JP7816616B2 - Electrodeionization apparatus and its operating method - Google Patents
Electrodeionization apparatus and its operating methodInfo
- Publication number
- JP7816616B2 JP7816616B2 JP2025075454A JP2025075454A JP7816616B2 JP 7816616 B2 JP7816616 B2 JP 7816616B2 JP 2025075454 A JP2025075454 A JP 2025075454A JP 2025075454 A JP2025075454 A JP 2025075454A JP 7816616 B2 JP7816616 B2 JP 7816616B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- concentrated
- treated
- concentrated water
- concentration
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
Description
本発明は、電気脱イオン装置及びその運転方法に関し、特に高水質の処理水を効率よく製造することの可能な電気脱イオン装置及びその運転方法に関する。 The present invention relates to an electrodeionization apparatus and its operating method, and in particular to an electrodeionization apparatus and its operating method that can efficiently produce high-quality treated water.
電気脱イオン装置は、一般に陰極（カソード）及び陽極（アノード）間にカチオン交換膜とアニオン交換膜とを交互に配置し、これらカチオン交換膜及びアニオン交換膜により区画を構成することで脱塩室及び濃縮室を形成し、この脱塩室及び濃縮室にイオン交換樹脂を充填したものである。カチオン交換膜やアニオン交換膜などのイオン交換膜としては、粉末状のイオン交換樹脂にポリスチレンなどの結合剤を加えて製膜した不均質膜や、スチレン－ジビニルベンゼン等の重合によって製膜した均質膜などのほか、各種アニオン交換機能あるいはカチオン交換機能を有する単量体をグラフト重合により製膜したものなどが用いられている。 An electrodeionization device generally consists of alternating cation exchange membranes and anion exchange membranes arranged between a negative electrode (cathode) and a positive electrode (anode), with deionization and concentration compartments formed by these cation exchange and anion exchange membranes. These deionization and concentration compartments are filled with ion exchange resin. Ion exchange membranes such as cation exchange and anion exchange membranes include heterogeneous membranes made by adding a binder such as polystyrene to powdered ion exchange resin, homogeneous membranes made by polymerizing styrene-divinylbenzene, and membranes made by graft polymerization of various monomers with anion or cation exchange functions.
この電気脱イオン装置としては、図６及び図７に示すような構成を有するものが特許文献１に開示されている。 Patent Document 1 discloses an electrodeionization device having the configuration shown in Figures 6 and 7.
図６において、電気脱イオン装置２１は、電極（陽極３１、陰極３２）の間に複数のアニオン交換膜３３及びカチオン交換膜３４を交互に配列して濃縮室３５と脱塩室３６とを交互に形成したものであり、脱塩室３６には、イオン交換樹脂、イオン交換繊維もしくはグラフト交換体等からなるイオン交換体（アニオン交換体及びカチオン交換体）が混合もしくは複層状に充填されている。また、濃縮室３５と、正極室３７及び陰極室３８にも、イオン交換体が充填されている。 In Figure 6, the electrodeionization device 21 has multiple anion exchange membranes 33 and cation exchange membranes 34 arranged alternately between electrodes (anode 31, cathode 32) to form alternating concentration compartments 35 and deionization compartments 36. The deionization compartments 36 are filled with a mixture or multiple layers of ion exchangers (anion exchangers and cation exchangers) made of ion exchange resin, ion exchange fibers, graft exchangers, etc. In addition, the concentration compartments 35, positive electrode compartment 37, and cathode compartment 38 are also filled with ion exchangers.
この電気脱イオン装置２１には、脱塩室３６に被処理水Ｗ１を通水して処理水Ｗ２を取り出す通水手段（図示せず）と、濃縮室３５に濃縮水Ｗ３を通水する濃縮水通水手段（図示せず）とが設けられていて、本実施形態においては濃縮水Ｗ３を脱塩室３６の処理水Ｗ２の取り出し口に近い側から濃縮室３５内に導入すると共に、脱塩室３６の入口に近い側から流出する、すなわち脱塩室３６における被処理水Ｗ１の流通方向と反対方向から濃縮水Ｗ３を濃縮室３５に導入して濃縮排水Ｗ４を吐出する構成となっている。そして、この濃縮水Ｗ３としては、給水（被処理水Ｗ１）よりシリカ又はホウ素濃度の低い水を、該濃縮室のうち脱塩室の脱イオン水取り出し口に近い側から該濃縮室内に導入すると共に、該濃縮室のうち脱塩室の原水入口に近い側から流出させることが記載されている。 This electrodeionization device 21 is equipped with a water-passing means (not shown) for passing water W1 to be treated through the deionization chamber 36 and extracting treated water W2, and a concentrated water-passing means (not shown) for passing concentrated water W3 through the concentration chamber 35. In this embodiment, concentrated water W3 is introduced into the concentration chamber 35 from the side of the deionization chamber 36 closer to the treated water W2 outlet and flows out from the side closer to the inlet of the deionization chamber 36. In other words, concentrated water W3 is introduced into the concentration chamber 35 in the opposite direction to the flow of water W1 to be treated through the deionization chamber 36, and concentrated wastewater W4 is discharged. The description also describes how concentrated water W3, which has a lower silica or boron concentration than the feedwater (water W1 to be treated), is introduced into the concentration chamber from the side closer to the deionized water outlet of the deionization chamber and flows out from the side closer to the raw water inlet of the deionization chamber.
特に図７に示すように脱塩室３６から得られる処理水Ｗ２の一部を濃縮水Ｗ３として用いることで、イオン濃度が低減された濃縮排水Ｗ４を流通することが好ましい態様として記載されている。 In particular, as shown in Figure 7, a preferred embodiment is described in which a portion of the treated water W2 obtained from the deionization chamber 36 is used as concentrated water W3, and concentrated wastewater W4 with a reduced ion concentration is circulated.
このような電気脱イオン装置は、種々の産業、例えば半導体チップの製造工程、火力又は原子力発電所、石油化学工場、医薬品製造工程などにおいて純水製造装置として利用されている。 Such electrodeionization devices are used as pure water production equipment in a variety of industries, such as semiconductor chip manufacturing processes, thermal or nuclear power plants, petrochemical plants, and pharmaceutical manufacturing processes.
特に半導体市場で要求される生産水の水質は高く、処理水比抵抗値１５ＭΩ・ｃｍ以上や、高いホウ素・シリカ除去率が必要な場合も多い。また、近年は、処理水水質の高純度化に加え、節電や節水も考慮した運転条件設定が求められている。 The semiconductor market in particular demands high quality produced water, often requiring a specific resistance of 15 MΩ-cm or more and a high boron and silica removal rate. In recent years, there has also been a demand for operating conditions that take into account energy and water conservation in addition to achieving high levels of purity in the treated water.
また、半導体製造工程向けの汎用的な電気脱イオン装置として、Ｘｙｌｅｍ社製のＩＰ－ＶＮＸ－５５ＥＸ－２が市販されている。図８に示すようにこの電気脱イオン装置４０は、フレーム５０内にサブブロック４１～４６を備えている。各サブブロック４１～４６は、交互に配置されたカチオン交換膜ＣＥＭとアニオン交換膜ＡＥＭとによって、脱塩室と濃縮室のペアが複数個形成されたものである。 The IP-VNX-55EX-2, manufactured by Xylem, is a commercially available general-purpose electrodeionization apparatus for use in semiconductor manufacturing processes. As shown in Figure 8, this electrodeionization apparatus 40 comprises sub-blocks 41 to 46 within a frame 50. Each of the sub-blocks 41 to 46 is made up of alternating cation exchange membranes (CEM) and anion exchange membranes (AEM), forming multiple pairs of deionization and concentration compartments.
この電気脱イオン装置４０のサブブロック４１，４３は、脱塩室と濃縮室のペアを１７個備え、サブブロック４２は該ペアを１６個備えている。サブブロック４４，４６は該ペアを１７個備え、サブブロック４５は該ペアを１６個備えている。なお、図８中の「－」は陰極室４７を示し、「＋」は正極室４８を示す。符号４９は電源ボックスを示す。 Sub-blocks 41 and 43 of this electrodeionization device 40 each have 17 pairs of deionization compartments and concentration compartments, while sub-block 42 has 16 such pairs. Sub-blocks 44 and 46 each have 17 such pairs, and sub-block 45 has 16 such pairs. Note that in Figure 8, "-" indicates the cathode compartment 47, and "+" indicates the cathode compartment 48. Reference numeral 49 denotes the power supply box.
図８に示す電気脱イオン装置４０の運転方法では、サブブロック４１～４３に給水（被処理水）Ｗ１と、濃縮水Ｗ３がそれぞれのポートから供給される。給水Ｗ１の一部は、サブブロック４１～４３の給水路（上側ヘッド部）を通過してサブブロック４４～４６の給水路（上側ヘッド部）に供給される。この給水は、各サブブロック４１～４６の各脱塩室を通り、脱塩水集水路（下側ヘッド部）を経て処理水取出ポートから処理水Ｗ２として取り出される。 In the operating method of the electrodeionization apparatus 40 shown in Figure 8, feedwater (water to be treated) W1 and concentrated water W3 are supplied to sub-blocks 41-43 from their respective ports. A portion of feedwater W1 passes through the water supply channels (upper head sections) of sub-blocks 41-43 and is supplied to the water supply channels (upper head sections) of sub-blocks 44-46. This feedwater passes through each desalination chamber of each sub-block 41-46, passes through the desalinated water collection channel (lower head section), and is extracted from the treated water extraction port as treated water W2.
濃縮水はサブブロック４１～４３のヘッド部（上側ヘッド部）に供給され、サブブロック４１～４３の各濃縮室を通過し、サブブロック４１～４３の濃縮水集水路（下側ヘッド部）からサブブロック４４～４６の濃縮水ヘッド部（下側ヘッド部）に導入され、サブブロック４４～４６の各濃縮室に通水され、サブブロック４４～４６の濃縮室の上側ヘッド部を経て濃縮排水取出ポートから濃縮排水Ｗ４として取り出される。すなわち、図８に示す電気脱イオン装置４０では、すべての脱塩室に給水Ｗ１を下降流にて通水している。一方、濃縮水Ｗ３通水向きは、前半（サブブロック４１，４２，４３）は下降流とし、後半（サブブロック４４，４５，４６）は上向流としている。このようにサブブロック４１～４３とサブブロック４４～４６とで濃縮水Ｗ３の通水方向を逆にすることで濃縮排水Ｗ４の使用水量を半分にしている。 Concentrated water is supplied to the heads (upper heads) of sub-blocks 41-43, passes through each concentration chamber of sub-blocks 41-43, and is introduced through the concentrated water collection channels (lower heads) of sub-blocks 41-43 to the concentrated water heads (lower heads) of sub-blocks 44-46. The water is then passed through each concentration chamber of sub-blocks 44-46, passes through the upper heads of the concentration chambers of sub-blocks 44-46, and is discharged as concentrated wastewater W4 from the concentrated wastewater outlet port. In other words, in the electrodeionization device 40 shown in Figure 8, water supply W1 flows downward through all deionization chambers. Meanwhile, the flow direction of concentrated water W3 is downward in the first half (sub-blocks 41, 42, 43) and upward in the second half (sub-blocks 44, 45, 46). By reversing the flow direction of concentrated water W3 between sub-blocks 41-43 and sub-blocks 44-46, the amount of concentrated wastewater W4 used is halved.
しかしながら、図８に示す電気脱イオン装置４０の通水方法によると、サブブロック４４～４６は、脱塩室下部と濃縮室下部とでイオン濃度差が大きくなるため、濃度拡散により濃縮室から脱塩室へイオンが移動し、処理水水質が低下してしまう、という問題点がある。 However, with the water flow method of the electrodeionization device 40 shown in Figure 8, the difference in ion concentration between the lower part of the deionization compartment and the lower part of the concentration compartment in the sub-blocks 44-46 becomes large, causing ions to move from the concentration compartment to the deionization compartment due to concentration diffusion, resulting in a deterioration in the quality of the treated water.
そこで、本出願人は、図９に示すような電気脱イオン装置を出願した（特許文献２、特許文献３）。この電気脱イオン装置１は、フレーム２，２間にサブブロック３Ａ～３Ｆを並設してなる。各サブブロック３Ａ～３Ｆは、交互に配置されたカチオン交換膜ＣＥＭとアニオン交換膜ＡＥＭとによって、脱塩室（図示せず）と濃縮室（図示せず）のペアが複数個形成されたものである。これらサブブロック３Ａ～３Ｆが連設したセルの一側（図示上側）の両端部には、脱塩室に被処理水Ｗ１を通水するための給水ライン４を配設する給水ポート４Ａ，４Ｂが形成されている一方、セルの他側（図示下側）の両端部には、脱塩室で処理した脱イオン水としての処理水Ｗ２を排出するための処理水流出ライン５を配設する処理水流出ポート５Ａ，５Ｂが形成されている。給水ライン４は、それぞれサブブロック３Ａ～３Ｆにおいて分岐していて、被処理水流入分岐管として各脱塩室の上側に接続しているとともに、各脱塩室の下側には、処理水流出管が連通していて、これら各処理水流出管が処理水流出ライン５に合流している。これにより、被処理水Ｗ１を給水ポート４Ａ，４Ｂ側から給水ライン４を経て各脱塩室の上側から供給し、さらに各脱塩室の下側から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から処理水Ｗ２を排出可能となっている。 Therefore, the applicant filed patent applications for an electrodeionization apparatus as shown in Figure 9 (Patent Document 2 and Patent Document 3). This electrodeionization apparatus 1 comprises sub-blocks 3A-3F arranged side by side between frames 2, 2. Each sub-block 3A-3F has multiple pairs of deionization compartments (not shown) and concentration compartments (not shown) formed by alternatingly arranged cation exchange membranes CEM and anion exchange membranes AEM. Water supply ports 4A and 4B are formed at both ends of one side (the upper side in the figure) of the cell in which these sub-blocks 3A-3F are connected, and through which water supply lines 4 are installed to pass water W1 to be treated into the deionization compartments. Meanwhile, treated water outlet ports 5A and 5B are formed at both ends of the other side (the lower side in the figure) of the cell, and through which treated water outlet lines 5 are installed to discharge treated water W2, which is deionized water treated in the deionization compartments. The water supply line 4 branches off in each of the sub-blocks 3A to 3F, connecting the upper side of each deionization chamber as a treated water inlet branch pipe, while a treated water outlet pipe is connected to the lower side of each deionization chamber, and these treated water outlet pipes merge into the treated water outlet line 5. This allows treated water W1 to be supplied from the upper side of each deionization chamber via the water supply line 4 from the water supply ports 4A and 4B, and treated water W2 can be discharged from the lower side of each deionization chamber via the treated water outlet line 5 and the treated water outlet ports 5A and 5B.
また、サブブロック３Ａ～３Ｆが連設したセルの図示下側の両端部には、濃縮室に濃縮水Ｗ３を通水するための濃縮水供給ライン６を配設する濃縮水給水ポート６Ａ，６Ｂが形成されている一方、セルの図示上側の両端部には、濃縮排水Ｗ４を排出するための濃縮排水流出ライン７を配設する濃縮排水流出ポート７Ａ，７Ｂが形成されている。濃縮水供給ライン６は、それぞれサブブロック３Ａ～３Ｆにおいて分岐して濃縮水流入分岐管として各濃縮室の下側に接続しているとともに、各濃縮室の上側には濃縮排水流出管が連通していて、これら各濃縮排水流出管が濃縮排水流出ライン７に合流している。これにより、濃縮水Ｗ３を濃縮水給水ポート６Ａ，６Ｂ側から濃縮水供給ライン６を経て各濃縮室の下側から供給し、さらに各濃縮室の上側から濃縮排水Ｗ４を濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出可能となっている。 Furthermore, concentrated water supply ports 6A, 6B are formed at both ends of the lower side of the cell in which sub-blocks 3A-3F are connected, and a concentrated water supply line 6 is provided for passing concentrated water W3 through the concentration chambers. Concentrated wastewater outlet ports 7A, 7B are formed at both ends of the upper side of the cell, and a concentrated wastewater outlet line 7 is provided for discharging concentrated wastewater W4. The concentrated water supply line 6 branches off in each of the sub-blocks 3A-3F and connects to the lower side of each concentration chamber as a concentrated water inlet branch pipe. Concentrated wastewater outlet pipes are connected to the upper side of each concentration chamber, and these concentrated wastewater outlet pipes merge into the concentrated wastewater outlet line 7. This allows concentrated water W3 to be supplied from the lower side of each concentration chamber via the concentrated water supply line 6 from the concentrated water supply ports 6A, 6B, and the concentrated wastewater W4 can be discharged from the upper side of each concentration chamber via the concentrated wastewater outlet line 7 and from the concentrated wastewater outlet ports 7A, 7B.
図９に示す電気脱イオン装置１は、サブブロック３Ａ，３Ｃ，３Ｄ及び３Ｆは脱塩室と濃縮室のペアを複数（例えば１７個）え、サブブロック３Ｂ及び３Ｅは脱塩室と濃縮室のペアを１個少なく（例えば１６個）備えている。なお、図９中の「－」は陰極室８を示し、「＋」は正極室９を示し、符号１０は電源ボックスを示す。 In the electrodeionization device 1 shown in Figure 9, sub-blocks 3A, 3C, 3D, and 3F have multiple pairs of dilution compartments and concentration compartments (e.g., 17), while sub-blocks 3B and 3E have one fewer pair of dilution compartments and concentration compartments (e.g., 16). Note that in Figure 9, "-" indicates the cathode compartment 8, "+" indicates the cathode compartment 9, and symbol 10 indicates the power supply box.
特許文献２及び特許文献３に記載された電気脱イオン装置により、図８に示すような電気脱イオン装置における処理水水質の低下を抑制することができた。 The electrodeionization devices described in Patent Documents 2 and 3 were able to suppress the deterioration of treated water quality in electrodeionization devices, as shown in Figure 8.
この特許文献２、３の電気脱イオン装置では、濃縮排水Ｗ４による水の消費量を最小限に抑制するために、濃縮水供給ライン６の基端側に定流量弁を設けて、濃縮水供給ライン６への供給量を制限している。そして、濃縮排水流出ライン７は図示左右に二分割されていて、濃縮排水流出ポート７Ａ，７Ｂ側から濃縮排水Ｗ４が排出される構造、すなわち、濃縮室も濃縮排水流出ポート７Ａ側から排出されるものと、濃縮排水流出ポート７Ｂ側から排出されるものとに分流されることになる。しかしながら、本発明者らの検討の結果、濃縮室に充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、濃縮排水流出ポート７Ａ，７Ｂで流量が異なることがあり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなることがわかった。 In the electrodeionization apparatuses of Patent Documents 2 and 3, a constant flow valve is provided at the base end of the concentrated water supply line 6 to limit the amount of water supplied to the concentrated water supply line 6 in order to minimize water consumption by the concentrated wastewater W4. The concentrated wastewater outlet line 7 is divided into two parts, left and right, as shown in the figure, and the concentrated wastewater W4 is discharged from the concentrated wastewater outlet ports 7A and 7B. In other words, the concentration chambers are also divided into two, one discharged from the concentrated wastewater outlet port 7A and the other discharged from the concentrated wastewater outlet port 7B. However, the inventors' investigations revealed that factors such as slight differences in the filling rate of the ion exchange resin in the concentration chambers can cause differences in flow rate between the concentrated wastewater outlet ports 7A and 7B. This results in a lower flow rate of concentrated water in the concentration chambers connected to the port with the lower flow rate, making scale more likely to form.
本発明は、上記課題に鑑みてなされたものであり、高水質の処理水を効率よく製造することの可能な電気脱イオン装置及びその運転方法を提供することを目的とする。 The present invention was made in consideration of the above-mentioned problems, and aims to provide an electrodeionization apparatus and an operating method thereof that can efficiently produce high-quality treated water.
上記目的を達成するために本発明は第一に、陰極及び陽極と、該陰極及び陽極の間に配置された複数のカチオン交換膜及びアニオン交換膜と、これらカチオン交換膜及びアニオン交換膜により区画形成された複数の脱塩室及び濃縮室とを備え、前記脱塩室及び前記濃縮室にイオン交換樹脂が充填されていて、前記複数の脱塩室に被処理水を通水して脱イオン水を取り出す手段と前記濃縮室に濃縮水を通水する濃縮水通水手段とを有する電気脱イオン装置であって、前記各脱塩室の一側には、被処理水の供給ラインから順次分岐した被処理水流入分岐管がそれぞれ連通しているとともに、前記各脱塩室の他側には処理水の流出管がそれぞれ連通していて、これら各処理水の流出管が処理水の流出ラインに合流しており、前記被処理水の供給ラインの両側から前記被処理水が供給可能となっており、前記各濃縮室の他側には、濃縮水の供給ラインから順次分岐した濃縮水流入分岐管がそれぞれ連通しており、前記各濃縮室の一側には濃縮排水の流出管がそれぞれ連通していて、これら各濃縮排水の流出管が濃縮排水の流出ラインに合流しており、前記濃縮水の供給ラインの両側から前記濃縮水が供給可能となっているとともに、前記濃縮排水の流出ラインの両側から前記濃縮水が両側から排出可能となっていて、前記濃縮排水の流出ラインの両側から排出する流量を制御する流量制御手段を有する、電気脱イオン装置を提供する（発明１）。 To achieve the above-mentioned object, the present invention provides, first, an electrodeionization apparatus comprising a cathode and an anode, a plurality of cation exchange membranes and anion exchange membranes arranged between the cathode and anode, and a plurality of deionization compartments and concentration compartments partitioned by these cation exchange membranes and anion exchange membranes, the deionization compartments and the concentration compartments filled with ion exchange resin, a means for passing water to be treated through the plurality of deionization compartments to extract deionized water, and a concentrated water passing means for passing concentrated water through the concentration compartments, wherein one side of each deionization compartment is connected to a water inlet branch pipe branched in sequence from a water supply line, and the other side of each deionization compartment is connected to a treated water outlet pipe, and each of these treated water The outlet pipes of the concentrate chambers merge into a treated water outlet line, allowing the water to be supplied from both sides of the water supply line; the other side of each concentrate chamber is connected to a concentrated water inlet branch pipe that branches off in sequence from the concentrated water supply line; one side of each concentrate chamber is connected to a concentrated wastewater outlet pipe, and these concentrated wastewater outlet pipes merge into the concentrated wastewater outlet line, allowing the concentrated water to be supplied from both sides of the concentrated water supply line and discharged from both sides of the concentrated wastewater outlet line; and a flow control means is provided for controlling the flow rate discharged from both sides of the concentrated wastewater outlet line (Invention 1).
かかる発明（発明１）によれば、濃縮排水の流出ラインの流量を、流量制御手段により同流量となるように制御することで、各濃縮室の濃縮水の流量が均等化するため、濃縮水の供給ラインの両側から供給する濃縮水を最適化すれば濃縮室でのスケールの発生を抑制することができる。 According to this invention (Invention 1), the flow rate of the concentrated wastewater outflow line is controlled to be the same using a flow control means, thereby equalizing the flow rate of concentrated water in each concentration compartment. Therefore, by optimizing the concentrated water supplied from both sides of the concentrated water supply line, it is possible to suppress the formation of scale in the concentration compartment.
上記発明（発明１）においては、前記電気脱イオン装置の処理水流量が５～５０ｍ３／ｈであることが好ましい（発明２）。 In the above invention (Invention 1), it is preferable that the flow rate of treated water from the electrodeionization device is 5 to 50 m 3 /h (Invention 2).
かかる発明（発明２）によれば、濃縮水の水量を減少させても、濃縮室でのスケールの発生を抑制することができるので、被処理水に占める濃縮水の割合が大きくなりやすい脱塩室での処理水量が５０ｍ３／ｈ以下、特に２５ｍ３／ｈ以下の比較的処理水量の少ない電気脱イオン装置に好適に適用することができる。 According to this invention (Invention 2), even if the amount of concentrated water is reduced, the formation of scale in the concentration compartment can be suppressed, and therefore the invention can be suitably applied to an electrodeionization apparatus with a relatively small amount of treated water in the deionization compartment of 50 m 3 /h or less, particularly 25 m 3 /h or less, where the proportion of concentrated water in the treated water tends to be large.
また、本発明は第二に、陰極及び陽極と、該陰極及び陽極の間に配置された複数のカチオン交換膜及びアニオン交換膜と、これらカチオン交換膜及びアニオン交換膜により区画形成された複数の脱塩室及び濃縮室とを備え、前記脱塩室及び前記濃縮室にイオン交換樹脂が充填されていて、前記複数の脱塩室に被処理水を通水して脱イオン水を取り出す手段と前記濃縮室に濃縮水を通水する濃縮水通水手段とを有し、前記各脱塩室の一側には、被処理水の供給ラインから順次分岐した被処理水流入分岐管がそれぞれ連通しているとともに、前記各脱塩室の他側には処理水の流出管がそれぞれ連通していて、これら各処理水の流出管が処理水の流出ラインに合流しており、前記被処理水の供給ラインの両側から前記被処理水が供給可能となっており、前記各濃縮室の他側には、濃縮水の供給ラインから順次分岐した濃縮水流入分岐管がそれぞれ連通しており、前記各濃縮室の一側には濃縮排水の流出管がそれぞれ連通していて、これら各濃縮排水の流出管が濃縮排水の流出ラインに合流しており、前記濃縮水の供給ラインの両側から前記濃縮水が供給可能となっているとともに、前記濃縮排水の流出ラインの両側から前記濃縮水が両側から排出可能となっていて、前記濃縮排水の流出ラインの流量を制御する流量制御手段を有する、電気脱イオン装置の運転方法であって、前記供給ラインの両側から前記被処理水を供給して前記流出ラインから処理水を取り出し、前記濃縮水の供給ラインの両側から濃縮水を供給して、前記濃縮排水の流出ラインの両側から濃縮排水を排出するに際し、これら濃縮排水の流出ラインの両側の流量が同量となるように前記流量制御手段により制御する、電気脱イオン装置の運転方法を提供する（発明３）。 Secondly, the present invention provides a water treatment system comprising a cathode and an anode, a plurality of cation exchange membranes and anion exchange membranes arranged between the cathode and anode, and a plurality of deionization compartments and concentration compartments partitioned by these cation exchange membranes and anion exchange membranes, the deionization compartments and the concentration compartments being filled with ion exchange resin, a means for passing water to be treated through the plurality of deionization compartments to extract deionized water, and a concentrated water passing means for passing concentrated water through the concentration compartments, one side of each deionization compartment is connected to a water inlet branch pipe branched in sequence from a water supply line, and the other side of each deionization compartment is connected to a treated water outlet pipe, and each treated water outlet pipe merges with the treated water outlet line, so that the water to be treated can be supplied from both sides of the water supply line, and the other side of each concentration compartment is connected to a concentrated water inlet branch pipe branched in sequence from a concentrated water supply line. An operating method for an electrodeionization apparatus is provided in which inlet branch pipes are connected to each other, one side of each concentration chamber is connected to a concentrated wastewater outlet pipe, and these concentrated wastewater outlet pipes merge into a concentrated wastewater outlet line, so that the concentrated water can be supplied from both sides of the concentrated water supply line and discharged from both sides of the concentrated wastewater outlet line, and the method has a flow control means for controlling the flow rate of the concentrated wastewater outlet line, in which the water to be treated is supplied from both sides of the supply line and treated water is discharged from the outlet line, concentrated water is supplied from both sides of the concentrated water supply line, and concentrated wastewater is discharged from both sides of the concentrated wastewater outlet line, and the flow rate on both sides of the concentrated wastewater outlet line is controlled by the flow control means to be equal (Invention 3).
かかる発明（発明３）によれば、濃縮排水の流出ラインの流量が同量と同じになるように前記流量制御手段により制御することで、各濃縮室の濃縮水の流量が均等化するため、濃縮水の供給ラインの両側から供給する濃縮水を最適化すれば濃縮室でのスケールの発生を抑制することができる。なお、本明細書中において、濃縮排水の流出ラインの両側の流量が同量とは、完全に一致するだけでなく、±５％程度、特に±１％程度、流量（ｍ３／ｈ）が異なる場合も含む。 According to this invention (Invention 3), by controlling the flow rate of the concentrated wastewater outlet line so that it is the same, the flow rate of concentrated water in each concentration compartment is equalized by the flow rate control means, and therefore, by optimizing the concentrated water supplied from both sides of the concentrated water supply line, it is possible to suppress the formation of scale in the concentration compartment. Note that in this specification, the same flow rate on both sides of the concentrated wastewater outlet line does not only mean a perfect match, but also includes a case where the flow rate ( m3 /h) differs by about ±5%, particularly about ±1%.
上記発明（発明３）においては、前記電気脱イオン装置の処理水流量が５～５０ｍ３／ｈであることが好ましい（発明４）。 In the above invention (Invention 3), it is preferable that the flow rate of treated water from the electrodeionization device is 5 to 50 m 3 /h (Invention 4).
かかる発明（発明４）によれば、濃縮水の水量を減少させても、濃縮室でのスケールの発生を抑制することができるので、被処理水に占める濃縮水の割合が大きくなりやすい脱塩室での処理水量が５０ｍ３／ｈ以下、特に２５ｍ３／ｈ以下の比較的処理水量の少ない電気脱イオン装置の運転を好適に行うことができる。 According to this invention (Invention 4), even if the amount of concentrated water is reduced, the formation of scale in the concentration compartment can be suppressed, and therefore, the electrodeionization apparatus can be suitably operated with a relatively small amount of treated water in the deionization compartment, where the proportion of concentrated water in the treated water tends to be large, of 50 m 3 /h or less, particularly 25 m 3 /h or less.
本発明の電気脱イオン装置は、脱塩室の被処理水の流通方向と、濃縮室への濃縮水の流通方向とを逆方向とし、さらに濃縮水の供給ラインの両側から濃縮水が供給可能となっているとともに、濃縮排水の流出ラインが各濃縮室を二分割するように両方向に開放していて、この流出ラインの両側から前記濃縮水が両側から排出可能となっていて、この濃縮排水の流出ラインの流量を制御する流量制御手段を有するので、濃縮排水の流出ラインの流量を、流量制御手段により同流量となるように制御することで、各濃縮室の濃縮水の流量が均等化するため、濃縮水の供給ラインの両側から供給する濃縮水を最適化すれば濃縮室でのスケールの発生を抑制することができる。 In the electrodeionization apparatus of the present invention, the flow direction of the water to be treated in the deionization compartments is opposite to the flow direction of the concentrated water to the concentration compartments. Furthermore, concentrated water can be supplied from both sides of the concentrated water supply line. The concentrated wastewater outlet line is open in both directions, dividing each concentration compartment in half, allowing the concentrated water to be discharged from both sides of this outlet line. A flow control means is provided to control the flow rate of the concentrated wastewater outlet line. Therefore, by controlling the flow rate of the concentrated wastewater outlet line to be the same using the flow control means, the flow rate of concentrated water in each concentration compartment is equalized. Therefore, by optimizing the concentrated water supplied from both sides of the concentrated water supply line, it is possible to suppress the formation of scale in the concentration compartments.
以下、本発明の電気脱イオン装置及びこれを用いたその運転方法について添付図面を参照して説明する。 The electrodeionization apparatus of the present invention and its operating method will be described below with reference to the accompanying drawings.
第一の実施形態
［電気脱イオン装置］
図１は、本発明の第一の実施形態による電気脱イオン装置を示している。図１において、電気脱イオン装置１は、フレーム２，２間にサブブロック３Ａ～３Ｆを並設してなる。各サブブロック３Ａ～３Ｆは、交互に配置されたカチオン交換膜ＣＥＭとアニオン交換膜ＡＥＭとによって、脱塩室（図示せず）と濃縮室（図示せず）のペアが複数個形成されたものである。これら脱塩室及び濃縮室にはイオン交換樹脂（例えば、アニオン交換樹脂とカチオン交換樹脂との混合樹脂）が充填されている。
First embodiment [electrodeionization device]
FIG. 1 shows an electrodeionization apparatus according to a first embodiment of the present invention. In FIG. 1, the electrodeionization apparatus 1 comprises sub-blocks 3A to 3F arranged side by side between frames 2, 2. Each sub-block 3A to 3F is formed with multiple pairs of deionization compartments (not shown) and concentration compartments (not shown) formed by alternatingly arranged cation exchange membranes CEM and anion exchange membranes AEM. These deionization compartments and concentration compartments are filled with ion exchange resin (e.g., a mixed resin of anion exchange resin and cation exchange resin).
これらサブブロック３Ａ～３Ｆが連設したセルの一側（図示上側）の両端部には、脱塩室に被処理水Ｗ１を通水するための給水ライン４を配設する給水ポート４Ａ，４Ｂが図示左右両側に形成されている一方、セルの他側（図示下側）の両端部には、脱塩室で処理した脱イオン水としての処理水Ｗ２を排出するための処理水流出ライン５を配設する処理水流出ポート５Ａ，５Ｂが左右側に形成されている。給水ライン４は、それぞれサブブロック３Ａ～３Ｆにおいて分岐していて、被処理水流入分岐管として各脱塩室の上側に接続しているとともに、各脱塩室の下側には、処理水流出管が連通していて、これら各処理水流出管が処理水流出ライン５に合流している。これにより、被処理水Ｗ１を左右の給水ポート４Ａ，４Ｂ側（両側）から給水ライン４を経て各脱塩室の上側から供給し、さらに各脱塩室の下側から処理水流出ライン５を経て左右の処理水流出ポート５Ａ，５Ｂ側から処理水Ｗ２を排出可能となっている。 At both ends of one side (the upper side in the figure) of the cell in which these sub-blocks 3A to 3F are connected, water supply ports 4A and 4B are formed on both the left and right sides in the figure, through which water supply lines 4 are installed to pass water to be treated W1 through the deionization chambers, while at both ends of the other side (the lower side in the figure) of the cell, treated water outlet ports 5A and 5B are formed on both the left and right sides, through which treated water outlet lines 5 are installed to discharge treated water W2 as deionized water treated in the deionization chambers. The water supply lines 4 branch off in each of the sub-blocks 3A to 3F, connecting to the upper side of each deionization chamber as treated water inlet branch pipes, and treated water outlet pipes are connected to the lower side of each deionization chamber, and these treated water outlet pipes merge into the treated water outlet line 5. This allows treated water W1 to be supplied from the top of each deionization chamber via water supply line 4 from the left and right water supply ports 4A, 4B (both sides), and treated water W2 can be discharged from the bottom of each deionization chamber via treated water outlet line 5 through the left and right treated water outlet ports 5A, 5B.
また、サブブロック３Ａ～３Ｆが連設したセルの図示下側の両端部には、濃縮室に濃縮水Ｗ３を通水するための濃縮水供給ライン６を配設する濃縮水給水ポート６Ａ，６Ｂが左右両側に形成されている一方、セルの図示上側の両端部には、濃縮排水Ｗ４を排出するための濃縮排水流出ライン７を配設する濃縮排水流出ポート７Ａ，７Ｂが左右両側に形成されている。濃縮排水流出ライン７は、濃縮室を二分割するように、左右一対となっている。濃縮水供給ライン６は、それぞれサブブロック３Ａ～３Ｆにおいて分岐して濃縮水流入分岐管として各濃縮室の下側に接続しているとともに、各濃縮室の上側には濃縮排水流出管が連通していて、これら各濃縮排水流出管が濃縮排水流出ライン７に合流している。これにより、濃縮水Ｗ３を濃縮水給水ポート６Ａ，６Ｂ側から濃縮水供給ライン６を経て各濃縮室の下側から供給し、さらに各濃縮室の上側から濃縮排水Ｗ４を濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出可能となっている。そして、本実施形態においては、濃縮水供給ライン６の左右両側には定流量弁１１Ａ，１１Ｂがそれぞれ設けられているとともに、濃縮排水流出ライン７の左右両側には、流量制御手段としての手動弁１２Ａ，１２Ｂがそれぞれ設けられている。 Furthermore, concentrated water supply ports 6A, 6B are formed on both left and right sides at both ends of the lower side of the cell in which sub-blocks 3A to 3F are connected, and these provide concentrated water supply lines 6 for passing concentrated water W3 through the concentration chambers. Concentrated wastewater outlet ports 7A, 7B are formed on both left and right sides at both ends of the upper side of the cell, and provide concentrated wastewater outlet lines 7 for discharging concentrated wastewater W4. The concentrated wastewater outlet lines 7 are provided in pairs, one on the left and one on the right, dividing the concentration chambers into two. The concentrated water supply lines 6 branch off in each of the sub-blocks 3A to 3F, connecting to the lower side of each concentration chamber as concentrated water inlet branch pipes. Concentrated wastewater outlet pipes are connected to the upper side of each concentration chamber, and these concentrated wastewater outlet pipes merge into the concentrated wastewater outlet line 7. This allows concentrated water W3 to be supplied from the bottom of each concentration compartment via concentrated water supply line 6 from concentrated water supply ports 6A, 6B, and concentrated wastewater W4 can be discharged from the top of each concentration compartment via concentrated wastewater outlet line 7 through concentrated wastewater outlet ports 7A, 7B. In this embodiment, constant flow valves 11A, 11B are provided on both the left and right sides of concentrated water supply line 6, and manual valves 12A, 12B are provided on both the left and right sides of concentrated wastewater outlet line 7 as flow control means.
図１に示す電気脱イオン装置１は、サブブロック３Ａ，３Ｃ，３Ｄ及び３Ｆは脱塩室と濃縮室のペアを複数（例えば１７個）え、サブブロック３Ｂ及び３Ｅは脱塩室と濃縮室のペアを１個少なく（例えば１６個）備えている。なお、図１中の「－」は負極室８を示し、「＋」は正極室９を示し、符号１０は電源ボックスを示す。 In the electrodeionization device 1 shown in Figure 1, sub-blocks 3A, 3C, 3D, and 3F have multiple pairs of dilution compartments and concentration compartments (e.g., 17), while sub-blocks 3B and 3E have one fewer pair of dilution compartments and concentration compartments (e.g., 16). Note that in Figure 1, "-" indicates the anode compartment 8, "+" indicates the cathode compartment 9, and symbol 10 indicates the power supply box.
［電気脱イオン装置の運転方法］
次に上述したような構成を有する電気脱イオン装置１の運転方法について説明する。
[Method of operating an electrodeionization apparatus]
Next, a method of operating the electrodeionization apparatus 1 having the above-described configuration will be described.
まず、給水ポートの４Ａ，４Ｂ側から給水ライン４を経てサブブロック３Ａ～３Ｆの脱塩室に上側から被処理水Ｗ１を供給するとともに、濃縮水Ｗ３を濃縮水給水ポート６Ａ，６Ｂ側から濃縮水供給ライン６を経て各濃縮室に下側から供給する。被処理水Ｗ１は、各サブブロック３Ａ～３Ｆの脱塩室を図示上側から下側に通過して、各処理水流出管から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から排出される。また、濃縮水Ｗ３は、濃縮水供給ライン６の左右両側から供給され、各サブブロック３Ａ～３Ｆの濃縮室を図示下側から上側に通過して、各濃縮排水流出管から濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出される。このとき、各濃縮室では充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、各濃縮室における濃縮水Ｗ３の通水抵抗が異なり、濃縮排水流出ポート７Ａ側と７Ｂ側とで濃縮水Ｗ３の流量が異なり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなる。そこで、本実施形態においては、濃縮水供給ライン６の左右両側から濃縮水給水ポート６Ａ，６Ｂ側から供給する濃縮水Ｗ３の流量を定流量弁１１Ａ，１１Ｂによりそれぞれ同量とする。さらに、濃縮排水流出ポート７Ａ側と７Ｂ側から排出する濃縮水Ｗ３の流量が同じになるように手動弁１２Ａ，１２Ｂを調整する。これにより、各濃縮室を流通する濃縮水の水量の均一化を図ることができ、各濃縮室におけるスケールの発生の傾向を同一化することができ、ひいては各濃縮室におけるスケールの発生を抑制することができる。 First, water to be treated W1 is supplied from above to the desalination chambers of sub-blocks 3A-3F via water supply line 4 from water supply ports 4A and 4B, and concentrated water W3 is supplied from below to each concentration chamber via concentrated water supply lines 6 from concentrated water supply ports 6A and 6B. The water to be treated W1 passes through the desalination chambers of each sub-block 3A-3F from top to bottom in the figure, passes through each treated water outlet pipe, passes through treated water outlet line 5, and is discharged from treated water outlet ports 5A and 5B. Concentrated water W3 is supplied from both the left and right sides of concentrated water supply line 6, passes through the concentration chambers of each sub-block 3A-3F from bottom to top in the figure, passes through each concentrated wastewater outlet pipe, passes through concentrated wastewater outlet line 7, and is discharged from concentrated wastewater outlet ports 7A and 7B. Due to factors such as slight differences in the filling rate of the ion exchange resin in each concentration compartment, the flow resistance of concentrated water W3 in each concentration compartment varies, resulting in different flow rates of concentrated water W3 between concentrated wastewater outlet ports 7A and 7B. The flow rate of concentrated water W3 in the concentration compartment with the lower flow rate port is lower, making it more susceptible to scale formation. Therefore, in this embodiment, the flow rates of concentrated water W3 supplied from concentrated water supply ports 6A and 6B on both sides of the concentrated water supply line 6 are set equal by constant flow valves 11A and 11B. Furthermore, manual valves 12A and 12B are adjusted so that the flow rates of concentrated water W3 discharged from concentrated wastewater outlet ports 7A and 7B are equal. This allows for uniform flow of concentrated water through each concentration compartment, uniforming the tendency for scale formation in each concentration compartment and ultimately suppressing scale formation in each concentration compartment.
上述したような本実施形態の電気脱イオン装置１の運転方法において、濃縮水Ｗ３としては、処理水Ｗ２を分取して用いても良いし、ＲＯ膜の処理水などの被処理水Ｗ１と同じものを用いてもよい。また、サブブロック３Ａ～３Ｆによる処理水Ｗ２の流量（脱塩室流量）は、５～５０ｍ３／ｈ、特に５～２５ｍ３／ｈ、さらに５～１５ｍ３／ｈであることが好ましい。処理水Ｗ２の流量（脱塩室流量）が５ｍ３／ｈ未満では、処理水量が少なすぎ実用的でない一方、５０ｍ３／ｈを超えると、本実施形態のようにコンパクトな構成とするのが困難となる。さらに、処理水Ｗ２の流量に対する濃縮排水Ｗ４の流量は２．５～１０容積％、特に５容積％程度が望ましい。濃縮排水Ｗ４の流量は２．５容積％未満では、濃縮排水Ｗ４が少なすぎるため、脱塩室から流入したイオン濃度が高くなり、逆拡散が無視できず処理水Ｗ２の水質の低下をきたしやすくなる一方、１０容積％を超えると濃縮水Ｗ３の給水量が多くなりすぎるため水の利用効率の点で好ましくない。 In the operating method of the electrodeionization apparatus 1 of this embodiment as described above, the concentrated water W3 may be a portion of the treated water W2, or the same water as the water to be treated W1, such as water treated by an RO membrane, may be used. Furthermore, the flow rate of the treated water W2 (demineralization compartment flow rate) through the sub-blocks 3A to 3F is preferably 5 to 50 m 3 /h, particularly 5 to 25 m 3 /h, and even more preferably 5 to 15 m 3 /h. If the flow rate of the treated water W2 (demineralization compartment flow rate) is less than 5 m 3 /h, the amount of treated water is too small to be practical, while if it exceeds 50 m 3 /h, it becomes difficult to achieve a compact configuration as in this embodiment. Furthermore, the flow rate of the concentrated wastewater W4 relative to the flow rate of the treated water W2 is preferably 2.5 to 10 vol%, particularly about 5 vol%. If the flow rate of concentrated wastewater W4 is less than 2.5% by volume, the amount of concentrated wastewater W4 is too small, resulting in a high concentration of ions flowing in from the desalination chamber, and back diffusion cannot be ignored, making it likely that the quality of the treated water W2 will deteriorate.On the other hand, if the flow rate exceeds 10% by volume, the amount of concentrated water W3 supplied will be too large, which is not desirable in terms of water utilization efficiency.
また、脱塩室の通水ＳＶは７０～１５０／ｈ、特に１００～１２０／ｈが好ましい。濃縮室の通水ＳＶは５～５０／ｈ、特に１０～２５／ｈが好ましい。回収率は８０～９９％、特に９０～９５％が好ましい。通電する電流は０．１５～２．３０Ａ／（ｍ３／ｈ）、特に０．７Ａ／（ｍ３／ｈ）～１．２Ａ／（ｍ３／ｈ）が好ましい。 The water flow rate SV of the deionization compartment is preferably 70 to 150/h, and more preferably 100 to 120/h. The water flow rate SV of the concentration compartment is preferably 5 to 50/h, and more preferably 10 to 25/h. The recovery rate is preferably 80 to 99%, and more preferably 90 to 95%. The current applied is preferably 0.15 to 2.30 A/(m 3 /h), and more preferably 0.7 A/(m 3 /h) to 1.2 A/(m 3 /h).
本実施形態においては、すべての脱塩室に被処理水Ｗ１を図示下降流にて通水する一方、すべての濃縮室に濃縮水Ｗ３を図示上向流にて通水する。 In this embodiment, the water to be treated W1 flows downward through all deionization compartments, while the concentrated water W3 flows upward through all concentration compartments.
この被処理水Ｗ１（給水）の導電率は、０．１～１ｍＳ／ｍ、特に０．１～０，５ｍＳ／ｍが好ましい。被処理水Ｗ１（給水）の導電率が１ｍＳ／ｍを超えると、濃縮室から脱塩室への逆拡散が生じやすくなり、処理水Ｗ２の水質の低下をきたしやすいため好ましくない。 The conductivity of this water to be treated W1 (feedwater) is preferably 0.1 to 1 mS/m, and particularly 0.1 to 0.5 mS/m. If the conductivity of the water to be treated W1 (feedwater) exceeds 1 mS/m, back diffusion from the concentration compartment to the deionization compartment is likely to occur, which is undesirable as it can easily lead to a deterioration in the quality of the treated water W2.
さらに、被処理水Ｗ１（給水）の無機炭酸濃度が５０～１０００μｇ／Ｌ ａｓ Ｃであることが好ましい。被処理水Ｗ１（給水）の無機炭酸濃度が１０００μｇ／Ｌ ａｓ Ｃを超えると、炭酸濃度が高すぎて、濃縮室から脱塩室への逆拡散が生じやすくなり、処理水Ｗ２の水質の低下をきたしやすいだけでなく、炭酸カルシウムなどの炭酸塩が電極などに析出しやすくなる。 Furthermore, it is preferable that the inorganic carbonate concentration of the water to be treated W1 (feed water) be 50 to 1000 μg/L as C. If the inorganic carbonate concentration of the water to be treated W1 (feed water) exceeds 1000 μg/L as C, the carbonate concentration will be too high, making it more likely that back diffusion will occur from the concentration compartment to the deionization compartment, which will not only likely lead to a deterioration in the quality of the treated water W2, but will also make it more likely that carbonates such as calcium carbonate will precipitate on electrodes, etc.
上述したような被処理水Ｗ１（給水）としては、工水、市水、井水などに必要に応じて前処理を施した後、逆浸透膜装置を含む水処理装置で処理したものを好適に用いることができる。この逆浸透膜装置の処理水の導電率、ホウ素濃度及び無機炭酸濃度を適宜センシングして上述した範囲内にあることを確認して用いることが好ましい。 The water to be treated W1 (supply water) described above can be industrial water, city water, well water, etc., which has been pretreated as necessary and then treated in a water treatment device including a reverse osmosis membrane device. It is preferable to appropriately sense the conductivity, boron concentration, and inorganic carbonate concentration of the treated water from this reverse osmosis membrane device to confirm that they are within the above-mentioned ranges before use.
第二の実施形態
［電気脱イオン装置］
図２は、本発明の第二の実施形態による電気脱イオン装置を示している。図２に示す電気脱イオン装置１は、基本的には前述した第一の実施形態と同じ構成を有し、同じ条件で運転可能であるので、同一の構成には同一の符号を付し、その詳細な説明を省略する。
Second embodiment [electrodeionization device]
Fig. 2 shows an electrodeionization apparatus according to a second embodiment of the present invention. The electrodeionization apparatus 1 shown in Fig. 2 has basically the same configuration as the first embodiment described above and can be operated under the same conditions. Therefore, the same components are denoted by the same reference numerals and detailed descriptions thereof are omitted.
図２において、電気脱イオン装置１は、濃縮水Ｗ３が図示左右に分岐した濃縮水供給ライン６１を経由して濃縮水給水ポート６Ａ，６Ｂ側から供給される構造となっている。この濃縮水供給ライン６１の分岐する手前に１個の定流量弁１１Ｃが設けられていて、濃縮水供給ライン６には定流量弁１１Ａ，１１Ｂを有しない以外は、前述した第一の実施形態と同じ構成を有する。 In Figure 2, the electrodeionization apparatus 1 is configured so that concentrated water W3 is supplied from concentrated water supply ports 6A and 6B via a concentrated water supply line 61 that branches to the left and right as shown. A single constant flow valve 11C is provided just before the branching of this concentrated water supply line 61, and the concentrated water supply line 6 does not have constant flow valves 11A and 11B. Other than this, the configuration is the same as the first embodiment described above.
［電気脱イオン装置の運転方法］
次に上述したような構成を有する電気脱イオン装置１の運転方法について説明する。
[Method of operating an electrodeionization apparatus]
Next, a method of operating the electrodeionization apparatus 1 having the above-described configuration will be described.
まず、給水ポート４Ａ，４Ｂ側から給水ライン４を経てサブブロック３Ａ～３Ｆの脱塩室に上側から被処理水Ｗ１を供給するとともに、濃縮水供給ライン６１から濃縮水Ｗ３を供給し、濃縮水供給ライン６を経て各濃縮室に下側から供給する。被処理水Ｗ１は、各サブブロック３Ａ～３Ｆの脱塩室を図示上側から下側に通過して、各処理水流出管から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から排出される。また、濃縮水Ｗ３は、濃縮水供給ライン６の左右両側から供給され、各サブブロック３Ａ～３Ｆの濃縮室を図示下側から上側に通過して、各濃縮排水流出管から濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出される。このとき、各濃縮室では充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、各濃縮室における濃縮水Ｗ３の通水抵抗が異なり、濃縮排水流出ポート７Ａ側と７Ｂ側とで流量が異なり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなる。そこで、本実施形態においては、濃縮水供給ライン６１から供給する濃縮水Ｗ３の流量を定流量弁１１Ｃで制御するとともに、濃縮排水流出ポート７Ａ側と７Ｂ側とから排出する濃縮水Ｗ３の流量が同じになるように手動弁１２Ａ，１２Ｂを調整する。これにより、各濃縮室を流通する濃縮水の水量の均一化を図ることができ、各濃縮室におけるスケールの発生の傾向を同一化することができ、ひいては各濃縮室におけるスケールの発生を抑制することができる。 First, water to be treated W1 is supplied from above to the deionization chambers of sub-blocks 3A-3F via water supply line 4 from water supply ports 4A and 4B, and concentrated water W3 is supplied from concentrated water supply line 6 and supplied to each concentration chamber from below. The water to be treated W1 passes through the deionization chambers of each sub-block 3A-3F from top to bottom in the figure, passes through each treated water outlet pipe, passes through treated water outlet line 5, and is discharged from treated water outlet ports 5A and 5B. Concentrated water W3 is supplied from both the left and right sides of concentrated water supply line 6, passes through the concentration chambers of each sub-block 3A-3F from bottom to top in the figure, passes through each concentrated wastewater outlet pipe, passes through concentrated wastewater outlet line 7, and is discharged from concentrated wastewater outlet ports 7A and 7B. At this time, factors such as slight differences in the filling rate of the ion exchange resin in each concentration compartment result in different resistances to the flow of concentrated water W3 in each concentration compartment, resulting in different flow rates between concentrated wastewater outlet ports 7A and 7B. The flow rate of concentrated water is lower in the concentration compartment with the lower flow rate, making it more susceptible to scale formation. Therefore, in this embodiment, the flow rate of concentrated water W3 supplied from concentrated water supply line 61 is controlled by constant flow valve 11C, and manual valves 12A and 12B are adjusted so that the flow rates of concentrated water W3 discharged from concentrated wastewater outlet ports 7A and 7B are the same. This allows the amount of concentrated water flowing through each concentration compartment to be uniform, which in turn allows the scale formation tendency in each concentration compartment to be uniform and ultimately suppresses scale formation in each concentration compartment.
第三の実施形態
［電気脱イオン装置］
図３は、本発明の第三の実施形態による電気脱イオン装置を示している。図３に示す電気脱イオン装置１は、基本的には前述した第一の実施形態と同じ構成を有し、同じ条件で運転可能であるので、同一の構成には同一の符号を付し、その詳細な説明を省略する。
Third embodiment [electrodeionization device]
3 shows an electrodeionization apparatus according to a third embodiment of the present invention. The electrodeionization apparatus 1 shown in FIG. 3 has basically the same configuration as the first embodiment described above and can be operated under the same conditions. Therefore, the same components are denoted by the same reference numerals and detailed descriptions thereof are omitted.
図３において、電気脱イオン装置１は、前述した第一の実施形態において、濃縮水供給ライン６の定流量弁１１Ａ，１１Ｂを有せず、濃縮排水流出ライン７の左右両側には、手動弁１２Ａ，１２Ｂの代わりに流量制御手段としての定流量弁１３Ａ，１３Ｂがそれぞれ設けられている以外、同じ構成を有する。 In Figure 3, the electrodeionization apparatus 1 has the same configuration as the first embodiment described above, except that it does not have constant flow valves 11A and 11B on the concentrated water supply line 6, and constant flow valves 13A and 13B are provided on both the left and right sides of the concentrated wastewater outflow line 7 as flow control means instead of manual valves 12A and 12B.
［電気脱イオン装置の運転方法］
次に上述したような構成を有する電気脱イオン装置１の運転方法について説明する。
[Method of operating an electrodeionization apparatus]
Next, a method of operating the electrodeionization apparatus 1 having the above-described configuration will be described.
まず、給水ポート４Ａ，４Ｂ側から給水ライン４を経てサブブロック３Ａ～３Ｆの脱塩室に上側から被処理水Ｗ１を供給するとともに、濃縮水供給ライン６１から濃縮水Ｗ３を供給し濃縮水供給ライン６を経て各濃縮室に下側から濃縮水Ｗ３を供給する。被処理水Ｗ１は、各サブブロック３Ａ～３Ｆの脱塩室を図示上側から下側に通過して、各処理水流出管から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から排出される。また、濃縮水Ｗ３は、濃縮水供給ライン６の左右両側から各サブブロック３Ａ～３Ｆの濃縮室を図示下側から上側に通過して、各濃縮排水流出管から濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出される。このとき、各濃縮室では充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、各濃縮室における濃縮水Ｗ３の通水抵抗が異なり、濃縮排水流出ポート７Ａ側と７Ｂ側とで流量が異なり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなる。そこで、本実施形態においては、定流量弁１３Ａ，１３Ｂを設けて、濃縮排水流出ポート７Ａ側と７Ｂ側とから排出する濃縮水Ｗ３の流量を一定量とする。この結果、各濃縮室を流通する濃縮水の水量の均一化を図ることができ、各濃縮室におけるスケールの発生の傾向を同一化することができ、ひいては各濃縮室におけるスケールの発生を抑制することができる。 First, water to be treated W1 is supplied from above to the deionization chambers of sub-blocks 3A-3F via water supply line 4 from water supply ports 4A and 4B, and concentrated water W3 is supplied from concentrated water supply line 6 to each concentration chamber from below. The water to be treated W1 passes through the deionization chambers of each sub-block 3A-3F from top to bottom in the figure, passes through each treated water outlet pipe, passes through treated water outlet line 5, and is discharged from treated water outlet ports 5A and 5B. Concentrated water W3 also passes through the concentration chambers of each sub-block 3A-3F from both the left and right sides of concentrated water supply line 6 from bottom to top in the figure, passes through each concentrated wastewater outlet pipe, passes through concentrated wastewater outlet line 7, and is discharged from concentrated wastewater outlet ports 7A and 7B. At this time, factors such as slight differences in the filling rate of the ion exchange resin in each concentration compartment cause differences in the flow resistance of concentrated water W3 in each concentration compartment, resulting in different flow rates between concentrated wastewater outlet ports 7A and 7B. The flow rate of concentrated water is lower in the concentration compartment with the lower flow rate, making it more susceptible to scale formation. Therefore, in this embodiment, constant flow valves 13A and 13B are provided to maintain a constant flow rate of concentrated water W3 discharged from concentrated wastewater outlet ports 7A and 7B. This results in uniform amounts of concentrated water flowing through each concentration compartment, which in turn unifies the tendency for scale formation in each concentration compartment and ultimately suppresses scale formation in each concentration compartment.
第四の実施形態
［電気脱イオン装置］
図４は、本発明の第四の実施形態による電気脱イオン装置を示している。本実施形態の電気脱イオン装置は、基本的には前述した第二の実施形態と同じ構成を有するので、同一の構成には同一の符号を付し、詳細な説明を省略する。図４において、電気脱イオン装置１は、フレーム２，２間にサブブロック３Ａ～３Ｇを並設してなる。各サブブロック３Ａ～３Ｇは、交互に配置されたカチオン交換膜ＣＥＭとアニオン交換膜ＡＥＭとによって、脱塩室（図示せず）と濃縮室（図示せず）のペアが複数個形成されたものである。これら脱塩室及び濃縮室にはイオン交換樹脂（例えば、アニオン交換樹脂とカチオン交換樹脂との混合樹脂）が充填されている。
Fourth embodiment [electrodeionization device]
FIG. 4 shows an electrodeionization apparatus according to a fourth embodiment of the present invention. Since the electrodeionization apparatus of this embodiment has essentially the same configuration as the second embodiment, the same components are designated by the same reference numerals and detailed descriptions are omitted. In FIG. 4, the electrodeionization apparatus 1 comprises sub-blocks 3A to 3G arranged side by side between frames 2. Each sub-block 3A to 3G is formed by alternatingly arranged cation exchange membranes CEM and anion exchange membranes AEM, forming multiple pairs of deionization compartments (not shown) and concentration compartments (not shown). These deionization compartments and concentration compartments are filled with ion exchange resin (e.g., a mixture of anion exchange resin and cation exchange resin).
これらサブブロック３Ａ～３Ｇが連設したセルの一側（図示上側）の両端部には、脱塩室に被処理水Ｗ１を通水するための給水ライン４を配設する給水ポート４Ａ，４Ｂが形成されている一方、セルの他側（図示下側）の両端部には、脱塩室で処理した脱イオン水としての処理水Ｗ２を排出するための処理水流出ライン５を配設する処理水流出ポート５Ａ，５Ｂが形成されている。給水ライン４は、それぞれサブブロック３Ａ～３Ｇにおいて分岐していて、被処理水流入分岐管として各脱塩室の上側に接続しているとともに、各脱塩室の下側には、処理水流出管が連通していて、これら各処理水流出管が処理水流出ライン５に合流している。これにより、被処理水Ｗ１を給水ポート４Ａ，４Ｂから給水ライン４を経て各脱塩室の上側から供給し、さらに各脱塩室の下側から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂから排出可能となっている。 At both ends of one side (the upper side in the figure) of each cell, which connects these sub-blocks 3A to 3G, are water supply ports 4A and 4B, through which water supply lines 4 are installed to pass water W1 to the deionization chambers. At both ends of the other side (the lower side in the figure), are treated water outlet ports 5A and 5B, through which treated water outlet lines 5 are installed to discharge treated water W2, deionized water, which has been treated in the deionization chambers. The water supply line 4 branches off in each of the sub-blocks 3A to 3G, connecting to the upper side of each deionization chamber as a treated water inlet branch pipe. Treated water outlet pipes are connected to the lower side of each deionization chamber, and these treated water outlet pipes merge into the treated water outlet line 5. This allows water W1 to be supplied from the upper side of each deionization chamber via the water supply ports 4A and 4B and the water supply line 4, and then discharged from the lower side of each deionization chamber via the treated water outlet line 5 and the treated water outlet ports 5A and 5B.
また、サブブロック３Ａ～３Ｇが連設したセルの図示下側の両端部には、濃縮室に濃縮水としての濃縮水Ｗ３を通水するための濃縮水供給ライン６を配設する濃縮水給水ポート６Ａ，６Ｂが形成されている一方、セルの図示上側の両端部には、濃縮排水Ｗ４を排出するための濃縮排水流出ライン７を配設する濃縮排水流出ポート７Ａ，７Ｂが形成されている。濃縮水供給ライン６は、それぞれサブブロック３Ａ～３Ｇにおいて分岐して濃縮水流入分岐管として各濃縮室の下側に接続しているとともに、各濃縮室の上側には濃縮排水流出管が連通していて、これら各濃縮排水流出管が濃縮排水流出ライン７に合流している。これにより、濃縮水Ｗ３を濃縮水給水ポート６Ａ，６Ｂから濃縮水供給ライン６を経て各濃縮室の下側から供給し、さらに各濃縮室の上側から濃縮水Ｗ３を濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂから排出可能となっている。 Furthermore, concentrated water supply ports 6A, 6B are formed at both ends of the lower side of the cell in which sub-blocks 3A-3G are connected, and these provide concentrated water supply lines 6 for passing concentrated water W3 (concentrated water) through the concentrating chambers. Concentrated wastewater outlet ports 7A, 7B are formed at both ends of the upper side of the cell, and these provide concentrated wastewater outlet lines 7 for discharging concentrated wastewater W4. The concentrated water supply line 6 branches off in each of the sub-blocks 3A-3G and connects to the lower side of each concentrating chamber as a concentrated water inlet branch pipe. Concentrated wastewater outlet pipes are connected to the upper side of each concentrating chamber, and these concentrated wastewater outlet pipes merge into the concentrated wastewater outlet line 7. This allows concentrated water W3 to be supplied from the lower side of each concentrating chamber via the concentrated water supply line 6 from the concentrated water supply ports 6A, 6B, and then the concentrated water W3 can be discharged from the upper side of each concentrating chamber via the concentrated wastewater outlet line 7 and the concentrated wastewater outlet ports 7A, 7B.
そして、本実施形態においては、フレーム２，２間の図示左端側には負極室（負極）８が配置されているとともに、右端側には陽極室（陽極）９が設けられており、サブブロック３Ａ～３Ｇの１ブロック構成となっていて、濃縮排水流出ライン７は、その中間部に閉止板１１が設けられることで、濃縮排水流出ライン７の流れが濃縮排水流出ポート７Ａと，７Ｂに分流するように構成されている。なお、符号１０は電源ボックスである。 In this embodiment, an anode chamber (negative electrode) 8 is located on the left end of the frame 2, 2, and an anode chamber (anode) 9 is provided on the right end, forming a single block of sub-blocks 3A to 3G. A closure plate 11 is provided in the middle of the concentrated wastewater outflow line 7, which divides the flow of the concentrated wastewater outflow line 7 into concentrated wastewater outflow ports 7A and 7B. Reference numeral 10 denotes a power supply box.
本実施形態のように左端側に負極８、右端側に陽極９を設けた１ブロック構成とすることにより、第一の実施形態のように中央に一対の陽極室（陽極）９を配置した場合よりも、フレーム２，２間の陽極室および陰極室の数か少なくてすむため、サブブロック３Ａ・・・の数を多くすることができるので、処理水Ｗ２の流量（脱塩室流量）を第一の実施形態よりも多くすることができる。その一方で、負極室（負極）８と陽極室（陽極）９の距離が長くなるので、第一の実施形態よりも高い電圧、特に約２倍以上の電圧を印加する必要があり、電流量も多くなるなど、電力供給条件が異なるが、それ以外の運転方法は、前述した第一の実施形態とほぼ同じでよい。 By using a single block configuration with the negative electrode 8 on the left end and the anode 9 on the right end, as in this embodiment, fewer anode chambers and cathode chambers are required between the frames 2, 2 than when a pair of anode chambers (anodes) 9 are arranged in the center, as in the first embodiment. This allows for a larger number of sub-blocks 3A..., and therefore allows for a higher flow rate of treated water W2 (demineralization chamber flow rate) than in the first embodiment. On the other hand, because the distance between the negative electrode chamber (negative electrode) 8 and the anode chamber (anode) 9 is longer, a higher voltage, particularly approximately twice the voltage, must be applied than in the first embodiment, and the amount of current is also increased. However, the power supply conditions are different, and the operating method is otherwise essentially the same as in the first embodiment described above.
図４において、電気脱イオン装置１は、濃縮水Ｗ３が図示左右に分岐した濃縮水供給ライン６１を経由して濃縮水給水ポート６Ａ，６Ｂ側から供給される構造となっている。この濃縮水供給ライン６１の分岐する手前に１個の定流量弁１１Ｃが設けられている。 In Figure 4, the electrodeionization device 1 is configured so that concentrated water W3 is supplied from the concentrated water supply ports 6A and 6B via a concentrated water supply line 61 that branches to the left and right as shown. A single constant flow valve 11C is provided just before the branching of this concentrated water supply line 61.
［電気脱イオン装置の運転方法］
次に上述したような構成を有する電気脱イオン装置の運転方法について説明する。
[Method of operating an electrodeionization apparatus]
Next, a method for operating the electrodeionization apparatus having the above-described configuration will be described.
まず、給水ポート４Ａ，４Ｂ側から給水ライン４を経てサブブロック３Ａ～３Ｇの脱塩室に上側から被処理水Ｗ１を供給するとともに、濃縮水供給ライン６１から濃縮水Ｗ３を供給し、濃縮水供給ライン６を経て各濃縮室に下側から供給する。被処理水Ｗ１は、各サブブロック３Ａ～３Ｇの脱塩室を図示上側から下側に通過して、各処理水流出管から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から排出される。また、濃縮水Ｗ３は、濃縮水供給ライン６の左右両側から供給され、各サブブロック３Ａ～３Ｆの濃縮室を図示下側から上側に通過して、各濃縮排水流出管から濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出される。このとき、各濃縮室では充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、各濃縮室における濃縮水Ｗ３の通水抵抗が異なり、濃縮排水流出ポート７Ａ側と７Ｂ側とで流量が異なり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなる。そこで、本実施形態においては、濃縮水供給ライン６１から供給する濃縮水Ｗ３の流量を定流量弁１１Ｃで制御するとともに、濃縮排水流出ポート７Ａ側と７Ｂ側とから排出する濃縮水Ｗ３の流量がサブブロック３Ａ～３Ｇの数に応じた流量比となるように両側の手動弁１２Ａ，１２Ｂを調整する。これにより、各濃縮室を流通する濃縮水の水量の均一化を図ることができ、各濃縮室におけるスケールの発生の傾向を同一化することができ、ひいては各濃縮室におけるスケールの発生を抑制することができる。 First, water to be treated W1 is supplied from above to the deionization chambers of sub-blocks 3A-3G via water supply line 4 from water supply ports 4A and 4B, and concentrated water W3 is supplied from concentrated water supply line 6 to each concentration chamber from below. The water to be treated W1 passes through the deionization chambers of each sub-block 3A-3G from top to bottom in the figure, passes through each treated water outlet pipe, passes through treated water outlet line 5, and is discharged from treated water outlet ports 5A and 5B. Concentrated water W3 is supplied from both the left and right sides of concentrated water supply line 6, passes through the concentration chambers of each sub-block 3A-3F from bottom to top in the figure, passes through each concentrated wastewater outlet pipe, passes through concentrated wastewater outlet line 7, and is discharged from concentrated wastewater outlet ports 7A and 7B. At this time, factors such as slight differences in the filling rate of the ion exchange resin in each concentration compartment result in different resistances to the flow of concentrated water W3 in each concentration compartment, resulting in different flow rates between concentrated wastewater outlet ports 7A and 7B. The concentration compartments with lower flow rates experience lower concentrated water flow rates, making them more susceptible to scale formation. Therefore, in this embodiment, the flow rate of concentrated water W3 supplied from the concentrated water supply line 61 is controlled by constant flow valve 11C, and the manual valves 12A and 12B on both sides are adjusted so that the flow rates of concentrated water W3 discharged from concentrated wastewater outlet ports 7A and 7B correspond to the number of sub-blocks 3A-3G. This allows for uniform flow of concentrated water through each concentration compartment, equating the tendency for scale formation in each concentration compartment and ultimately suppressing scale formation in each concentration compartment.
上述したような本実施形態の電気脱イオン装置１においては、濃縮水Ｗ３としては、処理水Ｗ２を分取して用いても良いし、ＲＯ膜の処理水などの被処理水Ｗ１と同じものを用いてもよい。また、サブブロック３Ａ～３Ｇによる処理水Ｗ２の流量（脱塩室流量）は、５～５０ｍ３／ｈ、特に５～２５ｍ３／ｈ、さらに５～１５ｍ３／ｈであることが好ましい。処理水Ｗ２の流量（脱塩室流量）が５ｍ３／ｈ未満では、処理水量が少なすぎ実用的でない一方、５０ｍ３／ｈ、特に２５ｍ３／ｈを超えると、処理水Ｗ２の流量が多くなり処理水Ｗ２を濃縮水Ｗ３として利用する場合と比べてメリットが十分に得られない。さらに、給水流量（処理水Ｗ２の流量＋濃縮排水Ｗ４の流量）に対する濃縮排水Ｗ４の流量は２．５～１０容積％、特に５容積％程度が望ましい。濃縮排水Ｗ４の流量は２．５容積％未満では、濃縮排水Ｗ４が少なすぎるため、脱塩室から流入するイオン濃度が高くなり、逆拡散が無視できず処理水Ｗ２の水質の低下をきたしやすくなる一方、１０容積％を超えると濃縮水Ｗ３が多くなり、被処理水Ｗ１を濃縮水Ｗ３とすることにより給水の量が多くなりすぎるため好ましくない。 In the electrodeionization apparatus 1 of this embodiment described above, the concentrated water W3 may be a fraction of the treated water W2, or the same water as the water to be treated W1, such as water treated by an RO membrane, may be used. Furthermore, the flow rate of the treated water W2 (demineralization chamber flow rate) through the sub-blocks 3A-3G is preferably 5 to 50 m 3 /h, particularly 5 to 25 m 3 /h, and even more preferably 5 to 15 m 3 /h. A flow rate of the treated water W2 (demineralization chamber flow rate) of less than 5 m 3 /h is too small to be practical. On the other hand, a flow rate of more than 50 m 3 /h, particularly 25 m 3 /h, increases the flow rate of the treated water W2, resulting in insufficient benefits compared to using the treated water W2 as the concentrated water W3. Furthermore, the flow rate of the concentrated wastewater W4 relative to the feedwater flow rate (the flow rate of the treated water W2 + the flow rate of the concentrated wastewater W4) is preferably 2.5 to 10 vol%, particularly approximately 5 vol%. If the flow rate of concentrated wastewater W4 is less than 2.5% by volume, the amount of concentrated wastewater W4 is too small, resulting in a high ion concentration flowing in from the desalination chamber, and back diffusion cannot be ignored, making it easy for the quality of the treated water W2 to deteriorate.On the other hand, if the flow rate exceeds 10% by volume, the amount of concentrated water W3 becomes too large, and converting the treated water W1 into concentrated water W3 results in an excessively large amount of water being supplied, which is not desirable.
第五の実施形態
［電気脱イオン装置］
図５は、本発明の第三の実施形態による電気脱イオン装置を示している。
図５において、電気脱イオン装置は、前述した第四の実施形態において、濃縮水供給ライン６１の定流量弁１１Ｃを有せず、濃縮排水流出ライン７の左右両側には、手動弁の代わりに流量制御手段としての定流量弁１３Ａ，１３Ｂがそれぞれ設けられている以外、同じ構成を有する。
Fifth embodiment [electrodeionization device]
FIG. 5 shows an electrodeionization apparatus according to a third embodiment of the present invention.
In Figure 5, the electrodeionization apparatus has the same configuration as in the fourth embodiment described above, except that it does not have the constant flow valve 11C on the concentrated water supply line 61, and constant flow valves 13A and 13B are provided on both the left and right sides of the concentrated wastewater outflow line 7 as flow control means instead of manual valves.
［電気脱イオン装置の運転方法］
次に上述したような構成を有する電気脱イオン装置の運転方法について説明する。
まず、給水ポート４Ａ，４Ｂ側から給水ライン４を経てサブブロック３Ａ～３Ｇの脱塩室に上側から被処理水Ｗ１を供給するとともに、濃縮水供給ライン６１から濃縮水Ｗ３を供給し濃縮水供給ライン６を経て各濃縮室に下側から濃縮水Ｗ３を供給する。被処理水Ｗ１は、各サブブロック３Ａ～３Ｇの脱塩室を図示上側から下側に通過して、各処理水流出管から処理水流出ライン５を経て処理水流出ポート５Ａ，５Ｂ側から排出される。また、濃縮水Ｗ３は、濃縮水供給ライン６の左右両側から各サブブロック３Ａ～３Ｆの濃縮室を図示下側から上側に通過して、各濃縮排水流出管から濃縮排水流出ライン７を経て濃縮排水流出ポート７Ａ，７Ｂ側から排出される。このとき、各濃縮室では充填されているイオン交換樹脂の充填率がわずかに異なるなどの要因により、各濃縮室における濃縮水Ｗ３の通水抵抗が異なり、濃縮排水流出ポート７Ａ側と７Ｂ側とで流量が異なり、流量が少ない側のポートの濃縮室では濃縮水の流量が少なくなるためにスケールが発生しやすくなる。そこで、本実施形態においては、濃縮排水流出ライン７の左右両側に定流量弁１３Ａ，１３Ｂを設けて、濃縮排水流出ポート７Ａ側と７Ｂ側とから排出する濃縮水Ｗ３の流量をサブブロック３Ａ～３Ｇの数に応じた流量比となるように設定する。この結果、各濃縮室を流通する濃縮水の水量の均一化を図ることができ、各濃縮室におけるスケールの発生の傾向を同一化することができ、ひいては各濃縮室におけるスケールの発生を抑制することができる。
[Method of operating an electrodeionization apparatus]
Next, a method for operating the electrodeionization apparatus having the above-described configuration will be described.
First, water to be treated W1 is supplied from above to the deionization chambers of sub-blocks 3A to 3G via water supply line 4 from water supply ports 4A and 4B, and concentrated water W3 is supplied from concentrated water supply line 6 to each concentration chamber from below. Water to be treated W1 passes through the deionization chambers of each sub-block 3A to 3G from top to bottom in the figure, passes through each treated water outlet pipe and treated water outlet line 5, and is discharged from treated water outlet ports 5A and 5B. Concentrated water W3 passes through the concentration chambers of each sub-block 3A to 3F from both the left and right sides of concentrated water supply line 6 from bottom to top in the figure, passes through each concentrated wastewater outlet pipe and concentrated wastewater outlet line 7, and is discharged from concentrated wastewater outlet ports 7A and 7B. In this case, due to factors such as slight differences in the filling rate of the ion exchange resin in each concentration compartment, the flow resistance of concentrated water W3 in each concentration compartment varies, resulting in different flow rates between the concentrated wastewater outlet ports 7A and 7B. The flow rate of concentrated water in the concentration compartment with the lower flow rate port is lower, making it more likely to produce scale. Therefore, in this embodiment, constant flow valves 13A and 13B are provided on both the left and right sides of the concentrated wastewater outlet line 7 to set the flow rates of concentrated water W3 discharged from the concentrated wastewater outlet ports 7A and 7B to a flow rate ratio corresponding to the number of sub-blocks 3A to 3G. This allows the amount of concentrated water flowing through each concentration compartment to be uniform, thereby equating the tendency for scale formation in each concentration compartment and ultimately suppressing scale formation in each concentration compartment.
以上、本発明の電気脱イオン装置及びその運転方法について添付図面を参照して説明してきたが、本発明は上記実施形態に限定されず、種々の変更実施が可能である。例えば、図１では、サブブロックは６個、図４では７個設置されているが、これに限定されず、１～１２個程度であればよい。また、１つのサブブロックにおける脱塩室と濃縮室とのペアの数は１～１００個程度であればよい。 The electrodeionization apparatus and its operating method of the present invention have been described above with reference to the accompanying drawings, but the present invention is not limited to the above embodiment and various modifications are possible. For example, while six sub-blocks are installed in Figure 1 and seven in Figure 4, this number is not limited to six and may be approximately one to twelve. Furthermore, the number of pairs of deionization compartments and concentration compartments in one sub-block may be approximately one to 100.
１ 電気脱イオン装置
２ フレーム
３Ａ～３Ｇ サブブロック
４ 給水ライン
４Ａ，４Ｂ 給水ポート
５ 処理水流出ライン
５Ａ，５Ｂ 処理水流出ポート
６ 濃縮水供給ライン
６１ 濃縮水供給ライン
６Ａ，６Ｂ 濃縮水給水ポート
７ 濃縮排水流出ライン
７Ａ，７Ｂ 濃縮排水流出ポート
８ 負極室
９ 正極室
１０ 電源ボックス
１１Ａ，１１Ｂ 定流量弁（流量制御手段）
１１Ｃ 定流量弁（流量制御手段）
１２Ａ，１２Ｂ 手動弁（流量制御手段）
１３Ａ，１３Ｂ 定流量弁（流量制御手段）
Ｗ１ 被処理水（給水）
Ｗ２ 処理水
Ｗ３ 濃縮水
Ｗ４ 濃縮排水
1 Electrodeionization device 2 Frames 3A to 3G Sub-block 4 Water supply lines 4A, 4B Water supply port 5 Treated water outflow lines 5A, 5B Treated water outflow port 6 Concentrated water supply line 61 Concentrated water supply lines 6A, 6B Concentrated water supply port 7 Concentrated wastewater outflow lines 7A, 7B Concentrated wastewater outflow port 8 Anode chamber 9 Cathode chamber 10 Power supply box 11A, 11B Constant flow valve (flow control means)
11C constant flow valve (flow control means)
12A, 12B Manual valve (flow rate control means)
13A, 13B Constant flow valve (flow control means)
W1 treated water (supply water)
W2 Treated water W3 Concentrated water W4 Concentrated wastewater
Claims (4)
前記各脱塩室の一側には、被処理水の供給ラインから順次分岐した被処理水流入分岐管がそれぞれ連通しており、前記各脱塩室の他側には、処理水の流出管がそれぞれ連通していて、これら各処理水の流出管が処理水の流出ラインに合流しており、前記被処理水の供給ラインの両側から前記被処理水が供給可能となっており、
前記各濃縮室の他側には、濃縮水の供給ラインから順次分岐した濃縮水流入分岐管がそれぞれ連通しており、前記各濃縮室の一側には、濃縮排水の流出管がそれぞれ連通していて、これら各濃縮排水の流出管が濃縮排水の流出ラインに合流しており、前記濃縮水の供給ラインの両側から前記濃縮水が供給可能となっているとともに、前記濃縮排水の流出ラインの両側から前記濃縮水が排出可能となっており、
前記濃縮水の供給ラインの両側から供給する前記濃縮水の流量及び前記濃縮排水の流出ラインの両側から排出する前記濃縮水の流量を制御する流量制御手段を有し、
前記流量制御手段は、前記濃縮水の供給ラインの両側から供給する前記濃縮水の流量がそれぞれ同量となるように制御するとともに、前記濃縮排水の流出ラインの両側から排出する前記濃縮水の流量がそれぞれ同量となるように制御する、電気脱イオン装置。 An electrodeionization apparatus comprising a cathode and an anode, a plurality of cation exchange membranes and anion exchange membranes disposed between the cathode and the anode, a plurality of deionization compartments and concentration compartments partitioned by the cation exchange membranes and the anion exchange membranes, the deionization compartments and the concentration compartments being filled with ion exchange resins, a means for passing water to be treated through the plurality of deionization compartments to extract deionized water as treated water , and a concentrated water passing means for passing concentrated water through the concentration compartments,
One side of each deionization chamber is connected to a water inlet branch pipe branching off from a water supply line, and the other side of each deionization chamber is connected to a water outlet pipe, which merges with the water outlet line , allowing the water to be supplied from both sides of the water supply line.
The other side of each of the concentration chambers is connected to a concentrated water inlet branch pipe branched in sequence from a concentrated water supply line, and one side of each of the concentration chambers is connected to a concentrated wastewater outlet pipe , and these concentrated wastewater outlet pipes merge into a concentrated wastewater outlet line, so that the concentrated water can be supplied from both sides of the concentrated water supply line and can be discharged from both sides of the concentrated wastewater outlet line,
a flow rate control means for controlling the flow rate of the concentrated water supplied from both sides of the concentrated water supply line and the flow rate of the concentrated water discharged from both sides of the concentrated wastewater discharge line;
The flow rate control means controls the flow rates of the concentrated water supplied from both sides of the concentrated water supply line to be equal, and controls the flow rates of the concentrated water discharged from both sides of the concentrated wastewater outlet line to be equal .
前記供給ラインの両側から前記被処理水を供給して前記流出ラインの両側から前記処理水を取り出し、
前記濃縮水の供給ラインの両側から前記濃縮水を供給して、前記濃縮排水の流出ラインの両側から前記濃縮水を排出するに際し、前記濃縮水の供給ラインの両側から供給する前記濃縮水の流量がそれぞれ同量となるように制御するとともに、前記濃縮排水の流出ラインの両側から排出する前記濃縮水の流量がそれぞれ同量となるように前記流量制御手段により制御する、電気脱イオン装置の運転方法。 The apparatus comprises a cathode and an anode, a plurality of cation exchange membranes and anion exchange membranes arranged between the cathode and anode, and a plurality of deionization compartments and concentration compartments partitioned by these cation exchange membranes and anion exchange membranes, the deionization compartments and the concentration compartments being filled with ion exchange resin, and comprises means for passing water to be treated through the plurality of deionization compartments to extract deionized water as treated water , and concentrated water passing means for passing concentrated water through the concentration compartments, one side of each deionization compartment is connected to a water to be treated inlet branch pipe which branches off in sequence from a water to be treated supply line , and the other side of each deionization compartment is connected to a treated water outlet pipe, and each treated water outlet pipe meets the treated water outlet line. a flow control means for controlling the flow rate of the concentrated water discharged from both sides of the concentrated wastewater outlet line, the method comprising: a flow control means for controlling the flow rate of the concentrated water discharged from both sides of the concentrated wastewater outlet line ; a concentrated water inlet branch pipe branching from the concentrated water supply line in sequence communicating with the other side of each of the concentration chambers; a concentrated wastewater outlet pipe communicating with one side of each of the concentration chambers; and the concentrated wastewater outlet pipes joining the concentrated wastewater outlet line, the concentrated water being able to be supplied from both sides of the concentrated water supply line and discharged from both sides of the concentrated wastewater outlet line;
The untreated water is supplied from both sides of the supply line and the treated water is taken out from both sides of the outflow line;
a flow rate control means for controlling the flow rates of the concentrated water discharged from both sides of the concentrated wastewater outlet line so as to be equal to each other when the concentrated water is supplied from both sides of the concentrated water supply line and discharged from both sides of the concentrated wastewater outlet line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| PCT/JP2025/019654 WO2026023244A1 (en) | 2024-07-25 | 2025-05-30 | Electric deionization apparatus and method for operating same |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2024120282 | 2024-07-25 | ||
| JP2024120282 | 2024-07-25 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2026020014A JP2026020014A (en) | 2026-02-05 |
| JP7816616B2 true JP7816616B2 (en) | 2026-02-18 |
Family
ID=98651029
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2025075454A Active JP7816616B2 (en) | 2024-07-25 | 2025-04-30 | Electrodeionization apparatus and its operating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP7816616B2 (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014104401A (en) | 2012-11-26 | 2014-06-09 | Miura Co Ltd | Pure water producing apparatus |
| JP2018176033A (en) | 2017-04-06 | 2018-11-15 | オルガノ株式会社 | Pure water production equipment |
| JP2022160867A (en) | 2021-04-07 | 2022-10-20 | 栗田工業株式会社 | Electrodeionization system and method for controlling electrodeionization system |
| JP2023112836A (en) | 2022-02-02 | 2023-08-15 | 栗田工業株式会社 | Pure water manufacturing equipment and method of operating pure water manufacturing equipment |
| JP2023115943A (en) | 2022-02-09 | 2023-08-22 | 三菱重工業株式会社 | Electrodialyzer |
| JP2024092938A (en) | 2022-12-26 | 2024-07-08 | 栗田工業株式会社 | Electrodeionization apparatus and method of operating same |
-
2025
- 2025-04-30 JP JP2025075454A patent/JP7816616B2/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2014104401A (en) | 2012-11-26 | 2014-06-09 | Miura Co Ltd | Pure water producing apparatus |
| JP2018176033A (en) | 2017-04-06 | 2018-11-15 | オルガノ株式会社 | Pure water production equipment |
| JP2022160867A (en) | 2021-04-07 | 2022-10-20 | 栗田工業株式会社 | Electrodeionization system and method for controlling electrodeionization system |
| JP2023112836A (en) | 2022-02-02 | 2023-08-15 | 栗田工業株式会社 | Pure water manufacturing equipment and method of operating pure water manufacturing equipment |
| JP2023115943A (en) | 2022-02-09 | 2023-08-22 | 三菱重工業株式会社 | Electrodialyzer |
| JP2024092938A (en) | 2022-12-26 | 2024-07-08 | 栗田工業株式会社 | Electrodeionization apparatus and method of operating same |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2026020014A (en) | 2026-02-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP3794268B2 (en) | Electrodeionization apparatus and operation method thereof | |
| US5026465A (en) | Electrodeionization polarity reversal apparatus and process | |
| CN101541686B (en) | Electrodeionizer | |
| US20230331586A1 (en) | Control method for ultrapure water producing apparatus | |
| JP4197380B2 (en) | Electrodeionization equipment | |
| JP7275536B2 (en) | Electrodeionization apparatus and method for producing deionized water using the same | |
| JP2001113281A (en) | Electrodeionization equipment and pure water production equipment | |
| US6565725B2 (en) | Method for producing deionized water | |
| JP7460012B1 (en) | Electrodeionization apparatus and method of operating same | |
| WO1997046491A1 (en) | Process for producing deionized water by electrical deionization technique | |
| CN1774403B (en) | Electrodeionization apparatus and method of operating the same | |
| JPWO2018235366A1 (en) | Control method and design method of electric deionization apparatus | |
| WO2004071968A1 (en) | Electric deionization apparatus and method of operating the same | |
| JPH08150393A (en) | Production of deionized water by electrolytic deionization method | |
| JP7816616B2 (en) | Electrodeionization apparatus and its operating method | |
| JP3900666B2 (en) | Deionized water production method | |
| CN107555619A (en) | A kind of electric deionizing method and device for strengthening antiscale | |
| WO2026023244A1 (en) | Electric deionization apparatus and method for operating same | |
| CN101671070A (en) | Electric deionizing method and device containing protective water flow | |
| JP4552273B2 (en) | Electrodeionization equipment | |
| JP3901107B2 (en) | Electrodeionization apparatus and operation method thereof | |
| JP7380730B2 (en) | How to operate an electrodeionization device | |
| JP2001079552A (en) | Electric deionizing device | |
| JP4803649B2 (en) | Operation method of electric deionized water production apparatus and electric deionized water production apparatus | |
| CN109012201A (en) | A kind of electric dialyzator |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A621 | Written request for application examination |
Free format text: JAPANESE INTERMEDIATE CODE: A621 Effective date: 20250530 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20250812 |
|
| A521 | Request for written amendment filed |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20251006 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20260106 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20260119 |
|
| R150 | Certificate of patent or registration of utility model |
Ref document number: 7816616 Country of ref document: JP Free format text: JAPANESE INTERMEDIATE CODE: R150 |