be described in detail with reference to the accompanying drawings. In addition, this invention is not limited to each following embodiment, It can implement by changing suitably. Also, the following embodiments can be implemented in combination as appropriate.
（第１の実施の形態）
　図１Ａは、第１の実施の形態に係る水処理装置の一例を示す模式図である。図１Ａに示すように、本実施の形態に係る水処理装置１Ａは、被処理水Ｗ１として固液分離及び濾過処理などの前処理により海水中の固形物などの濁質が予め低減された前処理水が供給される膜分離モジュール１１を備える。膜分離モジュール１１は、同一の圧力容器（ベッセル）１１０内に配置された第１膜処理部１１１及び第２膜処理部１１２を備える。第１膜処理部１１１は、圧力容器１１０内の被処理水Ｗ１入口側に配置され、第２膜処理部１１２は、被処理水Ｗ１の流れ方向における第１膜処理部１１１の下流側に配置される。第１膜処理部１１１は、被処理水Ｗ１を第１透過水Ｗ２と第１濃縮水（不図示）とに膜分離する。第２膜処理部１１２は、第１濃縮水を第２透過水Ｗ３と第２濃縮水Ｗ４とに膜分離する。膜分離モジュール１１は、第１透過水Ｗ２及び第２濃縮水Ｗ４を外部に排出すると共に、第２透過水Ｗ３を、膜分離モジュール１１に供給される被処理水Ｗ１に供給する。 (First embodiment)
Drawing 1A is a mimetic diagram showing an example of the water treatment equipment concerning a 1st embodiment. As shown in FIG. 1A, the water treatment apparatus 1A according to the present embodiment, contaminants such as solids in sea water is preliminarily reduced by pre-treatment such as solid-liquid separation and filtration process as the water to be treated W 1 A membrane separation module 11 to which pretreated water is supplied is provided. The membrane separation module 11 includes a first membrane treatment unit 111 and a second membrane treatment unit 112 arranged in the same pressure vessel (vessel) 110. The first membrane treatment unit 111 is arranged on the inlet side of the treated water W 1 in the pressure vessel 110, and the second membrane treatment unit 112 is downstream of the first membrane treatment unit 111 in the flow direction of the treated water W 1. Placed in. The first layer processing section 111 membrane separation in the water to be treated W 1 the first permeate W 2 and the first concentrated water (not shown). The second membrane treatment unit 112 performs membrane separation of the first concentrated water into the second permeated water W 3 and the second concentrated water W 4 . The membrane separation module 11 discharges the first permeated water W 2 and the second concentrated water W 4 to the outside, and supplies the second permeated water W 3 to the treated water W 1 supplied to the membrane separation module 11. .
　第１膜処理部１１１は、被処理水Ｗ１または前段から供給される濃縮水を透過水と濃縮水とに膜分離する第１分離膜１１１ａを有する複数（本実施の形態では４つ）の膜分離部：第１膜分離部１１１－１～第４膜分離部１１１－４を備える。第１分離膜１１１ａとしては、被処理水Ｗ１または前段から供給される濃縮水を透過水と濃縮水とに膜分離できるものであれば制限はなく、例えば、逆浸透（ＲＯ：Reverse Osmosis）膜などが用いられる。第１分離膜１１１ａとしては、例えば、脱塩率が９５％以上のものが好ましく、９７％以上のものがより好ましく、９９％以上のものが更に好ましい。 The first layer processing section 111, a plurality of (four in this embodiment) having a first separation film 111a to membrane separation to the permeate and the concentrated water concentrated water supplied from the water to be treated W 1 or preceding Membrane separation unit: provided with a first membrane separation unit 111-1 to a fourth membrane separation unit 111-4. The first separation membrane 111a, is not limited as long as it can film separated into permeated water and concentrated water concentrated water supplied from the water to be treated W 1 or preceding, e.g., reverse osmosis (RO: Reverse Osmosis) A membrane or the like is used. For example, the first separation membrane 111a preferably has a desalination rate of 95% or more, more preferably 97% or more, and still more preferably 99% or more.
　なお、本実施の形態では、第１膜処理部１１１が、４つの膜分離部１１１－１～１１１－４を備える例について説明するが、第１膜処理部１１１は、少なくとも一つの膜分離部を備えていればよく、膜分離部の数は適宜変更可能である。 In the present embodiment, an example in which the first membrane treatment unit 111 includes four membrane separation units 111-1 to 111-4 will be described. However, the first membrane treatment unit 111 includes at least one membrane separation unit. The number of membrane separation parts can be changed as appropriate.
　第２膜処理部１１２は、第１濃縮水または前段から供給される濃縮水を透過水と濃縮水とに膜分離する第２分離膜１１２ａを有する複数の（本実施の形態では３つ）の膜分離部：第１膜分離部１１２－１～第３膜分離部１１２－３を備える。第２分離膜１１２ａとしては、第１膜処理部１１１の第１分離膜１１１ａより脱塩率が相対的に低く、第１膜処理部１１１から供給される第１濃縮水または前段から供給される濃縮水を透過水と濃縮水とに膜分離できるものであれば制限はない。また、第２分離膜１１２ａとしては、ナトリウムイオン（Ｎａ＋）及び塩化物イオン（Ｃｌ－）などの１価イオン成分、並びに、カルシウムイオン（Ｃａ２＋）、マグネシウムイオン（Ｍｇ２＋）及び硫酸イオン（ＳＯ４ ２－）などの２価イオン成分の透過率が、第１分離膜１１１ａに対して相対的に高いものを用いてもよい。 The second membrane treatment unit 112 includes a plurality of (three in this embodiment) second separation membranes 112a that separate the first concentrated water or the concentrated water supplied from the previous stage into permeated water and concentrated water. Membrane separation unit: provided with a first membrane separation unit 112-1 to a third membrane separation unit 112-3. As the second separation membrane 112a, the desalination rate is relatively lower than that of the first separation membrane 111a of the first membrane treatment unit 111 and is supplied from the first concentrated water supplied from the first membrane treatment unit 111 or from the previous stage. There is no limitation as long as the concentrated water can be separated into permeated water and concentrated water. As the second separation membrane 112a, monovalent ion components such as sodium ions (Na + ) and chloride ions (Cl − ), calcium ions (Ca 2+ ), magnesium ions (Mg 2+ ), and sulfate ions ( A material having a relatively high transmittance for divalent ion components such as SO 4 2− ) relative to the first separation membrane 111a may be used.
　なお、本実施の形態では、３つの膜分離部１１２－１～１１２－３を備える例について説明するが、第２膜処理部１１２は、少なくとも一つの膜分離部を備えていればよく、膜分離部の数は適宜変更可能である。 In the present embodiment, an example in which three membrane separation units 112-1 to 112-3 are provided will be described. However, the second membrane processing unit 112 may include at least one membrane separation unit, and the membrane The number of separation parts can be changed as appropriate.
　第１膜分離部１１１－１は、被処理水Ｗ１を透過水と濃縮水とに膜分離する。また、第１膜分離部１１１－１は、膜分離により得られた透過水を第１透過水Ｗ２として水処理装置１Ａの外部に排出すると共に、膜分離により得られた濃縮水を第２膜分離部１１１－２に供給する。 The first membrane separation unit 111-1, the membrane separation treatment water W 1 to the permeate and the concentrated water. The first membrane separation unit 111-1, as well as discharged to the outside of the water treatment apparatus 1A as a first permeate W 2 permeate obtained by membrane separation, the concentrated water obtained by membrane separation second Supplied to the membrane separator 111-2.
　第２膜分離部１１１－２は、第１膜分離部１１１－１から供給された濃縮水を透過水と濃縮水とに膜分離する。また、第２膜分離部１１１－２は、膜分離により得られた透過水を第１透過水Ｗ２として水処理装置１Ａの外部に排出すると共に、膜分離により得られた濃縮水を第３膜分離部１１１－３に供給する。 The second membrane separation unit 111-2 membrane-separates the concentrated water supplied from the first membrane separation unit 111-1 into permeated water and concentrated water. The second membrane separation unit 111-2, film while discharged outside of the water treatment device 1A of the permeated water obtained as the first permeate W 2 by the separation, a third concentrated water obtained by membrane separation It supplies to the membrane separation part 111-3.
　第３膜分離部１１１－３は、第２膜分離部１１１－２から供給された濃縮水を透過水と濃縮水とに膜分離する。また、第３膜分離部１１１－３は、膜分離により得られた透過水を第１透過水Ｗ２として水処理装置１Ａの外部に排出すると共に、膜分離により得られた濃縮水を第４膜分離部１１１－４に供給する。 The third membrane separation unit 111-3 membrane-separates the concentrated water supplied from the second membrane separation unit 111-2 into permeated water and concentrated water. The third membrane separation unit 111-3, as well as discharged to the outside of the water treatment apparatus 1A as a first permeate W 2 permeate obtained by membrane separation, the concentrated water obtained by membrane separation fourth Supplied to the membrane separator 111-4.
　第４膜分離部１１１－４は、第３膜分離部１１１－３から供給された濃縮水を透過水と濃縮水とに膜分離する。また、第４膜分離部１１１－４は、膜分離により得られた透過水を第１透過水Ｗ２として水処理装置１Ａの外部に排出すると共に、膜分離により得られた濃縮水を第１濃縮水として第２膜処理部１１２の第１膜分離部１１２－１に供給する。 The fourth membrane separation unit 111-4 membrane-separates the concentrated water supplied from the third membrane separation unit 111-3 into permeated water and concentrated water. The fourth membrane separation unit 111-4, as well as discharged to the outside of the water treatment apparatus 1A as a first permeate W 2 permeate obtained by membrane separation, the concentrated water obtained by membrane separation first Concentrated water is supplied to the first membrane separation unit 112-1 of the second membrane processing unit 112.
　このように、第１膜処理部１１１は、第１分離膜１１１ａを含む複数の第１膜分離部１１１－１～第４膜分離部１１１－４が直列に接続されている。ここで、直列に接続とは、上流側の第１膜分離部１１１－１～第３膜分離部１１１－３の第１濃縮水が、次段の第２膜分離部１１１－２～第４膜分離部１１１－４に供給され、第１膜分離部１１１－１～第４膜分離部１１１－４の第１透過水Ｗ２が、第１膜処理部１１１の外部に排出されるように、第１膜分離部１１１－１～第４膜分離部１１１－４が接続されている状態をいう。これにより、第１膜処理部１１１は、被処理水Ｗ１を第１透過水Ｗ２と被処理水Ｗ１が順次濃縮された第１濃縮水とに膜分離し、第１透過水Ｗ２を水処理装置１Ａの外部に排出すると共に、高濃度に濃縮された第１濃縮水を第２膜処理部１１２に供給することができる。 Thus, the first membrane treatment unit 111 includes a plurality of first membrane separation units 111-1 to 111-4 including the first separation membrane 111a connected in series. Here, the series connection means that the first concentrated water of the first membrane separation unit 111-1 to the third membrane separation unit 111-3 on the upstream side is the second membrane separation unit 111-2 to the fourth of the next stage. The first permeated water W 2 supplied to the membrane separation unit 111-4 and discharged from the first membrane separation unit 111-1 to the fourth membrane separation unit 111-4 is discharged to the outside of the first membrane treatment unit 111. The state in which the first membrane separation unit 111-1 to the fourth membrane separation unit 111-4 are connected. As a result, the first membrane treatment unit 111 separates the treated water W 1 into the first permeated water W 2 and the first concentrated water obtained by sequentially concentrating the treated water W 1 , and the first permeated water W 2. Can be discharged to the outside of the water treatment apparatus 1 </ b> A, and the first concentrated water concentrated to a high concentration can be supplied to the second membrane treatment unit 112.
　第１膜分離部１１２－１は、第４膜分離部１１１－４から供給された第１濃縮水を透過水と濃縮水とに膜分離する。また、第１膜分離部１１２－１は、膜分離により得られた透過水を第２透過水Ｗ３として、膜分離モジュール１１に供給される被処理水Ｗ１に供給すると共に、膜分離により得られた濃縮水を第２膜分離部１１２－２に供給する。 The first membrane separation unit 112-1 membrane-separates the first concentrated water supplied from the fourth membrane separation unit 111-4 into permeated water and concentrated water. The first membrane separation unit 112-1, a permeate obtained by membrane separation as a second permeate W 3, and supplies the water to be treated W 1 supplied to the membrane separation module 11, the membrane separation The obtained concentrated water is supplied to the second membrane separation unit 112-2.
　第２膜分離部１１２－２は、第１膜分離部１１２－１から供給された濃縮水を透過水と濃縮水とに膜分離する。また、第２膜分離部１１２－２は、膜分離により得られた透過水を第２透過水Ｗ３として、膜分離モジュール１１に供給される被処理水Ｗ１に供給すると共に、膜分離により得られた濃縮水を第３膜分離部１１２－３に供給する。 The second membrane separation unit 112-2 membrane-separates the concentrated water supplied from the first membrane separation unit 112-1 into permeated water and concentrated water. The second membrane separation unit 112-2, a permeate obtained by membrane separation as a second permeate W 3, and supplies the water to be treated W 1 supplied to the membrane separation module 11, the membrane separation The obtained concentrated water is supplied to the third membrane separation unit 112-3.
　第３膜分離部１１２－３は、第２膜分離部１１２－２から供給された濃縮水を透過水と濃縮水とに膜分離する。また、第３膜分離部１１２－３は、膜分離により得られた透過水を第２透過水Ｗ３として、膜分離モジュール１１に供給される被処理水Ｗ１に供給すると共に、膜分離により得られた濃縮水を第２濃縮水Ｗ４として水処理装置１Ａの外部に排出する。 The third membrane separation unit 112-3 membrane-separates the concentrated water supplied from the second membrane separation unit 112-2 into permeated water and concentrated water. The third membrane separation unit 112-3, a permeate obtained by membrane separation as a second permeate W 3, and supplies the water to be treated W 1 supplied to the membrane separation module 11, the membrane separation the resulting concentrated solution as the second concentrated water W 4 is discharged to the outside of the water treatment apparatus 1A.
　このように、第２膜処理部１１２は、第２分離膜１１２ａを含む複数の第１膜分離部１１２－１～第３膜分離部１１２－３が直列に接続されている。ここで、直列に接続とは、上流側の第１膜分離部１１２－１、第２膜分離部１１２－２の第１濃縮水が、次段の第２膜分離部１１２－２、第３膜分離部１１２－３に供給され、第１膜分離部１１２－１～第３膜分離部１１２－３の第２透過水Ｗ３が、第２膜処理部１１２から、膜分離モジュール１１に供給される被処理水Ｗ１に供給されるように、第１膜分離部１１２－１～第３膜分離部１１２－３が接続されている状態をいう。これにより、第２膜処理部１１２は、第１膜処理部１１１から供給された第１濃縮水を、第２透過水Ｗ３と第１濃縮水が順次濃縮された第２濃縮水Ｗ４とに膜分離し、第２透過水Ｗ３を膜分離モジュール１１に供給される被処理水Ｗ１に供給すると共に、高濃度に濃縮された第２濃縮水Ｗ４を水処理装置１Ａの外部に排出することができる。そして、本実施の形態では、第１分離膜１１１ａに対して相対的に脱塩率が低い第２分離膜１１２ａを第１膜分離部１１２－１～第３膜分離部１１２－３に用いるので、第２透過水Ｗ３側でかかる透過水浸透圧を大きくすることが可能となる。これにより、第１膜分離部１１２－１～第３膜分離部１１２－３に第１分離膜１１１ａを用いる場合と比較して、第２濃縮水Ｗ４を高濃度に濃縮することが可能となるので、例えば、総溶解固形物（ＴＤＳ：Total Dissolved Solids）が８０，０００ｍｇ／Ｌ以上の高濃縮が可能となる。 As described above, in the second membrane treatment unit 112, the plurality of first membrane separation units 112-1 to 112-3 including the second separation membrane 112a are connected in series. Here, the series connection means that the first concentrated water from the first membrane separation unit 112-1 and the second membrane separation unit 112-2 on the upstream side is connected to the second membrane separation unit 112-2, the third is supplied to the membrane separation unit 112-3, supplying a second permeate W 3 of the first membrane separation unit 112-1 to the third membrane separation unit 112-3 is, from the second membrane unit 112, the membrane separation module 11 It is the to be supplied to the water to be treated W 1, means a state in which the first membrane separation unit 112-1 to the third membrane separation unit 112-3 is connected. Accordingly, the second membrane treatment unit 112 converts the first concentrated water supplied from the first membrane treatment unit 111 into the second concentrated water W 4 obtained by sequentially concentrating the second permeated water W 3 and the first concentrated water. to membrane separation, and supplies the water to be treated W 1 supplied a second permeate W 3 in the membrane separation module 11, the second concentrated water W 4 which is highly enriched in the outside of the water treatment apparatus 1A Can be discharged. In this embodiment, the second separation membrane 112a having a relatively low desalting rate relative to the first separation membrane 111a is used for the first membrane separation unit 112-1 to the third membrane separation unit 112-3. , it is possible to increase the permeate osmotic pressure according the second permeate W 3 side. Thus, the first membrane separation unit 112-1 to the third membrane separation unit 112-3 as compared with the case of using the first separation layer 111a, it is possible to concentrate the second concentrated water W 4 in a high concentration and Therefore, for example, it is possible to highly concentrate the total dissolved solids (TDS) at 80,000 mg / L or more.
　また、第２分離膜１１２ａとしては、膜分離後の第２濃縮水Ｗ４を高濃縮する観点から、第２分離膜１１２ａの脱塩率が８０％以下のものが好ましく、７０％以下のものがより好ましく、６０％以下のものが更に好ましい。また、第２分離膜１１２ａとしては、第２透過水Ｗ３中の塩類を低減する観点から、脱塩率が２０％以上のものが好ましく、３０％以上のものがより好ましく、４０％以上のものが更に好ましい。以上を考慮すると、第２分離膜１１２ａとしては、第１分離膜１１１ａの脱塩率に対する第２分離膜１１２ａの脱塩率が、２０％以上８０％以下のものが好ましく、３０％以上７０％以下のものがより好ましく、４０％以上６０％以下のものが更に好ましい。 Further, as the second separation membrane 112a, from the viewpoint of high concentration of the second concentrated water W 4 after membrane separation, desalting ratio thereof is preferably 80% or less of the second separation film 112a, those of 70% or less Is more preferable, and 60% or less is still more preferable. Further, as the second separation membrane 112a, from the viewpoint of reducing the salt of the second permeate W 3, salt rejection thereof is preferably 20% or more, more preferably not less than 30%, 40% or more More preferred. Considering the above, the second separation membrane 112a preferably has a desalination rate of the second separation membrane 112a of 20% to 80% with respect to the desalination rate of the first separation membrane 111a, preferably 30% to 70%. The following are more preferable, and those of 40% or more and 60% or less are more preferable.
　第２膜処理部１１２は、第１濃縮水の流れ方向における下流側に設けられた第２膜分離部１１２－２、第３膜分離部１１２－３の第２分離膜１１２ａの脱塩率が、上流側に設けられた第１膜分離部１１２－１、第２膜分離部１１２－２の第２分離膜１１２ａの脱塩率に対して相対的に低いことが好ましい。これにより、水処理装置１Ａは、第１濃縮水の流れ方向における上流側に設けられた第１膜分離部１１２－１、第２膜分離部１１２－２に対して、下流側に設けられた第２膜分離部１１２－２、第３膜分離部１１２－３の第２透過水Ｗ３側の透過水浸透圧が大きくなるので、第２濃縮水Ｗ４をより一層高濃度に濃縮することが可能となる。この場合、例えば、第１膜分離部１１２－１から第３膜分離部１１２－３に向けて、第２分離膜１１２ａの脱塩率が連続的に減少してもよく、脱塩率が段階的に減少してもよい。 The second membrane treatment unit 112 has a desalination rate of the second separation membrane 112a of the second membrane separation unit 112-2 and the third membrane separation unit 112-3 provided on the downstream side in the flow direction of the first concentrated water. It is preferable that the desalination rate of the second separation membrane 112a of the first membrane separation unit 112-1 and the second membrane separation unit 112-2 provided on the upstream side is relatively low. Thereby, the water treatment apparatus 1A is provided on the downstream side with respect to the first membrane separation unit 112-1 and the second membrane separation unit 112-2 provided on the upstream side in the flow direction of the first concentrated water. Since the permeated water osmotic pressure on the second permeated water W 3 side of the second membrane separating unit 112-2 and the third membrane separating unit 112-3 is increased, the second concentrated water W 4 is concentrated to a higher concentration. Is possible. In this case, for example, the desalination rate of the second separation membrane 112a may continuously decrease from the first membrane separation unit 112-1 to the third membrane separation unit 112-3, and the desalination rate is stepped. May be reduced.
　また、第２分離膜１１２ａとしては、膜分離後の第２濃縮水Ｗ４を高濃縮する観点から、透過水浸透圧が１．５ＭＰａ以上のものが好ましく、２．０ＭＰａ以上のものがより好ましく、２．５ＭＰａ以上のものが更に好ましく、３．０ＭＰａ以上のものがより更に好ましい。 Further, as the second separation membrane 112a, from the viewpoint of high concentration of the second concentrated water W 4 after membrane separation, preferably one permeate osmotic pressure is above 1.5 MPa, more preferably not less than 2.0MPa , More preferably 2.5 MPa or more, and even more preferably 3.0 MPa or more.
　次に、本実施の形態に係る水処理装置１Ａの全体動作について説明する。被処理水Ｗ１としての前処理水は、被処理水供給ラインＬ１を介して膜分離モジュール１１に供給される。膜分離モジュール１１に供給された被処理水Ｗ１は、第１膜処理部１１１の第１膜分離部１１１－１による膜分離で透過水と濃縮水とに膜分離される。第１膜分離部１１１－１で膜分離された透過水は、第１透過水Ｗ２として透過水排出ラインＬ２を介して水処理装置１Ａの外部に排出される。第１膜分離部１１１－１で膜分離された濃縮水は、第２膜分離部１１１－２～第４膜分離部１１１－４による膜分離で透過水と濃縮水とに順次膜分離される。第２膜分離部１１１－２～第４膜分離部１１１－４で膜分離された透過水は、第１透過水Ｗ２として透過水排出ラインＬ２を介して水処理装置１Ａの外部に排出される。第１膜分離部１１１－１～第４膜分離部１１１－４で順次濃縮された第１濃縮水は、第２膜処理部１１２の第１膜分離部１１２－１に供給される。 Next, the overall operation of the water treatment apparatus 1A according to the present embodiment will be described. Pretreated water as water to be treated W 1 is supplied to the membrane separation module 11 through the treated water supply line L 1. The treated water W 1 supplied to the membrane separation module 11 is membrane-separated into permeated water and concentrated water by membrane separation by the first membrane separation unit 111-1 of the first membrane treatment unit 111. Diafiltered permeate the first membrane separation unit 111-1, via the permeate discharge line L 2 is discharged to the outside of the water treatment apparatus 1A as a first permeate W 2. The concentrated water membrane-separated by the first membrane separation unit 111-1 is sequentially membrane-separated into permeated water and concentrated water by membrane separation by the second membrane separation unit 111-2 to the fourth membrane separation unit 111-4. . It diafiltered permeate in the second membrane separation unit 111-2 to the fourth membrane separation unit 111-4, discharged via the permeate discharge line L 2 to the outside of the water treatment apparatus 1A as a first permeate W 2 Is done. The first concentrated water sequentially concentrated by the first membrane separation unit 111-1 to the fourth membrane separation unit 111-4 is supplied to the first membrane separation unit 112-1 of the second membrane treatment unit 112.
　第１膜分離部１１２－１に供給された第１濃縮水は、第１膜分離部１１２－１による膜分離で第２透過水Ｗ３と第２濃縮水Ｗ４とに膜分離される。第１膜分離部１１２－１で膜分離された第２透過水Ｗ３は、透過水供給ラインＬ３を介して膜分離モジュール１１に供給される被処理水Ｗ１に供給される。第１膜分離部１１２－１で膜分離された第２濃縮水Ｗ４は、第２膜分離部１１２－２、第３膜分離部１１２－３による膜分離で第２透過水Ｗ３と第２濃縮水Ｗ４とに膜分離される。第２膜分離部１１２－２、第３膜分離部１１２－３で膜分離された第２透過水Ｗ３は、透過水供給ラインＬ３を介して膜分離モジュール１１に供給される被処理水Ｗ１に供給される第２膜分離部１１２－２、第３膜分離部１１２－３による膜分離で順次濃縮された高濃度の第２濃縮水Ｗ４は、濃縮水排出ラインＬ４を介して水処理装置１Ａの外部に排出される。 First concentrated water supplied to the first membrane separation unit 112-1 is membrane separation in the second permeate W 3 in the membrane separation of the first membrane separation unit 112-1 and the second concentrated water W 4. The second permeate W 3 which is membrane separated by the first membrane separation unit 112-1 is supplied to the water to be treated W 1 supplied to the membrane separation module 11 through the permeate supply line L 3. The second concentrated water W 4 membrane-separated by the first membrane separation unit 112-1 is separated from the second permeated water W 3 by the membrane separation by the second membrane separation unit 112-2 and the third membrane separation unit 112-3. is membrane separated into 2 concentrate W 4. The second membrane separation unit 112-2, the second permeate W 3 which is membrane separation by the third membrane separation unit 112-3, the treated water supplied to the membrane separation module 11 through the permeate supply line L 3 The high-concentration second concentrated water W 4 sequentially concentrated by membrane separation by the second membrane separation unit 112-2 and the third membrane separation unit 112-3 supplied to W 1 passes through the concentrated water discharge line L 4 . And discharged to the outside of the water treatment apparatus 1A.
　以上説明したように、上記実施の形態によれば、第１分離膜１１１ａで膜分離された第１濃縮水を第１分離膜１１１ａより相対的に脱塩率が低い第２分離膜１１２ａで膜分離するので、第２透過水Ｗ３側の透過水浸透圧が大きくなる。これにより、水処理装置１Ａは、第２分離膜１１２ａを用いずに第１分離膜１１１ａで被処理水Ｗ１を順次濃縮する場合と比較して、第２濃縮水Ｗ４を高濃度に濃縮することが可能となる。したがって、被処理水Ｗ１の膜分離後の第２濃縮水Ｗ４の総溶解固形物（ＴＤＳ：Total Dissolved Solids）が、例えば、８０，０００ｍｇ／Ｌ以上である高濃縮可能な水処理装置１Ａを実現できる。そして、水処理装置１Ａは、第２分離膜１１２ａで膜分離された不純物を含有し得る第２透過水Ｗ３を再度第２分離膜１１２ａに供給して膜分離するので、高純度の第１透過水Ｗ２を水処理装置１Ａの外部に取り出すことができる。また、第１膜処理部１１１及び第２膜処理部１１２を圧力容器１１０内に配置するので、水処理装置１Ａを小型化することもできる。 As described above, according to the above embodiment, the first concentrated water membrane-separated by the first separation membrane 111a is converted into a membrane by the second separation membrane 112a having a relatively lower desalting rate than the first separation membrane 111a. since separation, it permeates osmotic pressure of the second permeate W 3 side becomes greater. Thus, the water treatment device 1A, as compared with the case of sequentially concentrating treatment water W 1 in the first separation film 111a without using the second separation film 112a, concentrated second concentrated water W 4 in a high concentration It becomes possible to do. Thus, the total dissolved solids of the second concentrated water W 4 after the membrane separation of the treatment water W 1 (TDS: Total Dissolved Solids ) is, for example, high-condensable water treatment device 1A is 80,000mg / L or more Can be realized. The water treatment device 1A, since then supplied to the second separation film 112a in film may contain the separated impurities second permeate W 3 again second separation films 112a to membrane separation, high purity first the permeate W 2 can be taken out of the water treatment apparatus 1A. Moreover, since the 1st film | membrane process part 111 and the 2nd film | membrane process part 112 are arrange | positioned in the pressure vessel 110, 1 A of water treatment apparatuses can also be reduced in size.
　図１Ｂは、第１の実施の形態に係る水処理装置の他の例を示す模式図である。図１Ｂに示す水処理装置１Ｂは、図１Ａに示した水処理装置１Ａの構成に加えて、透過水排出ラインＬ２に設けた流量制御弁Ｖ２と、透過水供給ラインＬ３に設けられた流量制御弁Ｖ３とを備える。流量制御弁Ｖ２は、透過水供給ラインＬ２を流れる第１透過水Ｗ２の流量を制御する。流量制御弁Ｖ３は、透過水供給ラインＬ３を流れる第２透過水Ｗ３の流量を制御する。流量制御弁Ｖ２，Ｖ３の開度は、制御部２０によって制御される。制御部２０は、流量制御弁Ｖ２，Ｖ３の開度を変更することにより、第１膜処理部１１１から第１膜処理部１１１の外部に排出される第１透過水Ｗ２の水量及び第１膜処理部１１１に供給される被処理水Ｗ１に供給される第２透過水Ｗ３の水量をそれぞれ制御する。 FIG. 1B is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. Water treatment apparatus 1B shown in FIG. 1B, in addition to the configuration of the water treatment apparatus 1A shown in FIG. 1A, a flow control valve V 2 provided in the permeate discharge line L 2, provided permeate supply line L 3 It was provided with a flow control valve V 3. The flow control valve V 2 controls the first flow rate of the permeated water W 2 through the permeate supply line L 2. The flow control valve V 3 controls the flow rate of the second permeate W 3 through the permeate supply line L 3. Opening of the flow control valve V 2, V 3 is controlled by the control unit 20. The control unit 20 changes the opening of the flow rate control valves V 2 and V 3 to change the amount of the first permeated water W 2 discharged from the first membrane processing unit 111 to the outside of the first membrane processing unit 111 and the amount of water of the second permeate W 3 that is supplied to the water to be treated W 1 supplied to the first layer processing unit 111 controls, respectively.
　すなわち、水処理装置１Ｂでは、第１膜処理部１１１は、第１透過水Ｗ２の少なくとも一部を当該第１膜処理部１１１の外部に排出すると共に、第１透過水Ｗ２の少なくとも一部を透過水供給ラインＬ８により第１膜処理部１１１に供給される被処理水Ｗ１に供給可能となっている。また、第２膜処理部１１２は、第２透過水Ｗ３の少なくとも一部を第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、第２透過水Ｗ３の少なくとも一部を透過水供給ラインＬ９により水処置装置１Ｂの外部に排出可能となっている。このような構成により、第１透過水Ｗ２を再度第１分離膜１１１ａに供給して膜分離するので、被処理水の不純物が多い場合であっても、高純度の第１透過水Ｗ２を膜分離装置１Ｂの外部に取り出すことが可能となる。なお、図１Ｂに置いては、透過水排出ラインＬ２に流量制御弁Ｖ２を設けると共に、透過水供給ラインＬ３に流量制御弁Ｖ３を設ける例について説明したが、流量制御弁Ｖ２，Ｖ３は、少なくとも一方を設ける構成としてもよい。 That is, in the water treatment apparatus 1B, the first film processing section 111, at least a portion of the first permeate W 2 together with discharged to the outside of the first layer processing section 111, the first permeate W 2 at least a The portion can be supplied to the treated water W 1 supplied to the first membrane treatment unit 111 through the permeate supply line L 8 . The second film processing section 112 supplies the water to be treated W 1 supplied at least a portion of the second permeate W 3 in the first layer processing section 111, at least one second permeate W 3 It has become capable of discharging to the outside of the water treatment device 1B by permeated water supply line L 9 and parts. With such a configuration, the first permeated water W 2 is supplied again to the first separation membrane 111a and subjected to membrane separation. Therefore, even if there is a large amount of impurities in the water to be treated, the first permeated water W 2 with high purity is used. Can be taken out of the membrane separation apparatus 1B. Incidentally, the place in FIG. 1B, the permeate discharge line L 2 provided with a flow control valve V 2, an example has been described to provide a flow control valve V 3 to permeate supply line L 3, the flow control valve V 2 , V 3 may be provided with at least one of them.
　なお、図１Ａ，１Ｂに示した水処理装置１Ａ，１Ｂにおいては、被処理水Ｗ１として前処理水を用いた例について説明したが、被処理水Ｗ１は、前処理水に限定されない。図２Ａは、第１の実施の形態に係る水処理装置の他の例を示す模式図である。図２Ａに示すように、本実施の形態に係る水処理装置２Ａは、燃焼排ガスを洗浄水により洗浄する排煙脱硫部１２と、排煙脱硫部１２の後段に設けられた膜分離モジュール１１とを備える。排煙脱硫部１２は、火力発電所などから排出される燃焼排ガスを洗浄水などで洗浄して燃焼ガス中の硫黄分を除去する。また、排煙脱硫部１２は、燃焼排ガスの洗浄によって発生した硫黄分を含有する脱硫排水を、被処理水Ｗ１として被処理水供給ラインＬ１を介して膜分離モジュール１１に供給する。その他の構成については、図１に示した水処理装置１Ａと同様である。このような構成にすることにより、水処理装置２Ａは、脱硫排水を第２濃縮水Ｗ４として高濃度に濃縮することが可能となる。 In addition, in water treatment apparatus 1A, 1B shown to FIG. 1A, 1B, although the example using the pre-treatment water as the to-be-treated water W 1 was demonstrated, the to-be-treated water W 1 is not limited to the pre-treatment water. FIG. 2A is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. As shown in FIG. 2A, a water treatment apparatus 2A according to the present embodiment includes a flue gas desulfurization unit 12 that cleans combustion exhaust gas using washing water, and a membrane separation module 11 that is provided at a subsequent stage of the flue gas desulfurization unit 12. Is provided. The flue gas desulfurization unit 12 cleans combustion exhaust gas discharged from a thermal power plant or the like with cleaning water or the like to remove sulfur content in the combustion gas. Further, the flue gas desulfurization unit 12 supplies the desulfurization waste water containing the sulfur content generated by the cleaning of the combustion exhaust gas to the membrane separation module 11 as the treated water W 1 through the treated water supply line L 1 . About another structure, it is the same as that of 1 A of water treatment apparatuses shown in FIG. With such a configuration, the water treatment apparatus 2A, it is possible to highly concentrated the desulfurization effluent as a second concentrate W 4.
　図２Ｂは、第１の実施の形態に係る水処理装置の別の例を示す模式図である。図２Ｂに示すように、水処理装置２Ｂは、図２Ａに示した水処理装置２Ａの排煙脱硫部１２に代えて、逆浸透膜１３ａを備えた逆浸透膜濾過部１３を備える。逆浸透膜濾過部１３は、海水供給ラインＬ５を介して供給される海水Ｗ５を透過水Ｗ６と被処理水Ｗ１としての濃縮水とに膜分離する。また、逆浸透膜濾過部１３は、透過水排出ラインＬ６を介して透過水Ｗ６を排出すると共に、被処理水供給ラインＬ１を介して被処理水Ｗ１を膜分離モジュール１１に供給する。その他の構成については、図１に示した水処理装置１Ａと同様である。このような構成にすることにより、水処理装置２Ｂは、海水Ｗ５を第２濃縮水Ｗ４として高濃度に濃縮することが可能となる。 FIG. 2B is a schematic diagram illustrating another example of the water treatment device according to the first embodiment. As shown in FIG. 2B, the water treatment device 2B includes a reverse osmosis membrane filtration unit 13 including a reverse osmosis membrane 13a instead of the flue gas desulfurization unit 12 of the water treatment device 2A shown in FIG. 2A. Reverse osmosis membrane filtration unit 13 membrane separation in the concentrated water of the seawater W 5 supplied through a seawater supply line L 5 as permeate W 6 and water to be treated W 1. The reverse osmosis membrane filtration unit 13 discharges the permeated water W 6 via the permeate discharge line L 6 and supplies the treated water W 1 to the membrane separation module 11 via the treated water supply line L 1. To do. About another structure, it is the same as that of 1 A of water treatment apparatuses shown in FIG. With such a configuration, the water treatment apparatus 2B, it is possible to highly concentrated seawater W 5 as a second concentrate W 4.
（第２の実施の形態）
　次に、第２の実施の形態について説明する。なお、以下においては、上述した第１の実施の形態と共通する構成要素には同一の符号を付している。また、上述した第１の実施の形態との相違点を中心に説明し、説明の重複を避ける。 (Second Embodiment)
Next, a second embodiment will be described. In the following description, the same reference numerals are given to components common to the above-described first embodiment. Moreover, it demonstrates centering around difference with 1st Embodiment mentioned above, and avoids duplication of description.
　図３Ａは、第２の実施の形態に係る水処理装置の一例を示す模式図である。図３Ａに示すように、水処理装置３Ａは、図１に示した水処理装置１Ａの構成に加えて、膜分離モジュール１１の後段に設けられた蒸発処理部１４を備える。蒸発処理部１４は、膜分離モジュール１１から濃縮水排出ラインＬ４を介して供給される第２濃縮水Ｗ４から水分を蒸発させて蒸気を得ると共に、不純物が濃縮された残渣としての濃縮液及び固化物を得る。蒸発処理部１４としては、第２濃縮水Ｗ４中の水分を除去できるものであれば特に制限はなく、例えば、脱硫排水スプレードライヤ（ＷＳＤ：Wastewater Spray Dryer）などの各種スプレードライヤ、各種晶析装置などを用いることができる。また、蒸発処理部１４としては、第２濃縮水Ｗ４から水分を完全に蒸発させる必要がない場合には、蒸発濃縮器を用いてもよい。 FIG. 3A is a schematic diagram illustrating an example of a water treatment device according to the second embodiment. As shown in FIG. 3A, the water treatment device 3A includes an evaporation processing unit 14 provided in the subsequent stage of the membrane separation module 11 in addition to the configuration of the water treatment device 1A shown in FIG. The evaporation processing unit 14 evaporates moisture from the second concentrated water W 4 supplied from the membrane separation module 11 via the concentrated water discharge line L 4 to obtain steam, and also concentrates as a residue in which impurities are concentrated. And a solidified product is obtained. The evaporation processing unit 14 is not particularly limited as long as it can remove the water in the second concentrated water W 4. For example, various spray dryers such as a desulfurization waste water spray dryer (WSD), various crystallizations, and the like. A device or the like can be used. As the evaporation section 14, when it is not necessary to completely evaporate the water from the second concentrated water W 4, it may be used evaporative concentrator.
　図３Ｂは、第２の実施の形態に係る水処理装置の他の例を示す模式図である。図３Ｂに示すように、水処理装置３Ｂは、図１に示した水処理装置１Ａの構成に加えて、膜分離モジュール１１の後段に設けられた後処理部１５を備える。後処理部１５は、膜分離モジュール１１から濃縮水排出ラインＬ４を介して供給される第２濃縮水Ｗ４中に各種薬剤などを添加して、石炭灰、ライムなどのアルカリ及びセメントなどの第２濃縮水Ｗ４中の不純物を固化する。また、後処理部１５は、後処理水排出ラインＬ７を介して不純物を除去した後処理水Ｗ７を排出する。ここでは、後処理部１５は、イオン交換樹脂を使用したイオン交換処理及びキレート樹脂を使用したキレート処理などにより第２濃縮水Ｗ４中に含まれる有害金属などの不純物を除去してもよい。このような第２濃縮水Ｗ４中の不純物を除去する後処理部１５を設けることにより、第２濃縮水Ｗ４中の不純物を除去して放流することが可能となる。 FIG. 3B is a schematic diagram illustrating another example of the water treatment device according to the second embodiment. As shown in FIG. 3B, the water treatment device 3B includes a post-treatment unit 15 provided in the subsequent stage of the membrane separation module 11 in addition to the configuration of the water treatment device 1A shown in FIG. The post-processing unit 15 adds various chemicals and the like to the second concentrated water W 4 supplied from the membrane separation module 11 via the concentrated water discharge line L 4, so that alkali such as coal ash and lime, cement, and the like are added. Impurities in the second concentrated water W 4 are solidified. The post-treatment unit 15 discharges the post-treatment water W 7 from which impurities are removed via the post-treatment water discharge line L 7 . Here, the post-processing unit 15 may remove impurities such as harmful metals contained in the second concentrated water W 4 by ion exchange treatment using an ion exchange resin and chelate treatment using a chelate resin. By providing a post-processing unit 15 to remove impurities such second concentrated water W in 4, it is possible to discharge by removing the impurities of the second concentrated water W 4.
　なお、後処理部１５では、水銀吸着用キレート樹脂及びセレン（Ｓｅ）吸着用キレート樹脂などの各種キレート樹脂を用いることにより、水銀及びセレンが除去された後処理水Ｗ７を得ることもできる。水銀吸着用キレート樹脂としては、例えば、商品名：エポラス（登録商標）、型番：Ｚ－７、Ｚ－１００などが用いられる。セレン吸着用キレート樹脂としては、商品名：エポラス（登録商標）、型番：ＳＥ－３、ＡＳ－４などが用いられる。 In the post-processing unit 15, by using various chelating resins such as chelates for mercury adsorption resin and selenium (Se) adsorption chelate resin can also be obtained post-treatment water W 7 that mercury and selenium are removed. As the chelate resin for mercury adsorption, for example, trade name: Eporus (registered trademark), model number: Z-7, Z-100, etc. are used. As the chelating resin for adsorbing selenium, trade names: Eporus (registered trademark), model numbers: SE-3, AS-4, etc. are used.
　以上説明したように、本実施の形態によれば、第２濃縮水Ｗ４を蒸発処理する蒸発処理部１４を設けることにより、第２濃縮水Ｗ４の水分を蒸気として放出することができるので、水処理装置３Ａから排出される排水を大幅に削減することが可能となる。また、第２濃縮水Ｗ４中の不純物を除去する後処理部１５を設けることにより、第２濃縮水Ｗ４中の不純物を除去して放流することができるので、水処理装置３Ｂから排出される排水処理が必要となる排水を大幅に削減することが可能となる。 As described above, according to this embodiment, by providing the evaporation unit 14 for evaporated the second concentrated water W 4, since the water of the second concentrate W 4 can be released as a vapor The waste water discharged from the water treatment device 3A can be greatly reduced. In addition, by providing the post-processing unit 15 that removes impurities in the second concentrated water W 4 , impurities in the second concentrated water W 4 can be removed and discharged, so that the water is discharged from the water treatment device 3B. It is possible to greatly reduce the amount of wastewater that requires wastewater treatment.
（第３の実施の形態）
　次に、第３の実施の形態について説明する。なお、以下においては、上述した第１の実施の形態と共通する構成要素には同一の符号を付している。また、上述した第１の実施の形態との相違点を中心に説明し、説明の重複を避ける。 (Third embodiment)
Next, a third embodiment will be described. In the following description, the same reference numerals are given to components common to the above-described first embodiment. Moreover, it demonstrates centering around difference with 1st Embodiment mentioned above, and avoids duplication of description.
　図４Ａは、第３の実施の形態に係る水処理装置の一例を示す模式図である。図４Ａに示すように、本実施の形態に係る水処理装置４Ａは、被処理水Ｗ１として前処理水が供給される第１膜処理部１１１と、第１膜処理部１１１の後段に設けられた第２膜処理部１１２とを備える。第１膜処理部１１１は、第１膜処理部１１１に供給される被処理水Ｗ１を第１透過水Ｗ１１Ａ～第１透過水Ｗ１４Ａと第１濃縮水Ｗ１１Ｂ～第１濃縮水Ｗ１４Ｂとに膜分離して、第１透過水Ｗ１１Ａ～第１透過水Ｗ１４Ａを外部に排出する。第２膜処理部１１２は、第１濃縮水Ｗ１４Ｂを第２透過水Ｗ１５Ａ～第２透過水Ｗ１７Ａと第２濃縮水Ｗ１５Ｂ～第２濃縮水Ｗ１７Ｂとに膜分離する。第２膜処理部１１２は、第２濃縮水Ｗ１７Ｂを外部に排出すると共に、第２透過水Ｗ１５Ａ～第２透過水Ｗ１７Ａを第１膜処理部１１１に供給される被処理水Ｗ１に供給する。 FIG. 4A is a schematic diagram illustrating an example of a water treatment device according to the third embodiment. As shown in FIG. 4A, the water treatment apparatus 4A according to the present embodiment includes a first layer processing section 111 for pre-treated water is supplied as the water to be treated W 1, provided after the first layer processing section 111 The second film processing unit 112 is provided. The first layer processing section 111, the water to be treated W 1 supplied to the first layer processing section 111 first permeate W 11A ~ first permeate W 14A in the first concentrated water W 11B ~ first concentrated water W and membrane separation in the 14B, for discharging the first permeate W 11A ~ first permeate W 14A to the outside. The second membrane treatment unit 112 membrane-separates the first concentrated water W 14B into the second permeated water W 15A to the second permeated water W 17A and the second concentrated water W 15B to the second concentrated water W 17B . The second membrane treatment unit 112 discharges the second concentrated water W 17B to the outside, and the treated water W 1 supplied with the second permeated water W 15A to the second permeated water W 17A to the first membrane treatment unit 111. To supply.
　第１膜処理部１１１は、被処理水Ｗ１及び第１濃縮水Ｗ１１Ｂ～第１濃縮水Ｗ１３Ｂを、第１透過水Ｗ１１Ａ～第１透過水Ｗ１４Ａと第１濃縮水Ｗ１４Ｂとに膜分離する第１分離膜１１１ａを有する複数（本実施の形態では４つ）の膜分離部：第１膜分離部１１１－１～第４膜分離部１１１－４を備える。第１膜処理部１１１は、被処理水Ｗ１が供給される第１膜分離部１１１－１と、第１膜分離部１１１－１の後段に設けられた第２膜分離部１１１－２と、第２膜分離部１１１－２の後段に設けられた第３膜分離部１１１－３と、第３膜分離部１１１－３の後段に設けられた第４膜分離部１１１－４とを備える。第１分離膜１１１ａとしては、上述した第１の実施の形態に係る水処理装置１Ａと同様のものを用いることができる。なお、本実施の形態では、第１膜処理部１１１が、４つの膜分離部１１１－１～１１１－４を備える例について説明するが、第１膜処理部１１１は、少なくとも一つの膜分離部を備えていればよく、膜分離部の数は適宜変更可能である。 The first membrane treatment unit 111 includes the treated water W 1 and the first concentrated water W 11B to the first concentrated water W 13B , the first permeated water W 11A to the first permeated water W 14A, and the first concentrated water W 14B . A plurality of (four in the present embodiment) membrane separation units having a first separation membrane 111a for membrane separation: a first membrane separation unit 111-1 to a fourth membrane separation unit 111-4. The first layer processing unit 111, a first membrane separation unit 111-1 for-treatment water W 1 is supplied, a second membrane separation unit 111-2 disposed downstream of the first membrane separation unit 111-1 A third membrane separation unit 111-3 provided in the subsequent stage of the second membrane separation unit 111-2, and a fourth membrane separation unit 111-4 provided in the subsequent stage of the third membrane separation unit 111-3. . As the 1st separation membrane 111a, the thing similar to 1 A of water treatment apparatuses which concern on 1st Embodiment mentioned above can be used. In the present embodiment, an example in which the first membrane treatment unit 111 includes four membrane separation units 111-1 to 111-4 will be described. However, the first membrane treatment unit 111 includes at least one membrane separation unit. The number of membrane separation parts can be changed as appropriate.
　第２膜処理部１１２は、第１濃縮水Ｗ１４Ｂ及び第２濃縮水Ｗ１５Ｂ，Ｗ１６Ｂを第２透過水Ｗ１５Ａ～第２透過水Ｗ１７Ａと第２濃縮水Ｗ１５Ｂ～第２濃縮水Ｗ１７Ｂとに膜分離する第２分離膜１１２ａを有する複数の（本実施の形態では３つ）の膜分離部：第１膜分離部１１２－１～第３膜分離部１１２－３を備える。第２膜処理部１１２は、第１濃縮水Ｗ１４Ｂが供給される第１膜分離部１１２－１と、第１膜分離部１１２－１の後段に設けられた第２膜分離部１１２－２と、第２膜分離部１１２－２の後段に設けられた第３膜分離部１１２－３とを備える。第２分離膜１１２ａとしては、上述した第１の実施の形態に係る水処理装置１Ａと同様のものを用いることができる。なお、本実施の形態では、３つの膜分離部１１２－１～１１２－３を備える例について説明するが、第２膜処理部１１２は、少なくとも一つの膜分離部を備えていればよく、膜分離部の数は適宜変更可能である。 The second membrane treatment unit 112 converts the first concentrated water W 14B and the second concentrated water W 15B and W 16B into the second permeated water W 15A to the second permeated water W 17A and the second concentrated water W 15B to the second concentrated water. A plurality of (three in the present embodiment) membrane separation units having a second separation membrane 112a that performs membrane separation into W 17B : a first membrane separation unit 112-1 to a third membrane separation unit 112-3. The second membrane treatment unit 112 includes a first membrane separation unit 112-1 to which the first concentrated water W 14B is supplied, and a second membrane separation unit 112-2 provided at the subsequent stage of the first membrane separation unit 112-1. And a third membrane separation unit 112-3 provided at the subsequent stage of the second membrane separation unit 112-2. As the 2nd separation membrane 112a, the thing similar to 1 A of water treatment apparatuses which concern on 1st Embodiment mentioned above can be used. In the present embodiment, an example in which three membrane separation units 112-1 to 112-3 are provided will be described. However, the second membrane processing unit 112 may include at least one membrane separation unit, and the membrane The number of separation parts can be changed as appropriate.
　第１膜分離部１１１－１は、例えば排煙脱硫部から供給された被処理水Ｗ１を第１透過水Ｗ１１Ａと第１濃縮水Ｗ１１Ｂとに膜分離する。また、第１膜分離部１１１－１は、透過水排出ラインＬ１１Ａを介して膜分離により得られた第１透過水Ｗ１１Ａを水処理装置４Ａの外部に排出すると共に、濃縮水供給ラインＬ１１Ｂを介して第１濃縮水Ｗ１１Ｂを第２膜分離部１１１－２に供給する。 The first membrane separation unit 111-1, for example, membrane separation treatment water W 1 supplied from the flue gas desulfurization unit into a first permeate W 11A in the first concentrated water W 11B. Further, the first membrane separation unit 111-1 discharges the first permeate W 11A obtained by membrane separation via the permeate discharge line L 11A to the outside of the water treatment device 4A, and also supplies the concentrated water supply line L The first concentrated water W 11B is supplied to the second membrane separation unit 111-2 through 11B .
　第２膜分離部１１１－２は、第１膜分離部１１１－１から供給された第１濃縮水Ｗ１１Ｂを第１透過水Ｗ１２Ａと第１濃縮水Ｗ１２Ｂとに膜分離する。また、第２膜分離部１１１－２は、透過水排出ラインＬ１２Ａを介して膜分離により得られた第１透過水Ｗ１２Ａを水処理装置４Ａの外部に排出すると共に、濃縮水供給ラインＬ１２Ｂを介して第１濃縮水Ｗ１２Ｂを第３膜分離部１１１－３に供給する。 The second membrane separation unit 111-2 membrane-separates the first concentrated water W 11B supplied from the first membrane separation unit 111-1 into a first permeated water W 12A and a first concentrated water W 12B . The second membrane separation unit 111-2 discharges the first permeated water W 12A obtained by membrane separation through the permeated water discharge line L 12A to the outside of the water treatment device 4A, and also supplies the concentrated water supply line L The first concentrated water W 12B is supplied to the third membrane separation unit 111-3 through 12B .
　第３膜分離部１１１－３は、第２膜分離部１１１－２から供給された第１濃縮水Ｗ１２Ｂを第１透過水Ｗ１３Ａと第１濃縮水Ｗ１３Ｂとに膜分離する。また、第３膜分離部１１１－３は、透過水排出ラインＬ１３Ａを介して膜分離により得られた第１透過水Ｗ１３Ａを水処理装置４Ａの外部に排出すると共に、濃縮水供給ラインＬ１３Ｂを介して第１濃縮水Ｗ１３Ｂを第４膜分離部１１１－４に供給する。 The third membrane separation unit 111-3, membrane separates the first concentrated water W 12B supplied from the second membrane separation unit 111-2 into a first permeate W 13A in the first concentrated water W 13B. The third membrane separation unit 111-3 discharges the first permeated water W 13A obtained by membrane separation through the permeated water discharge line L 13A to the outside of the water treatment device 4A, and also supplies the concentrated water supply line L The first concentrated water W 13B is supplied to the fourth membrane separation unit 111-4 through 13B .
　第４膜分離部１１１－４は、第３膜分離部１１１－３から供給された第１濃縮水Ｗ１３Ｂを第１透過水Ｗ１４Ａと第１濃縮水Ｗ１４Ｂとに膜分離する。また、第４膜分離部１１１－４は、透過水排出ラインＬ１４Ａを介して膜分離により得られた第１透過水Ｗ１４Ａを水処理装置４Ａの外部に排出すると共に、濃縮水供給ラインＬ１４Ｂを介して第１濃縮水Ｗ１４Ｂを第２膜処理部１１２の第１膜分離部１１２－１に供給する。 The fourth membrane separation unit 111-4 membrane-separates the first concentrated water W 13B supplied from the third membrane separation unit 111-3 into the first permeated water W 14A and the first concentrated water W 14B . Further, the fourth membrane separation unit 111-4 discharges the first permeated water W 14A obtained by membrane separation through the permeated water discharge line L 14A to the outside of the water treatment device 4A, and also supplies the concentrated water supply line L The first concentrated water W 14B is supplied to the first membrane separation unit 112-1 of the second membrane processing unit 112 via 14B .
　このように、第１膜処理部１１１は、第１分離膜１１１ａを含む複数の第１膜分離部１１１－１～第４膜分離部１１１－４が直列に配置されている。これにより、第１膜処理部１１１は、被処理水Ｗ１を、第１透過水Ｗ１１Ａ～Ｗ１４Ａと被処理水Ｗ１が第１膜分離部１１１－１～第４膜分離部１１１－４によって順次濃縮された第１濃縮水Ｗ１１Ｂ～Ｗ１４Ｂとに膜分離し、第１透過水Ｗ１１Ａ～Ｗ１４Ａを水処理装置４Ａの外部に排出すると共に、濃縮された第１濃縮水Ｗ１４Ｂを第２膜処理部１１２に供給することができる。 As described above, the first membrane treatment unit 111 includes a plurality of first membrane separation units 111-1 to 111-4 including the first separation membrane 111a arranged in series. As a result, the first membrane treatment unit 111 converts the treated water W 1 into the first permeated water W 11A to W 14A and the treated water W 1 from the first membrane separation unit 111-1 to the fourth membrane separation unit 111-. 4 is separated into the first concentrated water W 11B to W 14B that are sequentially concentrated by 4, and the first permeated water W 11A to W 14A is discharged to the outside of the water treatment device 4A and the concentrated first concentrated water W 14B can be supplied to the second film processing unit 112.
　第１膜分離部１１２－１は、第４膜分離部１１１－４から供給された第１濃縮水Ｗ１４Ｂを第２透過水Ｗ１５Ａと第２濃縮水Ｗ１５Ｂとに膜分離する。また、第１膜分離部１１２－１は、透過水供給ラインＬ１５Ａを介して膜分離により得られた第２透過水Ｗ１５Ａを第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、濃縮水供給ラインＬ１５Ｂを介して第２濃縮水Ｗ１５Ｂを第２膜分離部１１２－２に供給する。 The first membrane separation unit 112-1 membrane-separates the first concentrated water W 14B supplied from the fourth membrane separation unit 111-4 into the second permeated water W 15A and the second concentrated water W 15B . Further, the first membrane separation unit 112-1 uses the second permeated water W 15A obtained by membrane separation via the permeated water supply line L 15A as the treated water W 1 supplied to the first membrane treatment unit 111. At the same time, the second concentrated water W 15B is supplied to the second membrane separation unit 112-2 through the concentrated water supply line L 15B .
　第２膜分離部１１２－２は、第１膜分離部１１２－１から供給された第２濃縮水Ｗ１５Ｂを第２透過水Ｗ１６Ａと第２濃縮水Ｗ１６Ｂとに膜分離する。また、第２膜分離部１１２－２は、透過水供給ラインＬ１６Ａを介して膜分離により得られた第２透過水Ｗ１６Ａを第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、濃縮水供給ラインＬ１６Ｂを介して第２濃縮水Ｗ１６Ｂを第３膜分離部１１２－３に供給する。 The second membrane separation unit 112-2 membrane-separates the second concentrated water W 15B supplied from the first membrane separation unit 112-1 into a second permeated water W 16A and a second concentrated water W 16B . In addition, the second membrane separation unit 112-2 uses the second permeated water W 16A obtained by membrane separation via the permeated water supply line L 16A as the treated water W 1 supplied to the first membrane treatment unit 111. At the same time, the second concentrated water W 16B is supplied to the third membrane separation unit 112-3 via the concentrated water supply line L 16B .
　第３膜分離部１１２－３は、第２膜分離部１１２－２から供給された第２濃縮水Ｗ１６Ｂを第２透過水Ｗ１７Ａと第２濃縮水Ｗ１７Ｂとに膜分離する。また、第３膜分離部１１２－３は、透過水供給ラインＬ１７Ａを介して膜分離により得られた第２透過水Ｗ１７Ａを第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、濃縮水排出ラインＬ１７Ｂを介して第２濃縮水Ｗ１７Ｂを水処理装置４Ａの外部に排出する。 The third membrane separation unit 112-3 membrane-separates the second concentrated water W 16B supplied from the second membrane separation unit 112-2 into a second permeated water W 17A and a second concentrated water W 17B . Further, the third membrane separation unit 112-3 supplies the second permeated water W 17A obtained by membrane separation via the permeated water supply line L 17A to the treated water W 1 supplied to the first membrane treatment unit 111. supplies, the second concentrated water W 17B is discharged to the outside of the water treatment device 4A through the concentrated water discharge line L 17B.
　このように、第２膜処理部１１２は、第２分離膜１１２ａを含む複数の第１膜分離部１１２－１～第３膜分離部１１２－３が直列に配置されている。これにより、第２膜処理部１１２は、第１膜処理部１１１から供給された第１濃縮水Ｗ１４Ｂを第２透過水Ｗ１５Ａ～Ｗ１７Ａと第２濃縮水Ｗ１５Ｂが順次濃縮された第２濃縮水Ｗ１５Ｂ～Ｗ１７Ｂとに膜分離し、第２透過水Ｗ１５Ａ～Ｗ１７Ａを第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、高濃度に濃縮された第２濃縮水Ｗ１７Ｂを水処理装置４Ａの外部に排出することができる。そして、本実施の形態では、第１分離膜１１１ａに対して相対的に脱塩率が低い第２分離膜１１２ａを第１膜分離部１１２－１～第３膜分離部１１２－３に用いるので、第２透過水Ｗ１５Ａ～Ｗ１７Ａ側でかかる透過水浸透圧を大きくすることが可能となる。これにより、第１膜分離部１１２－１～第３膜分離部１１２－３に第１分離膜１１１ａを用いる場合と比較して、第２濃縮水Ｗ１７Ｂを高濃度に濃縮することが可能となるので、例えば、総溶解固形物（ＴＤＳ：Total Dissolved Solids）が８０，０００ｍｇ／Ｌ以上の高濃縮が可能となる。 Thus, in the second membrane treatment unit 112, the plurality of first membrane separation units 112-1 to 112-3 including the second separation membrane 112a are arranged in series. As a result, the second membrane treatment unit 112 is configured such that the second permeated water W 15A to W 17A and the second concentrated water W 15B are sequentially concentrated from the first concentrated water W 14B supplied from the first membrane treatment unit 111. 2 The membrane was separated into concentrated water W 15B to W 17B, and the second permeated water W 15A to W 17A was supplied to the water to be treated W 1 supplied to the first membrane treatment unit 111 and concentrated to a high concentration. The second concentrated water W 17B can be discharged to the outside of the water treatment device 4A. In this embodiment, the second separation membrane 112a having a relatively low desalting rate relative to the first separation membrane 111a is used for the first membrane separation unit 112-1 to the third membrane separation unit 112-3. The permeated water osmotic pressure can be increased on the second permeated water W 15A to W 17A side. As a result, it is possible to concentrate the second concentrated water W 17B to a higher concentration than when the first separation membrane 111a is used for the first membrane separation unit 112-1 to the third membrane separation unit 112-3. Therefore, for example, it is possible to highly concentrate the total dissolved solids (TDS) at 80,000 mg / L or more.
　次に、本実施の形態に係る水処理装置４Ａの全体動作について説明する。被処理水Ｗ１としての前処理水は、被処理水供給ラインＬ１を介して膜分離モジュール１１に供給される。膜分離モジュール１１に供給された被処理水Ｗ１は、第１膜処理部１１１の第１膜分離部１１１－１による膜分離で第１透過水Ｗ１１Ａと第１濃縮水Ｗ１１Ｂとに膜分離される。第１膜分離部１１１－１で膜分離された第１透過水Ｗ１１Ａは、透過水排出ラインＬ１１Ａを介して水処理装置４Ａの外部に排出される。第１膜分離部１１１－１で膜分離された第１濃縮水Ｗ１１Ｂは、第２膜分離部１１１－１～第４膜分離部１１１－４による膜分離で第１透過水Ｗ１２Ａ～Ｗ１４Ａと第１濃縮水Ｗ１２Ｂ～Ｗ１４Ｂとに膜分離される。第２膜分離部１１１－２～第４膜分離部１１１－４で膜分離された第１透過水Ｗ１２Ａ～Ｗ１４Ａは、透過水排出ラインＬ１２Ａ～Ｌ１４Ａを介して水処理装置４Ａの外部に排出される。第１膜分離部１１１－１～第４膜分離部１１１－４で順次濃縮された第１濃縮水Ｗ１４Ｂは、第２膜処理部１１２の第１膜分離部１１２－１に供給される。 Next, the overall operation of the water treatment device 4A according to the present embodiment will be described. Pretreated water as water to be treated W 1 is supplied to the membrane separation module 11 through the treated water supply line L 1. The treated water W 1 supplied to the membrane separation module 11 is converted into a first permeated water W 11A and a first concentrated water W 11B by membrane separation by the first membrane separation unit 111-1 of the first membrane treatment unit 111. To be separated. The first permeated water W 11A membrane-separated by the first membrane separation unit 111-1 is discharged to the outside of the water treatment device 4A through the permeated water discharge line L 11A . The first concentrated water W 11B membrane-separated by the first membrane separation unit 111-1 is subjected to membrane separation by the second membrane separation unit 111-1 to the fourth membrane separation unit 111-4 and the first permeated water W 12A to W The membrane is separated into 14A and first concentrated waters W 12B to W 14B . The first permeated water W 12A to W 14A membrane-separated by the second membrane separating unit 111-2 to the fourth membrane separating unit 111-4 is passed through the permeated water discharge lines L 12A to L 14A . It is discharged outside. The first concentrated water W 14B sequentially concentrated by the first membrane separation unit 111-1 to the fourth membrane separation unit 111-4 is supplied to the first membrane separation unit 112-1 of the second membrane treatment unit 112.
　第１膜分離部１１２－１に供給された第１濃縮水Ｗ１４Ｂは、第１膜分離部１１２－１による膜分離で第２透過水Ｗ１５Ａと第２濃縮水Ｗ１５Ｂとに膜分離される。第１膜分離部１１２－１で膜分離された第２透過水Ｗ１５Ａは、透過水供給ラインＬ１５Ａを介して第１膜処理部１１１に供給される被処理水Ｗ１に供給される。第１膜分離部１１２－１で膜分離された第２濃縮水Ｗ１５Ｂは、第２膜分離部１１２－２、第３膜分離部１１２－３による膜分離で第２透過水Ｗ１６Ａ，Ｗ１７Ａと第２濃縮水Ｗ１６Ｂ，Ｗ１７Ｂとに膜分離される。第２膜分離部１１２－２、第３膜分離部１１２－３で膜分離された第２透過水Ｗ１６Ａ，Ｗ１７Ａは、透過水供給ラインＬ１６Ａ，Ｌ１７Ａを介して第１膜処理部１１１に供給される被処理水Ｗ１に供給される。第２膜分離部１１２－２、第３膜分離部１１２－３による膜分離で順次濃縮された高濃度の第２濃縮水Ｗ１７Ｂは、濃縮水排出ラインＬ１７Ｂを介して水処理装置４Ａの外部に排出される。 The first concentrated water W 14B supplied to the first membrane separation unit 112-1 is membrane-separated into the second permeated water W 15A and the second concentrated water W 15B by membrane separation by the first membrane separation unit 112-1. The The second permeated water W 15A membrane-separated by the first membrane separation unit 112-1 is supplied to the treated water W 1 supplied to the first membrane processing unit 111 via the permeated water supply line L 15A . The second concentrated water W 15B membrane-separated by the first membrane separation unit 112-1 is converted into the second permeated water W 16A , W by membrane separation by the second membrane separation unit 112-2 and the third membrane separation unit 112-3. The membrane is separated into 17A and second concentrated water W 16B and W 17B . The second permeated water W 16A and W 17A membrane-separated by the second membrane separation unit 112-2 and the third membrane separation unit 112-3 are passed through the permeated water supply lines L 16A and L 17A. Supplied to the treated water W 1 supplied to 111. The high-concentration second concentrated water W 17B, which is successively concentrated by membrane separation by the second membrane separation unit 112-2 and the third membrane separation unit 112-3, is supplied to the water treatment device 4A via the concentrated water discharge line L 17B . It is discharged outside.
　以上説明したように、上記実施の形態によれば、第１分離膜１１１ａで膜分離された第１濃縮水Ｗ１４Ｂを第１分離膜１１１ａより相対的に脱塩率が低い第２分離膜１１２ａで膜分離するので、第２透過水Ｗ１５Ａ～Ｗ１７Ａ側の透過水浸透圧が大きくなる。これにより、水処理装置４Ａは、第２分離膜１１２ａを用いずに第２分離膜１１２ａで被処理水Ｗ１を順次濃縮する場合と比較して、被処理水Ｗ１を高濃度に濃縮することが可能となる。そして、水処理装置４Ａは、第２分離膜１１２ａで膜分離された不純物を含有し得る第２透過水Ｗ１５Ａ、Ｗ１６Ａを再度第１分離膜１１１ａに供給して膜分離するので、高純度の第１透過水Ｗ１１Ａ～Ｗ１４Ａを水処理装置４Ａの外部に取り出すことができる。したがって、被処理水Ｗ１の膜分離後の第２濃縮水Ｗ１５Ｂ～Ｗ１７Ｂの総溶解固形物（ＴＤＳ：Total Dissolved Solids）が、例えば、８０，０００ｍｇ／Ｌ以上である高濃縮可能な水処理装置４Ａを実現できる。 As described above, according to the above embodiment, the first concentrated water W 14B which are membrane separation in the first separation film 111a first separation film 111a relatively more salt rejection is lower second separation films 112a Therefore, the permeated water osmotic pressure on the second permeated water W 15A to W 17A side is increased. Thus, the water treatment device 4A, as compared with the case of sequentially concentrating treatment water W 1 in the second separation film 112a without using the second separation film 112a, concentrating water to be treated W 1 at a high concentration It becomes possible. The water treatment device 4A, second permeate W 15A which may contain membrane separated impurities in the second separation membrane 112a, since then supplied to the first separation film 111a to W 16A again membrane separation, high purity The first permeated water W 11A to W 14A can be taken out of the water treatment apparatus 4A. Therefore, the water that can be highly concentrated in which the total dissolved solids (TDS: Total Dissolved Solids) of the second concentrated water W 15B to W 17B after membrane separation of the water to be treated W 1 is, for example, 80,000 mg / L or more. The processing device 4A can be realized.
　図４Ｂは、第３の実施の形態に係る水処理装置の他の例を示す模式図である。図４Ｂに示す水処理装置４Ｂは、図４Ａに示した水処理装置４Ａの構成に加えて、透過水排出ラインＬ１１Ａから分岐され、被処理水供給ラインＬ１に接続された透過水供給ラインＬ１４ｃと、透過水供給ラインＬ１７Ａから分岐された透過水排出ラインＬ１７ｃとを備える。透過水供給ラインＬ１４Ｃは、第１膜処理部１１１で膜分離された第１透過水Ｗ１１Ａ～Ｗ１４Ａを第１透過水Ｗ１４Ｃとして被処理水Ｗ１に供給し、透過水排出ラインＬ１７ｃは、第２膜処理１１２で膜分離された第２透過水Ｗ１７Ａを第２透過水Ｗ１７Ｃとして水処理装置４Ｂの外部に排出する。すなわち、水処理装置４Ｂでは、第１膜処理部１１１は、第１透過水Ｗ１１Ａ～Ｗ１４Ａの少なくとも一部を当該第１膜処理部１１１の外部に排出すると共に、第１透過水Ｗ１１Ａ～Ｗ１４Ａの少なくとも一部を第１透過水Ｗ１４Ｃとして第１膜処理部１１１に供給される被処理水Ｗ１に供給可能となっている。また、第２膜処理部１１２は、第２透過水Ｗ１７Ａの少なくとも一部を第１膜処理部１１１に供給される被処理水Ｗ１に供給すると共に、第２透過水Ｗ１７Ａの少なくとも一部を第２透過水Ｗ１７Ｃとして水処置装置４Ｂの外部に排出可能となっている。 FIG. 4B is a schematic diagram illustrating another example of the water treatment device according to the third embodiment. Water treatment apparatus 4B shown in FIG. 4B, in addition to the configuration of the water treatment apparatus 4A shown in FIG. 4A, is branched from the permeate discharge line L 11A, connected to permeate supply line to the water to be treated supply line L 1 L 14c and a permeate discharge line L 17c branched from the permeate supply line L 17A . The permeated water supply line L 14C supplies the first permeated water W 11A to W 14A membrane-separated by the first membrane treatment unit 111 to the treated water W 1 as the first permeated water W 14C , and the permeated water discharge line L 17c discharges the second permeate W 17A which are membrane separation in the second film processing 112 to the outside of the water treatment device 4B as a second permeate W 17C. That is, in the water treatment apparatus 4B, the first membrane treatment unit 111 discharges at least a part of the first permeate water W 11A to W 14A to the outside of the first membrane treatment unit 111 and the first permeate water W 11A. and it can be supplied to the water to be treated W 1 supplied to the first layer processing section 111 at least a portion of the ~ W 14A as a first permeate W 14C. Further, the second membrane treatment unit 112 supplies at least a part of the second permeated water W 17A to the treated water W 1 supplied to the first membrane treatment unit 111 and at least one of the second permeated water W 17A . The portion can be discharged to the outside of the water treatment device 4B as the second permeated water W17C .
　透過水供給ラインＬ１４Ｃには、透過水供給ラインＬ１４Ｃを流れる第１透過水Ｗ１４Ｃの流量を制御する流量制御弁Ｖ１４Ｃが設けられ、透過水排出ラインＬ１７Ｃには、透過水排出ラインＬ１７Ｃを流れる第２透過水Ｗ１７Ｃの流量を制御する流量制御弁Ｖ１７Ｃが設けられている。また、透過水供給ラインＬ１７Ａには、透過水供給ラインＬ１７Ａを流れる第２透過水Ｗ１７Ａの流量を制御する流量制御弁Ｖ１７Ａが設けられている。また、透過水排出ラインＬ１１Ａの透過水供給ラインＬ１４Ｃとの分岐部の後流側には、透過水排出ラインＬ１１Ａを流れる第１透過水Ｗ１１Ａ～Ｗ１４Ａの流量を制御する流量制御弁Ｖ１４Ａが設けられている。流量制御弁Ｖ１４Ａ，Ｖ１４Ｃ，Ｖ１７Ａ，Ｖ１７Ｃの開度は、制御部２０によって制御される。制御部２０は、流量制御弁Ｖ１４Ａ，Ｖ１４Ｃ，Ｖ１７Ａ，Ｖ１７Ｃの開度を変更することにより、第１膜処理部１１１から第１膜処理部１１１の外部に排出される第１透過水Ｗ１１Ａ～Ｗ１４Ａの水量及び第１膜処理部１１１に供給される被処理水Ｗ１に供給される第１透過水Ｗ１１Ａ～Ｗ１４Ｃの水量、並びに、第２膜処理部１１２から第１膜処理部１１１に供給される被処理水Ｗ１に供給される第２透過水Ｗ１７Ａの水量及び水処置装置４Ｂの外部に排出される第２透過水Ｗ１７Ｃの水量を制御する。このような構成により、第１透過水Ｗ１４Ｃを再度第１分離膜１１１ａに供給して膜分離するので、被処理水Ｗ１の不純物が多い場合であっても、高純度の第１透過水Ｗ１１Ａ～Ｗ１４Ａを水処理装置４Ｂの外部に取り出すことが可能となる。 The permeated water supply line L 14C is provided with a flow rate control valve V 14C for controlling the flow rate of the first permeated water W 14C flowing through the permeated water supply line L 14C . The permeated water discharge line L 17C is provided with a permeated water discharge line. A flow rate control valve V 17C for controlling the flow rate of the second permeated water W 17C flowing through L 17C is provided. In addition, the permeate supply line L 17A, the flow control valve V 17A for controlling the flow rate of the second permeate W 17A through the permeate supply line L 17A is provided. Further, a flow rate control for controlling the flow rates of the first permeate water W 11A to W 14A flowing through the permeate discharge line L 11A on the downstream side of the branch portion of the permeate discharge line L 11A with the permeate supply line L 14C. A valve V14A is provided. The opening degree of the flow rate control valves V 14A , V 14C , V 17A , V 17C is controlled by the control unit 20. The control unit 20 changes the opening degree of the flow control valves V 14A , V 14C , V 17A , V 17C , and thereby the first permeation discharged from the first film processing unit 111 to the outside of the first film processing unit 111. The amount of water W 11A to W 14A, the amount of first permeated water W 11A to W 14C supplied to the water to be treated W 1 supplied to the first membrane treatment unit 111, and the second membrane treatment unit 112 to controlling the amount of water of the second permeate W 17C is discharged to the outside of the water and the water treatment device 4B of the second permeate W 17A to be supplied to the water to be treated W 1 supplied to the first-layer processing unit 111. With such a configuration, the first permeated water W 14C is supplied again to the first separation membrane 111a for membrane separation, so even if there is a large amount of impurities in the water to be treated W 1 , the high-purity first permeated water W 11A to W 14A can be taken out of the water treatment device 4B.
　１Ａ，１Ｂ，２Ａ，２Ｂ，３Ａ，３Ｂ，４Ａ，４Ｂ　水処理装置
　１１　膜分離モジュール
　１１１　第１膜処理部
　１１１ａ　第１分離膜
　１１１－１　第１膜分離部
　１１１－２　第２膜分離部
　１１１－３　第３膜分離部
　１１１－４　第４膜分離部
　１１２　第２膜処理部
　１１２ａ　第２分離膜
　１１２－１　第１膜分離部
　１１２－２　第２膜分離部
　１１２－３　第３膜分離部
　１２　排煙脱硫部
　１３　逆浸透膜濾過部
　１３ａ　逆浸透膜
　１４　蒸発処理部
　１５　後処理部
　２０　制御部
　Ｗ１　被処理水
　Ｗ２，Ｗ１１Ａ，Ｗ１２Ａ，Ｗ１３Ａ，Ｗ１４Ａ，Ｗ１４Ｃ　第１透過水
　Ｗ１１Ｂ，Ｗ１２Ｂ，Ｗ１３Ｂ，Ｗ１４Ｂ　第１濃縮水
　Ｗ３，Ｗ１５Ａ，Ｗ１６Ａ，Ｗ１７Ａ，Ｗ１７Ｃ　第２透過水
　Ｗ４，Ｗ１５Ｂ，Ｗ１６Ｂ，Ｗ１７Ｂ　第２濃縮水
　Ｗ５　海水
　Ｗ６　透過水
　Ｗ７　後処理水
　Ｌ１　被処理水供給ライン
　Ｌ２，Ｌ３Ａ，Ｌ６，Ｌ１１Ａ，Ｌ１２Ａ，Ｌ１３Ａ，Ｌ１４Ａ，Ｌ１７Ｃ　透過水排出ライン
　Ｌ２Ａ，Ｌ３，Ｌ１４Ｃ，Ｌ１５Ａ，Ｌ１６Ａ，Ｌ１７Ａ　透過水供給ライン
　Ｌ４，Ｌ１７Ｂ　濃縮水排出ライン
　Ｌ５　海水供給ライン
　Ｌ１１Ｂ，Ｌ１２Ｂ，Ｌ１３Ｂ，Ｌ１４Ｂ，Ｌ１５Ｂ，Ｌ１６Ｂ　濃縮水供給ライン
　Ｌ７　後処理水排出ライン
　Ｖ２，Ｖ２Ａ，Ｖ３，Ｖ３Ａ，Ｖ１４Ａ，Ｖ１４Ｃ，Ｖ１７Ａ，Ｖ１７Ｃ　流量制御弁 1A, 1B, 2A, 2B, 3A, 3B, 4A, 4B Water treatment device 11 Membrane separation module 111 First membrane treatment section 111a First separation membrane 111-1 First membrane separation section 111-2 Second membrane separation section 111 -3 Third membrane separation unit 111-4 Fourth membrane separation unit 112 Second membrane treatment unit 112a Second separation membrane 112-1 First membrane separation unit 112-2 Second membrane separation unit 112-3 Third membrane separation unit 12 FGD unit 13 reverse osmosis membrane filtration unit 13a reverse osmosis membrane 14 evaporator unit 15 the post-processing section 20 control section W 1 water to be treated W 2, W 11A, W 12A , W 13A, W 14A, W 14C first permeate W 11B, W 12B, W 13B , W 14B first concentrated water W 3, W 15A, W 16A , W 17A, W 17C second permeate W 4, W 15B, W 16B , W 17B second concentrated water W 5 seawater W 6 permeated water W 7 post-treatment water L 1 treated water supply line L 2 , L 3A , L 6 , L 11A , L 12A , L 13A , L 14A , L 17C Permeated water discharge line L 2A , L 3 , L 14C, L 15A, L 16A, L 17A permeate supply line L 4, L 17B concentrated water discharge line L 5 seawater supply line L 11B, L 12B, L 13B , L 14B, L 15B, L 16B concentrated water supply line L 7 post-processing water discharge line V 2, V 2A, V 3 , V 3A, V 14A, V 14C, V 17A, V 17C flow control valve

Claims (12)

  1. 　被処理水を第１濃縮水と第１透過水とに膜分離する第１分離膜を有する少なくとも一つの膜分離部を備えた第１膜処理部と、
    　前記第１濃縮水を第２透過水と第２濃縮水とに膜分離する前記第１分離膜より相対的に脱塩率が低い第２分離膜を有する少なくとも一つの膜分離部を備えた第２膜処理部と、を具備し、
    　前記第１膜処理部は、前記第１透過水の少なくとも一部を当該第１膜処理部の外部に排出する一方、前記被処理水から膜分離された前記第１濃縮水を前記第２膜処理部に供給し、
    　前記第２膜処理部は、前記第２透過水の少なくとも一部を前記第１膜処理部に供給される前記被処理水に供給する一方、前記第１濃縮水から膜分離された前記第２濃縮水を排出することを特徴とする、水処理装置。     A first membrane treatment unit comprising at least one membrane separation unit having a first separation membrane for membrane separation of treated water into first concentrated water and first permeated water;
    A first separation unit having a second separation membrane having a lower desalination rate than the first separation membrane for separating the first concentrated water into a second permeated water and a second concentrated water; A two-film processing unit,
    The first membrane treatment unit discharges at least a part of the first permeate to the outside of the first membrane treatment unit, while the first concentrated water separated from the treated water by the second membrane Supply to the processing section,
    The second membrane treatment unit supplies at least a part of the second permeated water to the treated water supplied to the first membrane treatment unit, while the second membrane-separated from the first concentrated water. A water treatment apparatus for discharging concentrated water.
  2. 　前記第１膜処理部は、前記第１透過水の少なくとも一部を前記第１膜処理部に供給される前記被処理水に供給する、請求項１に記載の水処理装置。 The water treatment device according to claim 1, wherein the first membrane treatment unit supplies at least a part of the first permeated water to the water to be treated supplied to the first membrane treatment unit.
  3. 　前記第２分離膜の脱塩率が、前記第１分離膜の脱塩率の８０％以下である、請求項１又は請求項２に記載の水処理装置。 The water treatment device according to claim 1 or 2, wherein the desalination rate of the second separation membrane is 80% or less of the desalination rate of the first separation membrane.
  4. 　前記第１膜処理部は、複数の前記膜分離部を備え、前記被処理水から膜分離された濃縮水を複数の前記膜分離部により順次濃縮して前記第１濃縮水として前記第２膜処理部に供給し、
    　前記第２膜処理部は、複数の前記膜分離部を備え、前記第１膜処理部から供給された前記第１濃縮水から膜分離された濃縮水を複数の前記膜分離部により順次濃縮して前記第２濃縮水として排出することを特徴とする、請求項１から請求項３のいずれか１項に記載の水処理装置。     The first membrane treatment unit includes a plurality of the membrane separation units, and sequentially concentrates the concentrated water separated from the water to be treated by the plurality of membrane separation units as the first concentrated water. Supply to the processing section,
    The second membrane treatment unit includes a plurality of the membrane separation units, and sequentially concentrates the concentrated water separated from the first concentrated water supplied from the first membrane treatment unit by the plurality of membrane separation units. The water treatment device according to any one of claims 1 to 3, wherein the water treatment device is discharged as the second concentrated water.
  5. 　前記第２膜処理部は、前記第１濃縮水の流れ方向における下流側に設けられた前記膜分離部の前記第２分離膜の脱塩率が、上流側に設けられた前記第２膜処理部の前記第２分離膜の脱塩率に対して相対的に低い、請求項４に記載の水処理装置。 In the second membrane treatment unit, the desalination rate of the second separation membrane of the membrane separation unit provided on the downstream side in the flow direction of the first concentrated water is the second membrane treatment provided on the upstream side. The water treatment apparatus according to claim 4, which is relatively low with respect to a desalting rate of the second separation membrane of a part.
  6. 　前記第１膜処理部及び前記第２膜処理部が内部に設けられた圧力容器をさらに備えた、請求項１から請求項５のいずれか１項に記載の水処理装置。 The water treatment apparatus according to any one of claims 1 to 5, further comprising a pressure vessel in which the first membrane treatment unit and the second membrane treatment unit are provided.
  7. 　前記被処理水が、燃焼排ガスを脱硫する排煙脱硫部から排出される脱硫排水を含む、請求項１から請求項６のいずれか１項に記載の水処理装置。 The water treatment apparatus according to any one of claims 1 to 6, wherein the water to be treated includes desulfurization drainage discharged from a flue gas desulfurization unit that desulfurizes combustion exhaust gas.
  8. 　前記被処理水が、前処理により海水中の濁質を除去してなる前処理水を含む、請求項１から請求項６のいずれか１項に記載の水処理装置。 The water treatment apparatus according to any one of claims 1 to 6, wherein the treated water includes pretreated water obtained by removing turbidity in seawater by pretreatment.
  9. 　前記第２濃縮水を蒸発させて蒸発水を得る蒸発処理部をさらに備えた、請求項１から請求項８のいずれか１項に記載の水処理装置。 The water treatment apparatus according to any one of claims 1 to 8, further comprising an evaporation processing unit that evaporates the second concentrated water to obtain evaporated water.
  10. 　前記第２濃縮水中の不純物を除去して後処理水を得る後処理部をさらに備えた、請求項１から請求項８のいずれか１項に記載の水処理装置。 The water treatment apparatus according to any one of claims 1 to 8, further comprising a post-treatment unit that removes impurities in the second concentrated water to obtain post-treatment water.
  11. 　前記後処理部は、前記第２濃縮水中に薬剤を添加して前記不純物を固化して除去する、請求項１０に記載の水処理装置。 The water treatment device according to claim 10, wherein the post-treatment unit solidifies and removes the impurities by adding a chemical to the second concentrated water.
  12. 　第１分離膜を備えた少なくとも一つの膜分離部により被処理水を第１透過水と第１濃縮水とに膜分離する第１膜処理工程と、
    　前記第１分離膜より相対的に脱塩率が低い第２分離膜を備えた少なくとも一つの膜分離部により前記第１濃縮水を第２透過水と第２濃縮水とに膜分離する第２膜処理工程とを含み、
    　前記第１膜処理工程では、前記第１透過水の少なくとも一部を排出する一方、前記被処理水から膜分離された前記第１濃縮水を前記膜分離部に供給し、
    　前記第２膜処理工程では、前記第２透過水の少なくとも一部を前記膜分離部に供給される前記被処理水に供給する一方、前記第１濃縮水から膜分離された前記第２濃縮水を排出することを特徴とする、水処理方法。     A first membrane treatment step of membrane-separating treated water into first permeated water and first concentrated water by at least one membrane separation section having a first separation membrane;
    A second separator that separates the first concentrated water into a second permeated water and a second concentrated water by at least one membrane separation section having a second separation membrane having a lower desalting rate than the first separation membrane; Including a membrane treatment process,
    In the first membrane treatment step, while discharging at least a part of the first permeated water, supplying the first concentrated water membrane-separated from the treated water to the membrane separation unit,
    In the second membrane treatment step, at least a part of the second permeated water is supplied to the water to be treated supplied to the membrane separation unit, while the second concentrated water is membrane-separated from the first concentrated water. A water treatment method characterized by discharging water.
PCT/JP2018/010872 2018-03-19 2018-03-19 Water treatment device and water treatment method WO2019180789A1 (en)

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