TWI749260B - Electrical deionized water production apparatus - Google Patents
Electrical deionized water production apparatus Download PDFInfo
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- TWI749260B TWI749260B TW107132744A TW107132744A TWI749260B TW I749260 B TWI749260 B TW I749260B TW 107132744 A TW107132744 A TW 107132744A TW 107132744 A TW107132744 A TW 107132744A TW I749260 B TWI749260 B TW I749260B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 193
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 239000008367 deionised water Substances 0.000 title abstract description 9
- 229910021641 deionized water Inorganic materials 0.000 title abstract description 9
- 238000010612 desalination reaction Methods 0.000 claims abstract description 238
- 239000012528 membrane Substances 0.000 claims abstract description 215
- 239000003011 anion exchange membrane Substances 0.000 claims abstract description 164
- 238000005341 cation exchange Methods 0.000 claims abstract description 140
- 150000001450 anions Chemical class 0.000 claims abstract description 110
- 150000001768 cations Chemical class 0.000 claims description 63
- 239000003014 ion exchange membrane Substances 0.000 claims description 30
- 150000002500 ions Chemical class 0.000 claims description 29
- 239000008400 supply water Substances 0.000 claims description 8
- 230000002378 acidificating effect Effects 0.000 abstract description 2
- 239000002253 acid Substances 0.000 description 42
- 239000003957 anion exchange resin Substances 0.000 description 42
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 23
- 239000003729 cation exchange resin Substances 0.000 description 22
- 238000006460 hydrolysis reaction Methods 0.000 description 17
- 238000005115 demineralization Methods 0.000 description 16
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- 238000005342 ion exchange Methods 0.000 description 12
- 230000000052 comparative effect Effects 0.000 description 10
- 238000009826 distribution Methods 0.000 description 9
- -1 hydrogen ions Chemical class 0.000 description 9
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- 229920003303 ion-exchange polymer Polymers 0.000 description 7
- 238000006243 chemical reaction Methods 0.000 description 6
- 238000009792 diffusion process Methods 0.000 description 6
- 238000000034 method Methods 0.000 description 6
- 230000007062 hydrolysis Effects 0.000 description 5
- 230000007935 neutral effect Effects 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 239000003054 catalyst Substances 0.000 description 4
- 238000002242 deionisation method Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000010494 dissociation reaction Methods 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229920000642 polymer Polymers 0.000 description 4
- 239000011734 sodium Substances 0.000 description 4
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 3
- 238000005349 anion exchange Methods 0.000 description 3
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- 230000000694 effects Effects 0.000 description 3
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- 230000007246 mechanism Effects 0.000 description 3
- 238000001223 reverse osmosis Methods 0.000 description 3
- 229910052708 sodium Inorganic materials 0.000 description 3
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 2
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- 229910052796 boron Inorganic materials 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
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- 229920001577 copolymer Polymers 0.000 description 2
- 238000011033 desalting Methods 0.000 description 2
- 238000011156 evaluation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000011159 matrix material Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 239000010970 precious metal Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N 2-Propenoic acid Natural products OC(=O)C=C NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- MJUBAJMTFPBLMX-UHFFFAOYSA-N O=[Si]=O.O[Si](O)(O)O Chemical compound O=[Si]=O.O[Si](O)(O)O MJUBAJMTFPBLMX-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- YAWNFGAHEUCLNJ-UHFFFAOYSA-N [B].OB(O)O Chemical compound [B].OB(O)O YAWNFGAHEUCLNJ-UHFFFAOYSA-N 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
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- 125000000129 anionic group Chemical group 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 125000003178 carboxy group Chemical group [H]OC(*)=O 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
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- 229910001385 heavy metal Inorganic materials 0.000 description 1
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- 150000003512 tertiary amines Chemical class 0.000 description 1
- 125000001302 tertiary amino group Chemical group 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Classifications
-
- 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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—Apparatus therefor
- B01D61/463—Apparatus therefor comprising the membrane sequence AC or CA, where C is a cation exchange membrane
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
- C02F1/4695—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis electrodeionisation
-
- 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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—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
- B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
- B01D61/44—Ion-selective electrodialysis
- B01D61/46—Apparatus therefor
- B01D61/48—Apparatus therefor having one or more compartments filled with ion-exchange material, e.g. electrodeionisation
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
-
- 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
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- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Health & Medical Sciences (AREA)
- Urology & Nephrology (AREA)
- Life Sciences & Earth Sciences (AREA)
- Molecular Biology (AREA)
- Analytical Chemistry (AREA)
- Electrochemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
Description
本發明關於電去離子水製造裝置。The present invention relates to a device for producing electrodeionized water.
近年已開發出不需要利用藥劑再生之電去離子水製造裝置(以下有時稱為「EDI裝置」)，並已實用化。EDI裝置係組合了電泳與電透析之裝置。一般EDI裝置之基本結構如下所述。亦即，EDI裝置具有脫鹽室、配置於脫鹽室兩側之一對的濃縮室、配置於其中一濃縮室外側之陽極(正極)室、及配置於另一濃縮室外側之陰極(負極)室。脫鹽室具有互相對向配置之陰離子交換膜及陽離子交換膜、及填充在這些交換膜之間的離子交換體(陰離子交換體或/及陽離子交換體)。存在被處理水中之陰離子成分及陽離子成分各別通過陰離子交換膜及陽離子交換膜，並從脫鹽室移動到濃縮室，而從脫鹽室可獲得處理水亦即去離子水，從濃縮室可獲得濃縮水。In recent years, an electrodeionized water production device (hereinafter sometimes referred to as "EDI device") that does not require the use of chemical regeneration has been developed and has been put into practical use. The EDI device is a device that combines electrophoresis and electrodialysis. The basic structure of a general EDI device is as follows. That is, the EDI device has a desalination chamber, a pair of concentration chambers arranged on both sides of the desalination chamber, an anode (positive) chamber arranged on the outside of one of the concentration chambers, and a cathode (negative) chamber arranged on the outside of the other concentration chamber. . The desalination chamber has an anion exchange membrane and a cation exchange membrane arranged opposite to each other, and an ion exchanger (anion exchanger or/and cation exchanger) filled between these exchange membranes. The anion and cation components in the water to be treated pass through the anion exchange membrane and the cation exchange membrane, and move from the desalination chamber to the concentration chamber. The treated water, ie deionized water, can be obtained from the desalination chamber, and the concentration can be obtained from the concentration chamber. water.
製造去離子水時，係以在各別設於陽極室及陰極室之電極間施加直流電壓的狀態，使被處理水通水於脫鹽室中。於脫鹽室則利用陰離子交換體捕捉陰離子成分(Cl-
、CO3 2-
、HCO3 -
、SiO2
等)，並利用陽離子交換體捕捉陽離子成分(Na+
、Ca2+
、Mg2+
等)。同時例如在脫鹽室內之陰離子交換體與陽離子交換體之界面會發生水的解離反應，並產生氫離子與氫氧化物離子(H2
O→H+
+OH-
)。被離子交換體捕捉的離子成分會和前述氫離子及氫氧化物離子交換而從離子交換體游離出來。游離出的離子成分會沿著離子交換體電泳至離子交換膜(陰離子交換膜或陽離子交換膜)，並於離子交換膜經電透析而往濃縮室移動。移動至濃縮室之離子成分會藉由流經濃縮室的水而排出。When producing deionized water, the treated water is passed through the desalination chamber in a state where a DC voltage is applied between the electrodes separately provided in the anode chamber and the cathode chamber. Desalting compartment to the capture anion exchanger using anion component (Cl -, CO 3 2-, HCO 3 -,
EDI裝置會發生濃縮水所含的弱酸成分通過分隔濃縮室與脫鹽室之陽離子交換膜而擴散到處理水中，並使處理水的純度降低之現象。此現象起因於以碳酸、或二氧化矽(矽酸)、硼(硼酸)為代表之弱酸成分因應pH等之變化而有部分會形成未離子化的分子(中性分子)之形態，故不易受到陽離子交換膜所為之選擇透過性的影響。例如就碳酸而言，有式(1)~(3)表示之平衡關係。於碳酸的情況，上述未離子化的分子(中性分子)之形態為CO2 以及H2 CO3 ，它們可輕易通過陽離子交換膜。The EDI device will cause the weak acid components contained in the concentrated water to diffuse into the treated water through the cation exchange membrane that separates the concentration chamber and the desalination chamber, and reduce the purity of the treated water. This phenomenon is caused by weak acid components represented by carbonic acid, silicon dioxide (silicic acid), and boron (boric acid). Some of them will form unionized molecules (neutral molecules) in response to changes in pH, so it is not easy Affected by the selective permeability of the cation exchange membrane. For example, for carbonic acid, there is a balance relationship represented by formulas (1) to (3). In the case of carbonic acid, the aforementioned unionized molecules (neutral molecules) are in the form of CO 2 and H 2 CO 3 , which can easily pass through the cation exchange membrane.
[化1]
專利文獻1揭示一種可抑制從濃縮室擴散到脫鹽室之弱酸成分混入處理水之EDI裝置。該裝置利用離子交換膜將脫鹽室分隔成第1小脫鹽室與第2小脫鹽室，並於第1小脫鹽室填充陰離子交換體，於第2小脫鹽室以被處理水最後通過的離子交換體成為陰離子交換體之順序，填充陰離子交換體與陽離子交換體。
又，專利文獻1揭示為了促進水解離反應同時實現電流密度之適當的分配，在填充於第2小脫鹽室之陰離子交換體之靠陰極側，以雙極膜之陰離子交換膜面面向前述陰離子交換體的方式配置有該雙極膜。In addition,
專利文獻2、3也揭示於EDI裝置中使用雙極膜。專利文獻4、5、非專利文獻1揭示雙極膜。
[先前技術文獻]
[專利文獻]
專利文獻1：日本特開2012-161758號公報 專利文獻2：國際公開第2013/018818號小冊 專利文獻3：國際公開第2011/152226號小冊 專利文獻4：日本特開平7-11021號公報 專利文獻5：日本特開2010-132829號公報 [非專利文獻]Patent Document 1: JP 2012-161758 A Patent Document 2: International Publication No. 2013/018818 Pamphlet Patent Document 3: International Publication No. 2011/152226 Pamphlet Patent Document 4: Japanese Patent Laid-Open No. 7-11021 Patent Document 5: Japanese Patent Application Laid-Open No. 2010-132829 [Non-Patent Literature]
非專利文獻1：田中良修，「離子交換膜 基礎與應用」，2016年，丸善出版，p15~18。Non-Patent Document 1: Ryosuke Tanaka, "Ion Exchange Membrane" Basics and Applications", 2016, Maruzen Publishing, p15~18.
[發明所欲解決之課題][The problem to be solved by the invention]
在EDI裝置，如何有效率地從被處理水去除從濃縮室擴散到脫鹽室內之被處理水中的弱酸成分非常重要。In the EDI device, how to efficiently remove the weak acid components in the treated water that diffuses from the concentration chamber to the desalination chamber from the treated water is very important.
本發明之目的係提供能有效率地從被處理水去除從濃縮室擴散到脫鹽室內之被處理水中的弱酸成分之新式結構的EDI裝置。 [解決課題之手段]The object of the present invention is to provide an EDI device with a new structure that can efficiently remove the weak acid components in the treated water that diffuses from the concentration chamber into the desalination chamber from the treated water. [Means to solve the problem]
根據本發明之一態樣，係提供一種電去離子水製造裝置， 在互相對向的陰極與陽極之間設有至少一個脫鹽處理部， 前述脫鹽處理部具有至少填充有陰離子交換體之脫鹽室、及設於該脫鹽室兩旁之一對的濃縮室， 前述脫鹽室藉由陽離子交換膜而鄰接於前述一對的濃縮室之中靠前述陰極側之濃縮室，同時藉由第1陰離子交換膜而鄰接於前述一對的濃縮室之中靠前述陽極側之濃縮室，其特徵為： 在前述陽離子交換膜之靠脫鹽室側之面的一部分區域重疊設置有和前述陽離子交換膜不為同體之第2陰離子交換膜， 前述陰離子交換體與前述第2陰離子交換膜之靠脫鹽室側之面的至少一部分接觸。 [發明之效果]According to one aspect of the present invention, there is provided a device for producing electrodeionized water, At least one desalination treatment part is provided between the cathode and the anode facing each other, The aforementioned desalination treatment section has a desalination chamber filled with at least an anion exchanger, and a pair of concentration chambers provided on both sides of the desalination chamber, The desalination chamber is adjacent to the concentration chamber on the cathode side of the pair of concentration chambers by a cation exchange membrane, and is adjacent to the anode side of the pair of concentration chambers by a first anion exchange membrane. The enrichment room is characterized by: A second anion exchange membrane that is not the same body as the cation exchange membrane is overlapped with a part of the surface of the cation exchange membrane on the side of the desalination chamber, The anion exchanger is in contact with at least a part of the surface of the second anion exchange membrane on the side of the desalination chamber. [Effects of the invention]
根據本發明可提供能有效率地從被處理水去除從濃縮室擴散到脫鹽室內之被處理水中的弱酸成分之新式結構的EDI裝置。According to the present invention, it is possible to provide an EDI device with a new structure that can efficiently remove weak acid components in the treated water that diffuses from the concentration chamber into the desalination chamber from the treated water.
在脫鹽室填充有陰離子交換體之EDI裝置，可利用該陰離子交換體捕捉從濃縮室擴散到脫鹽室之弱酸成分並從處理水去除。但是，在接近脫鹽室之出口的區域，從濃縮室擴散而來的弱酸成分之一部分，容易在被脫鹽室內之陰離子交換體捕捉而去除之前，便從脫鹽室排出並混入處理水中。據認為會發生此現象乃因從濃縮室擴散而來的弱酸成分並未充分和該陰離子交換體接觸而滲漏到處理水側所致。An EDI device filled with an anion exchanger in the desalination chamber can use the anion exchanger to capture the weak acid components diffused from the concentration chamber to the desalination chamber and remove it from the treated water. However, in the area close to the outlet of the desalination chamber, a part of the weak acid components diffused from the concentration chamber is easily discharged from the desalination chamber and mixed into the treated water before being captured and removed by the anion exchanger in the desalination chamber. It is thought that this phenomenon occurs because the weak acid component diffused from the concentration chamber does not sufficiently contact the anion exchanger and leaks to the treated water side.
圖7(a)係針對以往的EDI裝置之一例，概念性地顯示脫鹽室23與脫鹽室23之靠陰極側之濃縮室24的邊界附近。在該EDI裝置中，陽離子交換膜33區劃出脫鹽室23與脫鹽室23之靠陰極側之濃縮室24。脫鹽室23填充有粒狀的陰離子交換樹脂51作為陰離子交換體，陰離子交換樹脂51與陽離子交換膜33之靠脫鹽室側之面接觸。在如此的裝置中，就陽離子交換膜33與陰離子交換樹脂51接觸的部分而言，從濃縮室24經由陽離子交換膜33擴散而來的弱酸成分，可利用陰離子交換樹脂51的離子交換反應而離子化並捕捉。例如碳酸(H2
CO3
)會被陰離子交換樹脂51轉化為碳酸氫離子(HCO3 -
)或碳酸離子(CO3 2-
)並予以捕捉。受到捕捉的陰離子能沿著陰離子交換樹脂51而移動到對向側(陽極側)之濃縮室。另一方面，據認為在陽離子交換膜33未與陰離子交換樹脂51接觸的部分，弱酸成分會從陽離子交換膜33放出到脫鹽室23內的液相中，而其中一部分會直接混入處理水中。Fig. 7(a) is an example of a conventional EDI device, conceptually showing the vicinity of the boundary between the
本發明人們發現如圖7(b)所示，在區劃脫鹽室23與濃縮室24之陽離子交換膜33之靠脫鹽室側之面重疊配置陰離子交換膜40之結構，用來解決前述課題可能有效。根據此結構，經由陽離子交換膜33而擴散到脫鹽室側之弱酸成分會穿透過陰離子交換膜40。此時弱酸成分會在陰離子交換膜40之內部經離子交換而從中性分子轉化為陰離子，從而成為容易受脫鹽室23內部之陰離子交換樹脂51捕捉之離子形態。The present inventors found that as shown in Figure 7(b), the structure of overlapping the
本發明人們為了實現如圖7(b)般的結構，探討有關使用雙極膜來替代圖7(a)之陽離子交換膜33的情況。雙極膜係陽離子交換膜與陰離子交換膜成為一體之膜，通常具有將陽離子交換膜與陰離子交換膜貼合而成的結構。又，雙極膜係以其陽離子交換膜與陰離子交換膜之貼合面具有對水的解離反應最佳化之結構並使水的解離反應容易進行的方式構成。因該目的，一般而言會在貼合面導入水解離用之具有觸媒作用的物質。就觸媒成分而言，例如使用如非專利文獻1之揭示內容般之金屬(尤其是重金屬離子)或三級胺等觸媒成分等。In order to realize the structure as shown in FIG. 7(b), the present inventors discussed the use of a bipolar membrane to replace the
圖9顯示如上述般使用雙極膜之結構。雙極膜50具有陽離子交換膜部50c及陰離子交換膜部50a。在陽離子交換膜部50c與陰離子交換膜部50a之貼合面，H2
O因水解離反應而轉化為H+
與OH-
並消耗，故需要有效率地供給水。該水係利用沿各別之膜部(50a、50c)之厚度方向滲透至貼合面的水分而進行供給。因此，為了平順地進行水的供給，雙極膜50之陽離子交換膜部50c及陰離子交換膜部50a中至少一者需要薄化。但是，考量強度的觀點、或製造上的問題，有時也有無法將陽離子交換膜部、陰離子交換膜部之厚度薄化的情況。Figure 9 shows a structure using bipolar membranes as described above. The
另一方面，據認為為了以圖7(b)所示之結構更確實地在陰離子交換膜40中將擴散自濃縮室之弱酸成分予以離子化，較厚的陰離子交換膜40較適合。由此可見不使用雙極膜而實現如圖7(b)般的結構較為理想。又，具有陰離子交換膜與陽離子交換膜之貼合結構的雙極膜，比起以單一離子交換體構成的陰離子交換膜或陽離子交換膜，前者就成本而言會變高。因此，考慮成本的觀點，不使用雙極膜也較理想。On the other hand, it is considered that in order to more reliably ionize the weak acid component diffused from the concentration chamber in the
關於此點，本發明人們發現藉由使陽離子交換膜33與陰離子交換膜40不為同體，且將陰離子交換膜40重疊設置於陽離子交換膜33之靠脫鹽室側之面的一部分區域而非全部，可將水平順地供給至陽離子交換膜33與陰離子交換膜40之界面。根據此結構，在決定各別的離子交換膜之厚度時，不需要考慮朝這些離子交換膜之界面之水的供給。因此，設計的自由度高，且將陰離子交換膜40加厚較容易。In this regard, the present inventors found that the
將該結構概念性地顯示於圖8。另外，圖8省略了陰離子交換樹脂51之圖示。又，圖8可觀察到陽離子交換膜33與陰離子交換膜40似為分離，但這些膜可抵接。This structure is conceptually shown in FIG. 8. In addition, the illustration of the anion exchange resin 51 is omitted in FIG. 8. In addition, in FIG. 8, it can be observed that the
在陽離子交換膜33與陰離子交換膜40之界面，若水解離反應進行並消耗H2
O的話，脫鹽室23內的水會從陰離子交換膜40之端部(圖8中沿紙面上下方向之端部)與陽離子交換膜33之間供給。而且，OH-
離子會通過陰離子交換膜40而供給於脫鹽室23，H+
離子會通過陽離子交換膜33而供給於濃縮室24。At the interface between the
另外，本發明人們的探討也發現在圖8所示之結構中使用雙極膜替代陰離子交換膜40時(參照後述比較例3)，有時會發生電流集中流通於雙極膜的現象。據認為此係因水解離反應被雙極膜顯著促進所致。In addition, the inventors of the present invention also discovered that when a bipolar membrane is used instead of the
相對於此，在圖8所示之結構中，水解離反應在不為同體之離子交換膜彼此疊合的界面進行之電壓會接近通常離子交換樹脂與離子交換膜之接觸點(例如圖7(a)中的陽離子交換膜33與陰離子交換樹脂51之接觸點)所進行的水解離反應之電壓。因此，根據圖8所示之結構，比起於水解離的反應部使用具有觸媒功能之雙極膜時，前者容易抑制電流集中地流通之現象。In contrast, in the structure shown in Figure 8, the voltage at which the hydrolysis reaction proceeds at the interface where the ion exchange membranes that are not homologous overlap each other is close to the contact point between the usual ion exchange resin and the ion exchange membrane (for example, Figure 7 (a) The contact point between the
本發明係基於上述見解而成。根據本發明，能有效率地處理從濃縮室擴散而來的弱酸成分，並獲得高純度的處理水。此外，亦可緩解如上述般利用雙極膜時所發生的電流集中，其結果能獲得更高純度的處理水。The present invention is based on the above findings. According to the present invention, the weak acid components diffused from the concentration chamber can be efficiently treated, and high-purity treated water can be obtained. In addition, the current concentration that occurs when the bipolar membrane is used as described above can also be alleviated, and as a result, higher-purity treated water can be obtained.
以下，參照圖式同時針對本發明之形態進行詳細地說明，但本發明並不限於此。Hereinafter, the form of the present invention will be described in detail with reference to the drawings, but the present invention is not limited to this.
圖1顯示基於本發明之EDI裝置的基本態樣。EDI裝置係在互相對向的陰極12與陽極11之間設有至少1個脫鹽處理部。該脫鹽處理部具有脫鹽室23、及設於脫鹽室23兩旁之一對的濃縮室22與24，且還具有係第1陰離子交換膜之陰離子交換膜(AEM)32與陽離子交換膜(CEM)33。Figure 1 shows the basic state of the EDI device based on the present invention. The EDI device is provided with at least one desalination treatment section between the
脫鹽室23藉由陽離子交換膜33而鄰接於一對的濃縮室22、24之中靠陰極側之濃縮室24，且藉由陰離子交換膜32而鄰接於一對的濃縮室22、24之中靠陽極側之濃縮室22。因此，脫鹽室23係以位在其面對陽極11之側的陰離子交換膜32與其位在面對陰極12之側的陽離子交換膜33區劃而成。The
圖1所示之EDI裝置中，在具備陽極11之陽極室21與具備陰極12之陰極室25之間，係從陽極室21側開始按順序設置有濃縮室22、脫鹽室23及濃縮室24。陽極室21與濃縮室22係間隔陽離子交換膜31而鄰接，濃縮室24與陰極室25係間隔陰離子交換膜34而鄰接。In the EDI device shown in FIG. 1, between the
脫鹽室23內至少填充有陰離子交換體。在圖1所示之例中，陰離子交換體與陽離子交換體係成為混床(MB)而填充於脫鹽室23內。但不限於此，也可僅將陰離子交換體填充於脫鹽室23中。或亦可將一個以上的陰離子交換體床(由陰離子交換體構成的床)與一個以上的陽離子交換體床(由陽離子交換體構成的床)設置於脫鹽室23中。此時，宜以被處理水最後通過的離子交換體成為陰離子交換體之順序，將陰離子交換體床與陽離子交換體床填充於脫鹽室中。The
此外，該EDI裝置中，陽離子交換體係填充於陽極室21內，陰離子交換體係填充於濃縮室22、24及陰極室25內。但是，陽極室21、濃縮室22、24及陰極室25中並非一定要填充離子交換體(陰離子交換體或陽離子交換體)。In addition, in this EDI device, the cation exchange system is filled in the
惟，將陰離子交換體填充於濃縮室22、24時，本發明的效果較顯著。原因乃將陰離子交換體填充於濃縮室22、24時，弱酸成分從濃縮室往脫鹽室的擴散現象有較顯著的傾向所致。However, when the anion exchanger is filled in the
就陰離子交換體而言例如使用陰離子交換樹脂(AER)，就陽離子交換體而言例如使用陽離子交換樹脂(CER)。離子交換樹脂係指將官能基(離子交換基)導入到具有三維網目結構之高分子母體中而成的合成樹脂，通常使用的是粒徑為約0.4~0.8mm之球狀粒子。就離子交換樹脂的高分子母體而言，例如苯乙烯-二乙烯苯之共聚物(苯乙烯系)、丙烯酸-二乙烯苯之共聚物(丙烯酸系)等。For the anion exchanger, for example, an anion exchange resin (AER) is used, and for the cation exchanger, for example, a cation exchange resin (CER) is used. Ion exchange resin refers to a synthetic resin formed by introducing functional groups (ion exchange groups) into a polymer matrix with a three-dimensional network structure. Generally, spherical particles with a particle size of about 0.4 to 0.8 mm are used. As for the polymer matrix of the ion exchange resin, for example, styrene-divinylbenzene copolymer (styrene series), acrylic acid-divinylbenzene copolymer (acrylic acid series), and the like.
離子交換樹脂大致分為其官能基表現酸性之陽離子交換樹脂與表現鹼性之陰離子交換樹脂，此外，取決於所導入的離子交換基之種類，而有強酸性陽離子交換樹脂、弱酸性陽離子交換樹脂、強鹼性陰離子交換樹脂、弱鹼性陰離子交換樹脂等。就強鹼性陰離子交換樹脂而言，例如具有四級銨基作為官能基(離子交換基)者，就弱鹼性陰離子交換樹脂而言，例如具有一級~三級胺基作為官能基者。就強酸性陽離子交換樹脂而言，例如具有磺酸基作為官能基者，就弱酸性陽離子交換樹脂而言，例如具有羧基作為官能基者。Ion exchange resins are roughly divided into cation exchange resins with acidic functional groups and anion exchange resins with basicity. In addition, depending on the type of ion exchange groups introduced, there are strong acid cation exchange resins and weak acid cation exchange resins. , Strongly basic anion exchange resin, weakly basic anion exchange resin, etc. A strong basic anion exchange resin has, for example, a quaternary ammonium group as a functional group (ion exchange group), and a weakly basic anion exchange resin has, for example, a primary to tertiary amine group as a functional group. A strong acid cation exchange resin has a sulfonic acid group as a functional group, and a weak acid cation exchange resin has a carboxyl group as a functional group, for example.
然後，針對利用圖1所示之EDI裝置所為的去離子水(處理水)之製造進行說明。將供給水通水於陽極室21、濃縮室22、24及陰極室25，並於陽極11與陰極12之間施加直流電壓的狀態，將被處理水通水於脫鹽室23。然後，被處理水中的離子成分則會吸附於脫鹽室23內的離子交換體，而實施去離子化(脫鹽)處理，並從脫鹽室23以處理水的形式流出去離子水。此時，在脫鹽室23中，因為施加電壓而主要在不同種的離子交換體(也可為離子交換膜)彼此的界面發生水的解離反應，而生成氫離子及氫氧化物離子。然後，先前吸附於脫鹽室23內的離子交換體之離子成分會藉由該氫離子與氫氧化物離子而進行離子交換，並從離子交換體游離出來。游離出的離子成分之中，陰離子經由陰離子交換膜32而移動到靠陽極側之濃縮室22，並從該濃縮室22以濃縮水的形式排出，陽離子則經由陽離子交換膜33而移動到靠陰極側之濃縮室24，並從該濃縮室24以濃縮水的形式排出。結果，供給至脫鹽室23之被處理水中的離子成分會遷移至濃縮室22、24而被排出，同時脫鹽室23的離子交換體會再生。另外，從陽極室21及陰極室25則有電極水排出。Next, the production of deionized water (treated water) using the EDI device shown in FIG. 1 will be described. The supply water is passed through the
本發明之EDI裝置中，區劃脫鹽室23與濃縮室24之陽離子交換膜33之靠脫鹽室23側的面(以下有時稱為「脫鹽室側之面」)有部分區域重疊配置有係第2陰離子交換膜之陰離子交換膜40，而非全部區域。陰離子交換膜40和陽離子交換膜33不為同體，亦即，陰離子交換膜40並未和陽離子交換膜33一體化。In the EDI device of the present invention, the surface of the
陽離子交換膜33係以區劃濃縮室24與脫鹽室23的方式設置，因此，係在脫鹽室23與濃縮室24之間的邊界實質地設置於全部區域。另一方面，如前所述，陽離子交換膜33之靠脫鹽室側之面的一部分區域重疊有陰離子交換膜40。因此，陰離子交換膜40的面積比陽離子交換膜33的面積小。利用如此的結構，陽離子交換膜33與陰離子交換膜40之界面能和脫鹽室23內的水接觸。因此，如使用圖8進行說明般，可將脫鹽室23內的水從陰離子交換膜40之端部(圖1中沿紙面上下方向之端部)與陽離子交換膜33之間供給到陽離子交換膜33與陰離子交換膜40之界面。The
以下，有時會將前述一部分區域(亦即陽離子交換膜33之靠脫鹽室側之面之中，重疊有陰離子交換膜40之區域)稱為「重疊區域」。關於一片陽離子交換膜33，能存在一個重疊區域(參照圖1~3、5~6)，也可互相間隔而存在多個重疊區域(參照圖4)。陽離子交換膜33之靠脫鹽室側之面存在一個重疊區域時，可在該區域重疊一片陰離子交換膜40。陽離子交換膜33之靠脫鹽室側之面存在多個重疊區域時，可在各別的區域逐一重疊一片陰離子交換膜40。又，存在多個重疊區域時，這些區域可沿脫鹽室23內之被處理水的通水方向，互相間隔而存在。Hereinafter, the aforementioned part of the area (that is, the area where the
考慮防止弱酸成分混入到處理水中之觀點，重疊區域宜包含陽離子交換膜33之靠脫鹽室側之面之中到達陽離子交換膜33之靠脫鹽室出口側端緣(處理水出口側之端緣)之區域。亦即，若為一個重疊區域，則該重疊區域宜到達陽離子交換膜33之靠脫鹽室出口側之端緣。有多個重疊區域時，該多個重疊區域中之一個宜到達陽離子交換膜33之靠脫鹽室出口側之端緣。尤其是重疊區域係沿脫鹽室23內之被處理水的通水方向，互相間隔而存在多個時，位在通水方向最下游之重疊區域宜到達陽離子交換膜33之靠脫鹽室出口側之端緣。Considering the viewpoint of preventing the mixing of weak acid components into the treated water, the overlapping area should preferably include the edge of the
例如，陰離子交換膜40具有和陽離子交換膜33相同之寬度(圖1中從紙面往深處方向的尺寸)，並具有比陽離子交換膜33短的長度(圖1中沿紙面上下方向的尺寸)。For example, the
又，陰離子交換膜40之靠脫鹽室23側之面的至少一部分和陰離子交換體接觸。本形態係混床(MB)和陰離子交換膜40之靠脫鹽室側之面接觸。因此，混床所含的陰離子交換體(尤其是陰離子交換樹脂)會和陰離子交換膜40之靠脫鹽室側之面接觸。藉此，輕易地將從濃縮室擴散而來且經由陰離子交換膜40而從中性分子變換為陰離子的弱酸成分，沿著填充於脫鹽室23之陰離子交換體，再通過陰離子交換膜32，而有效率地排出到濃縮室22。考慮此觀點，為了形成陰離子從陰離子交換膜40到陰離子交換膜32利用陰離子交換體來移動之路徑，宜在脫鹽室內設置陰離子交換體床或混床以使陰離子交換膜40及32連接。In addition, at least a part of the surface of the
就陽離子交換膜33、陰離子交換膜40而言，可分別使用EDI裝置、電透析裝置(ED)之領域中公知者。As the
陽離子交換膜33及陰離子交換膜40之膜厚，一般而言均為約100μm~700μm，尤其為約200~600μm。The thickness of the
考慮防止電流集中之觀點，陽離子交換膜33及陰離子交換膜40均不含如雙極膜所含之用以促進水解離反應之觸媒成分較理想。Considering the viewpoint of preventing current concentration, it is desirable that neither the
離子交換膜可大致分為異質膜與均質膜。異質膜係使離子交換樹脂之微粉末分散於適當的黏結劑(高分子化合物)，並加熱而成形為膜狀而成。異質膜的膜面存在不具有離子交換基之由不活潑的高分子化合物構成的部分。異質膜比均質膜容易製造。另一方面，均質膜係合成為膜狀之離子交換體。均質膜就膜整體係利用高程度之交聯而化學性地鍵結，並具有大量離子交換基均勻分佈的結構，且電阻比異質膜低之觀點，係優異的離子交換膜。異質膜、均質膜一般會為了改善機械性強度而以網狀物(mesh)、不織布等作為補強體而予以一體化。另外，離子交換膜和離子交換樹脂同樣，取決於所導入的官能基之種類而分類成陰離子交換膜與陽離子交換膜。Ion exchange membranes can be roughly classified into heterogeneous membranes and homogeneous membranes. The heterogeneous membrane is formed by dispersing fine powder of ion exchange resin in an appropriate binder (polymer compound) and heating it to form a film. The membrane surface of the heterogeneous membrane has a portion composed of an inactive polymer compound that does not have an ion exchange group. Heterogeneous membranes are easier to manufacture than homogeneous membranes. On the other hand, homogeneous membranes are synthesized into membrane-like ion exchangers. The homogeneous membrane is chemically bonded with a high degree of cross-linking as the whole membrane, and has a structure in which a large number of ion exchange groups are uniformly distributed, and the resistance is lower than that of a heterogeneous membrane. It is an excellent ion exchange membrane. In order to improve mechanical strength, heterogeneous membranes and homogeneous membranes are generally integrated with meshes, non-woven fabrics, etc. as reinforcements. In addition, ion exchange membranes, like ion exchange resins, are classified into anion exchange membranes and cation exchange membranes depending on the type of functional group to be introduced.
在本發明中，異質膜、均質膜中之任一者均可採用。惟，針對陽離子交換膜33與陰離子交換膜40，宜採用均質膜/均質膜、異質膜/均質膜、均質膜/異質膜中之任一者(斜線「/」之前表示陽離子交換膜33的種類，「/」之後表示陰離子交換膜40的種類)。亦即陽離子交換膜33與陰離子交換膜40中之至少一者宜為均質膜。原因乃異質膜由於具有部分無離子交換基之不活潑的區域，故在發生水解離反應的位置使用異質膜/異質膜的組合的話，有時會有水解離的反應點變少，電壓變高的情況。In the present invention, either a heterogeneous membrane or a homogeneous membrane can be used. However, for the
陽離子交換膜33與陰離子交換膜40藉由一起疊合，可在濕潤狀態下使其接觸。藉由在濕潤狀態下使兩者互相接觸，當水解離反應而水被消耗時，水會從疊合之端部被抽吸，而朝兩者之間的水供給會變得容易。又，兩者的接觸位置係作為水解離之反應部而發揮功能。The
將陽離子交換膜33與陰離子交換膜40納入EDI裝置時，可採用將各別的膜於乾燥狀態下疊合納入，然後藉由通水而成為濕潤狀態之方法。或也可在將兩者納入EDI裝置時，即以濕潤狀態進行疊合納入。例如，在將陽離子交換膜33與陰離子交換膜40重疊時，可使各別的膜成為濕潤狀態，以乾淨的純水等流洗表面髒污後再重疊。又，可使用適當的方法將兩者互相固定。When the
又，就陽離子交換膜33與陰離子交換膜40之疊合的端部而言，若為其一部分成為可從脫鹽室23將水供給(抽吸)到水解離反應部即可(並未密封，亦即為開放狀態)。例如，也可為疊合的端部之一部分未密封，而其他部分被密封。端部也可全部區域開放。就密封的方法而言，有使用黏接劑的黏接、利用加熱或超音波振動等將膜構成材料融熔而使其一體化之熔接、以及利用框架體來挾持固定的方法等。In addition, as for the overlapped end of the
就陽極11及陰極12而言，可使用EDI裝置之領域中所公知者。例如在陰極使用不銹鋼，在陽極使用鉑等貴金屬、或貴金屬鍍敷電極。As for the
就陽離子交換膜31、陰離子交換膜32、34而言，也可使用EDI裝置之領域中所公知者。又，雖然未圖示，但可將陽極11及陰極12、陽極室21、濃縮室22及24、脫鹽室23、陰極室25、陽離子交換膜31及33、以及陰離子交換膜32、34及40容納於適當的框架體(未圖示)中。As for the
就供給水、被處理水而言，也可使用EDI裝置之領域中所公知者。一般而言係使用逆滲透膜(RO)之透過水，以RO膜經2段以上處理者更佳。而且有時亦會使用脫碳酸塔、脫碳酸膜來去除碳酸。此外，在近年也有將經EDI處理後之水使用於供給水、被處理水的情況。Regarding the supply water and the water to be treated, those known in the field of EDI devices can also be used. Generally speaking, reverse osmosis membrane (RO) permeate is used, and RO membrane is better treated with more than 2 stages. In addition, decarbonation towers and decarbonation membranes are sometimes used to remove carbonic acid. In addition, in recent years, EDI-treated water has also been used for supply water and treated water.
在圖1所示之裝置中，係從下方將供給水導入到陽極室21、濃縮室22及24、以及陰極室25中，並從上方將水(電極水或濃縮水)排出，另一方面，在脫鹽室23係從上方供給被處理水，並將處理水排出到下方。但是，並不限於此，水的行進方向可適當地決定。此外，也可不從外部將水供給至陽極室21，而是將陰極室25之出口水(電極水)供給至陽極室21，亦可相反。In the device shown in Figure 1, feed water is introduced into the
從濃縮室24朝脫鹽室23之弱酸成分的擴散也會受濃縮室24中的弱酸成分之濃度影響，濃度愈高則擴散的量也會增加。在濃縮室24中，隨著從其入口往出口，濃縮倍率會上昇且弱酸成分的濃度也會變高。藉由將濃縮室24的入口側配置在鄰接於脫鹽室23的出口側，可抑制來自濃縮室24的擴散更大量的發生在脫鹽室23的處理水出口附近的位置之情況。因此，濃縮室24中的水的行進方向和鄰接的脫鹽室(於圖1所示之形態係指脫鹽室23，於圖6所示之形態係指第2小脫鹽室27)中的水的行進方向宜為逆流。The diffusion of the weak acid component from the
另外，濃縮室兼具電極室之結構亦包含於本發明中。例如也可將陰極設置於圖1所示之濃縮室24中並省略陰極室25。即使是該情況，由脫鹽室及一對的濃縮室構成的脫鹽處理部仍是配置於陰極與陽極之間。In addition, the structure of the concentrating chamber and the electrode chamber is also included in the present invention. For example, the cathode may be installed in the
EDI裝置可具有多個脫鹽處理部。因此，可將多個由[濃縮室｜第1陰離子交換膜(AEM)｜脫鹽室｜陽離子交換膜(CEM)(重疊有第2陰離子交換膜)｜濃縮室]構成的基本結構(亦即槽室套組，cell set)並排設置於陽極與陰極之間。此時，鄰接的槽室套組間可共有相鄰的濃縮室。因此，可令陰離子交換膜32、脫鹽室23、陽離子交換膜33(重疊有陰離子交換膜40)及濃縮室24構成1個槽室套組，並將多個該槽室套組配置在距離陽極室21最近的濃縮室22與陰極室25之間。圖1中，「N」意指該槽室套組的個數，N為1以上之整數。The EDI device may have multiple desalination treatment sections. Therefore, a plurality of basic structures (that is, tanks) composed of [concentration chamber | first anion exchange membrane (AEM) | The cell set is arranged side by side between the anode and the cathode. At this time, adjacent tank chamber sets can share adjacent concentration chambers. Therefore, the
以上，已針對根據本發明之EDI裝置的基本結構進行說明，但本發明可廣泛地適用於各種結構的EDI裝置中。以下，針對可應用本發明之EDI裝置的結構例進行說明。Above, the basic structure of the EDI device according to the present invention has been described, but the present invention can be widely applied to EDI devices of various structures. Hereinafter, a structural example of an EDI device to which the present invention can be applied will be described.
使用圖2，針對具有2個脫鹽處理部之形態的EDI裝置進行說明。該EDI裝置係於圖1所示之裝置中，將2個槽室套組配置於距離陽極室21最近的濃縮室22與陰極室25之間。圖2中，表示構成靠近陰極室25的槽室套組之構成要件的符號係加上「’(撇號)」。Using Fig. 2, an EDI device having two desalination treatment units will be described. The EDI device is in the device shown in FIG. In Fig. 2, the symbols showing the constituent elements constituting the cell set close to the
陽極室21中填充有陽離子交換樹脂(CER)，濃縮室22與陰極室25中填充有陰離子交換樹脂(AER)。濃縮室24及24’中均填充有陰離子交換樹脂(AER)。脫鹽室23及23’中均以混床(MB)形式填充有陰離子交換樹脂與陽離子交換樹脂。The
陽極室21與濃縮室22係利用陽離子交換膜31區劃。濃縮室22與脫鹽室23係利用陰離子交換膜32區劃。脫鹽室23與濃縮室24係利用陽離子交換膜33區劃。濃縮室24與脫鹽室23’係利用陰離子交換膜32’區劃。脫鹽室23’與濃縮室24’係利用陽離子交換膜33’區劃。濃縮室24’與陰極室25係利用陰離子交換膜34區劃。The
在陽離子交換膜33上重疊有陰離子交換膜40。在陽離子交換膜33’上重疊有陰離子交換膜40’。An
陰離子交換膜32’及40’、脫鹽室23’、陽離子交換膜33’以及濃縮室24’之構成可分別和陰離子交換膜32及40、脫鹽室23、陽離子交換膜33以及濃縮室24相同或相異。The composition of the anion exchange membranes 32' and 40', the desalination chamber 23', the cation exchange membrane 33' and the concentration chamber 24' can be the same as the
在本形態也可獲得和圖1所示之形態同樣的效果。Also in this form, the same effect as the form shown in Fig. 1 can be obtained.
另外，CO3 2-
、HCO3 -
等來自弱酸之陰離子會從脫鹽室23’通過陰離子交換膜32’而移動到濃縮室24。因而在濃縮室24內，供給水除了含有原本已含的弱酸成分之外，更含有通過陰離子交換膜32’移動而來的弱酸成分。因此，濃縮室24內的弱酸成分之濃度變得較高，弱酸成分從濃縮室24往脫鹽室23之擴散現象容易變顯著。據此，本發明在具備多個脫鹽處理部之EDI裝置中特別有效。In addition, anions from weak acids such as CO 3 2- and HCO 3 - move from the
圖3顯示依據本發明之EDI裝置的另一形態。該EDI裝置與圖1所示者同樣，惟脫鹽室23之靠入口側之區域配置有陽離子交換樹脂(CER)，靠出口側之區域配置有陰離子交換樹脂(AER)。亦即，脫鹽室23中係沿被處理水的通水方向逐一疊層由陽離子交換樹脂構成的床(陽離子交換樹脂床，亦即陽離子交換體床)及由陰離子交換樹脂構成的床(陰離子交換樹脂床，亦即陰離子交換體床)。亦即，在脫鹽室中以被處理水最後通過的離子交換體成為陰離子交換體之順序填充陰離子交換體床與陽離子交換體床。然後，在脫鹽室23內之陰離子交換體床之靠陰極側，亦即在該陰離子交換體床與陽離子交換膜33之間，配置陰離子交換膜40。脫鹽室23內之陽離子交換體床之靠陰極側則未配置陰離子交換膜40。Figure 3 shows another form of the EDI device according to the present invention. This EDI device is the same as that shown in FIG. 1, except that the area on the inlet side of the
如圖3所示脫鹽室23內之各床沿通水方向之長度(圖3中沿紙面上下方向之長度)可互為相同，但也可相異。As shown in FIG. 3, the length of each bed in the
當然該形態也可令陰離子交換膜32、脫鹽室23、陽離子交換膜33(重疊有陰離子交換膜40)及濃縮室24構成1個槽室套組，並將N(N為1以上之整數)個該槽室套組配置在距離陽極室21最近的濃縮室22與陰極室25之間。Of course, this form can also make the
圖4所示之EDI裝置與圖3所示者同樣，惟將脫鹽室23沿被處理水的通水方向分成4個區域，並以第1陽離子交換體床、第1陰離子交換體床、第2陽離子交換體床、第2陰離子交換體床之排列方式，從被處理水之入口側按順序將離子交換樹脂配置於各別區域而成。而且，第1陰離子交換體床之靠陰極側及第2陰離子交換體床之靠陰極側分別配置有陰離子交換膜40(和陽離子交換膜33重疊)。第1陽離子交換體床之靠陰極側及第2陽離子交換體床之靠陰極側均未配置陰離子交換膜40。該裝置中，重疊區域(陽離子交換膜33之靠脫鹽室側之面之中重疊有陰離子交換膜40的區域)有二個，且沿脫鹽室23內之被處理水的通水方向互相分離間隔而存在。而且，二個重疊區域之中位於通水方向最下游的一個重疊區域到達陽離子交換膜33之靠脫鹽室出口側之端緣。The EDI device shown in Fig. 4 is the same as that shown in Fig. 3, except that the
如圖4所示脫鹽室23內之各床沿通水方向之長度可互為相同，但也可相異。又，各床的數量如圖4係4個，但在製造上可行的範圍內也可為5個，亦可為6個或超過6個。As shown in Fig. 4, the lengths of the beds in the
圖5所示之EDI裝置與圖1所示者同樣，惟在脫鹽室23中，於陰離子交換膜40之靠脫鹽室側設有陰離子交換體床來替換混床(MB)。脫鹽室23在被處理水通水方向上不存在陰離子交換膜40的區域則和圖1所示之形態同樣地設有混床。The EDI device shown in FIG. 5 is the same as that shown in FIG. 1, except that in the
亦即，在該形態中，脫鹽室23之靠入口側區域配置有陰離子交換樹脂與陽離子交換樹脂之混床(MB)，靠出口側區域配置有陰離子交換體床(AER床)。亦即，混床與陰離子交換體床係沿通水方向逐一疊層於脫鹽室23中。That is, in this form, the mixed bed (MB) of anion exchange resin and cation exchange resin is arranged in the inlet side region of the
在依據本發明之EDI裝置中，各脫鹽室之靠陽極側之陰離子交換膜與靠陰極側之陽離子交換膜之間可設置中間離子交換膜(IIEM)，並利用中間離子交換膜將該脫鹽室區劃成第1小脫鹽室及第2小脫鹽室。並且能以被處理水供給於第1小脫鹽室及第2小脫鹽室中之其中一個小脫鹽室，且從該小脫鹽室流出的水流入另一個小脫鹽室的方式，將第1及第2小脫鹽室連通配置。就中間離子交換膜而言，陰離子交換膜及陽離子交換膜均可使用。此時，令靠陽極側之小脫鹽室為第1小脫鹽室，並令靠陰極側之小脫鹽室為第2小脫鹽室。例如，第1小脫鹽室中至少填充有陰離子交換體，第2小脫鹽室中至少填充有陽離子交換體。In the EDI device according to the present invention, an intermediate ion exchange membrane (IIEM) can be installed between the anion exchange membrane on the anode side and the cation exchange membrane on the cathode side of each desalination chamber, and the intermediate ion exchange membrane is used for the desalination chamber It is divided into the first small desalination room and the second small desalination room. In addition, the treated water can be supplied to one of the first and second small desalination chambers, and the water flowing out of the small desalination chamber can flow into the other small desalination chamber. 2 The small desalination chamber is connected to the configuration. As for the intermediate ion exchange membrane, both anion exchange membrane and cation exchange membrane can be used. At this time, let the small desalination chamber on the anode side be the first small desalination chamber, and let the small desalination chamber on the cathode side be the second small desalination chamber. For example, the first small desalination chamber is filled with at least an anion exchanger, and the second small desalination chamber is filled with at least a cation exchanger.
圖6顯示如上述般利用中間離子交換膜將脫鹽室區劃成2個小脫鹽室而成的EDI裝置之例。該EDI裝置具有如下結構：利用位在陰離子交換膜32與陽離子交換膜33之間的中間離子交換膜36，將圖1所示之EDI裝置中的各脫鹽室23區劃成靠陽極11側之第1小脫鹽室26及靠陰極12側之第2小脫鹽室27。第1小脫鹽室26位在陰離子交換膜32與中間離子交換膜36之間，第2小脫鹽室27位在陽離子交換膜33與中間離子交換膜36之間。第1小脫鹽室26及第2小脫鹽室27係以對第1小脫鹽室26供給被處理水後，從第1小脫鹽室26流出之水流入第2小脫鹽室27的方式進行連通。Fig. 6 shows an example of an EDI device in which the desalination chamber is divided into two small desalination chambers using an intermediate ion exchange membrane as described above. The EDI device has the following structure: using an intermediate
於第1小脫鹽室26填充陰離子交換樹脂。於第2小脫鹽室27之入口側區域配置陽離子交換樹脂，並於出口側區域配置陰離子交換樹脂。亦即，陽離子交換體床及陰離子交換體床係按此順序沿被處理水的通水方向設置於第2小脫鹽室27中。被處理水係供給於第1小脫鹽室26，且第1小脫鹽室26之出口水會送到第2小脫鹽室27，而從第2小脫鹽室27以處理水的形式獲得去離子水。因此，陰離子交換體床及陽離子交換體床係以被處理水最後通過的離子交換體成為陰離子交換體之順序填充於脫鹽室23中。The first
第2小脫鹽室27內之陰離子交換體床之靠陰極側配置有陰離子交換膜40(和陽離子交換膜33重疊)。第2小脫鹽室27內之陽離子交換體床之靠陰極側未配置陰離子交換膜40。前述重疊區域(陽離子交換膜33之靠脫鹽室側之面之中重疊有陰離子交換膜40之區域)存在一個。該重疊區域到達陽離子交換膜33之脫鹽室出口側端緣。在此，脫鹽室出口為處理水出口，在該裝置即為第2小脫鹽室27之出口。The anion exchange membrane 40 (overlaps the cation exchange membrane 33) is arranged on the cathode side of the anion exchanger bed in the second
如圖6所示第2小脫鹽室27內之各床沿通水方向之長度可互為相同，但也可相異。As shown in Fig. 6, the lengths of the beds in the second
中間離子交換膜36係使用例如陰離子交換膜。As the intermediate
在圖6所示之裝置中，第1小脫鹽室26中的水流與第2小脫鹽室27中的水流係為逆流。但不限於此，這些水流也可為並流。In the device shown in FIG. 6, the water flow in the first
被處理水係供給於第1小脫鹽室26中。所供給的被處理水中的陰離子成分會在被處理水通過第1小脫鹽室26的過程中被捕捉。在第1小脫鹽室26中，被捕捉的陰離子成分會沿第1小脫鹽室26經由陰離子交換膜32而往鄰接的濃縮室22移動，並和通水於濃縮室22之濃縮水一起排出到系統外。The treated water system is supplied to the first
然後，通過第1小脫鹽室26的被處理水會供給至第2小脫鹽室27。供給至第2小脫鹽室27之被處理水，首先通過陽離子交換體床，然後通過陰離子交換體床。此時，被處理水中的陽離子成分在被處理水通過陽離子交換體床的過程中被捕捉。具體而言，被第2小脫鹽室27內的陽離子交換體捕捉的陽離子成分會經由陽離子交換膜33而往鄰接於第2小脫鹽室27之濃縮室24移動，並從濃縮室24和濃縮水一起排出到系統外。Then, the water to be treated that has passed through the first
然後，在第2小脫鹽室27中，已通過陽離子交換體床的被處理水會通過下一階段的陰離子交換體床。此時，被處理水中的陰離子成分會再度被捕捉。具體而言，被第2小脫鹽室27之陰離子交換體捕捉的陰離子成分會經由中間離子交換膜36而往鄰接於第2小脫鹽室27之第1小脫鹽室26移動。往第1小脫鹽室26移動的陰離子成分會經由陰離子交換膜32而往鄰接於第1小脫鹽室26之濃縮室22移動，並和通水於濃縮室22之濃縮水一起排出到系統外。Then, in the second
在此，考慮有關發生濃縮室24內的濃縮水所含的弱酸成分(碳酸、二氧化矽、或硼)以中性分子的形態通過陽離子交換膜33並往第2小脫鹽室27移動之擴散現象的情況。Here, consider the diffusion of weak acid components (carbonic acid, silica, or boron) contained in the concentrated water in the
從濃縮室24往第2小脫鹽室27移動之弱酸成分會均勻地擴散至陽離子交換膜33之靠陽極側表面上。亦即，弱酸成分不僅會擴散至陽離子交換膜33之和陰離子交換膜40相接的表面區域，也會擴散至陽離子交換膜33之和第2小脫鹽室27內之陽離子交換體床相接的表面區域。而且，弱酸成分不會被陽離子交換體捕捉，故擴散至陽離子交換膜33之靠陽極側表面之中和陽離子交換體床相接的區域之弱酸成分會和被處理水一起通過陽離子交換體床。但是，在第2小脫鹽室27中沿被處理水的通水方向疊層有陽離子交換體床與陰離子交換體床。因此，通過陽離子交換體床之弱酸成分會在下一階段的陰離子交換體床中再度被離子化而捕捉，並往第1小脫鹽室26移動。移動到第1小脫鹽室26之弱酸成分會通過陰離子交換膜32而往濃縮室22移動，並和通水於濃縮室22之濃縮水一起排出到系統外。The weak acid component moving from the
如此，該形態中即使弱酸成分通過陽離子交換膜33，下一階段仍有陰離子交換體床，故可輕易使該弱酸成分從濃縮室22排出，結果可輕易抑制處理水的純度降低。當然在該形態中，也可利用陰離子交換膜40將擴散至陽離子交換膜33之和陰離子交換膜40相接的表面區域的弱酸成分有效率地從被處理水中去除。In this manner, even if the weak acid component passes through the
由上述說明可理解設置於脫鹽室內，尤其設置於第2小脫鹽室27內之離子交換體床的疊層體的最終階段宜為陰離子交換體床的情況。比起最終階段之陰離子交換體床更前面階段之離子交換體床的種類、疊層順序、疊層數並無特別限制。From the above description, it can be understood that the final stage of the laminated body of the ion exchanger bed installed in the desalination chamber, especially in the second
又，在本形態之EDI裝置中，最先被供給被處理水之第1小脫鹽室26填充有陰離子交換體，隨後被供給被處理水之第2小脫鹽室27係按順序疊層有陽離子交換體床與陰離子交換體床。因此，被處理水會先通過陰離子交換體床。藉此，陰離子成分會從被處理水去除，被處理水的pH會上昇。In addition, in the EDI device of this form, the first
此外，通過第1小脫鹽室26之被處理水會供給於按順序疊層有陽離子交換體床與陰離子交換體床之第2小脫鹽室27。亦即，通過第1小脫鹽室26內的陰離子交換體床之被處理水，隨後會通過陽離子交換體床，然後再度通過陰離子交換體床。簡而言之，依據本形態之結構，被處理水會交替通過陰離子交換體床與陽離子交換體床。In addition, the water to be treated passing through the first
在此，陰離子交換體對陰離子成分的捕捉能力在被處理水之pH低時為高，陽離子交換體對陽離子成分的捕捉能力在被處理水之pH高時為高。因此，依據被處理水最先通過陰離子交換體床，然後交替通過陽離子交換體床與陰離子交換體床之本形態的結構，陰離子成分藉由通過陰離子交換體而去除，且pH上昇後之被處理水隨後會通過陽離子交換體床。因此，會比通常更為促進陽離子交換體所為之陽離子去除反應。Here, the anion exchanger's ability to capture anion components is high when the pH of the water to be treated is low, and the cation exchanger's ability to capture cation components is high when the pH of the water to be treated is high. Therefore, according to the structure of the original form in which the treated water first passes through the anion exchanger bed and then alternately passes through the cation exchanger bed and the anion exchanger bed, the anion component is removed by passing through the anion exchanger, and the pH is increased after the treatment The water then passes through the cation exchanger bed. Therefore, the cation removal reaction by the cation exchanger is promoted more than usual.
此外，陽離子成分藉由通過陽離子交換體床而去除，且pH降低後之被處理水隨後會通過陰離子交換體床。因此，會比通常更為促進陰離子交換體所為之陰離子去除反應。因此，不僅更改善包含碳酸、二氧化矽、或硼之陰離子成分的去除能力，也改善陽離子成分之去除能力，所以處理水的純度會進一步改善。In addition, the cation components are removed by passing through the cation exchanger bed, and the treated water after the pH decreases will then pass through the anion exchanger bed. Therefore, the anion removal reaction by the anion exchanger is promoted more than usual. Therefore, not only the removal ability of anion components containing carbonic acid, silica, or boron is improved, but also the removal ability of cationic components is improved, so the purity of the treated water will be further improved.
如上所述，宜以被處理水最後通過的離子交換體成為陰離子交換體之順序交替使用陽離子交換體床與陰離子交換體床。此非僅針對圖6所示之形態而言，亦為針對圖3、4所示之形態而言。 [實施例]As mentioned above, it is advisable to alternately use the cation exchanger bed and the anion exchanger bed in the order that the ion exchanger which the treated water passes last becomes the anion exchanger. This is not only for the configuration shown in FIG. 6, but also for the configuration shown in FIGS. 3 and 4. [Example]
[實施例1] 使用具有圖6所示之結構之EDI裝置，處理被處理水並獲得處理水(去離子水)。EDI裝置之規格及試驗條件如下所示。[Example 1] The EDI device with the structure shown in Fig. 6 was used to process the treated water and obtain treated water (deionized water). The specifications and test conditions of the EDI device are shown below.
另外，濃縮室22及24之規格、條件相同，且它們所獲得的濃縮水之規格、條件也相同。又，填充於陽極室21、第2小脫鹽室27之一部分(入口側區域)的陽離子交換樹脂(CER)相同。填充於陰極室25、濃縮室22、24、第1小脫鹽室26、第2小脫鹽室27之剩餘部分(出口側區域)的陰離子交換樹脂(AER)相同。陽離子交換膜31及33相同，陰離子交換膜32及34、以及中間離子交換膜36相同。In addition, the specifications and conditions of the
又，以下「縱」意指圖中沿紙面上下方向(沿水的行進方向之方向)，「橫」意指從紙面往深處方向。 ・槽室套組數(N)：1個 ・陽極室21：尺寸 縱100×橫100×厚度10mm，填充CER ・陰極室25：尺寸 縱100×橫100×厚度10mm，填充AER ・濃縮室22，24：尺寸 縱100×橫100×厚度10mm，填充AER ・第1小脫鹽室26：尺寸 縱100×橫100×厚度10mm，填充AER ・第2小脫鹽室27：尺寸 縱100×橫100×厚度10mm，填充CER(入口側1/2的區域)及AER(出口側1/2的區域) ・CER：強酸性陽離子交換樹脂 ・AER：強鹼性陰離子交換樹脂 ・陽離子交換膜31、33：均質膜，通電部有效膜尺寸 縱100×橫100mm，厚度290μm ・陰離子交換膜32、34及中間離子交換膜36：均質膜，通電部有效膜尺寸 縱100×橫100mm，厚度220μm ・陰離子交換膜40：均質膜，通電部有效膜尺寸 縱50×橫100mm，厚度220μm ・供給水及被處理水：2段RO(逆滲透膜)透過水，導電率2.0~2.5μS/cm ・處理水(去離子水)流量：25L/h ・濃縮水流量：6L/h ・電極水流量：5L/h(陽極、陰極相同) ・施加電流值：0.5A。In addition, the following "longitudinal" means the up and down direction along the paper in the figure (the direction along the direction of water travel), and "horizontal" means the direction from the paper to the depths. ・Number of tank chamber sets (N): 1 ・Anode chamber 21: Dimensions: length 100×width 100×thickness 10mm, filled with CER ・Cathode chamber 25: Dimensions: length 100×width 100×thickness 10mm, filled with AER ・Concentration chamber 22, 24: Dimensions: length 100×width 100×thickness 10mm, filled with AER ・The first small desalination chamber 26: Dimensions: length 100×width 100×thickness 10mm, filled with AER ・Second small desalination chamber 27: Dimensions: length 100×width 100×thickness 10mm, filled with CER (1/2 area on the inlet side) and AER (1/2 area on the outlet side) ・CER: Strong acid cation exchange resin ・AER: Strongly basic anion exchange resin ・Cation exchange membranes 31 and 33: homogeneous membrane, effective membrane size of the energized part length 100 × width 100 mm, thickness 290 μm ・Anion exchange membranes 32, 34 and intermediate ion exchange membrane 36: homogeneous membrane, effective membrane size of the energized part length 100 × width 100 mm, thickness 220 μm ・Anion Exchange Membrane 40: Homogenous membrane, the effective membrane size of the energized part length 50 × width 100mm, thickness 220μm ・Supply water and treated water: 2-stage RO (reverse osmosis membrane) permeable water, conductivity 2.0~2.5μS/cm ・Flow rate of treated water (deionized water): 25L/h ・Concentrated water flow rate: 6L/h ・Electrode water flow rate: 5L/h (anode and cathode are the same) ・Applied current value: 0.5A.
形成於第2小脫鹽室27之靠出口側1/2的區域之陰離子交換樹脂床之靠陰極側配置有第2陰離子交換膜40。此時，陽離子交換膜33之靠脫鹽室出口側端(沿紙面上下方向之上端)的位置和陰離子交換膜40之靠脫鹽室出口側端的位置對齊。又，陽離子交換膜33於橫向(從紙面往深處方向)的位置與陰離子交換膜40於橫向的位置對齊。The second
[比較例1]
未使用陰離子交換膜40。亦即第2小脫鹽室27與濃縮室24之間僅使用陽離子交換膜33。除此之外以和實施例1同樣的方式處理被處理水，並獲得處理水。[Comparative Example 1]
The
[比較例2]
使用陽離子交換膜替換第2陰離子交換膜40。該陽離子交換膜係和實施例1所使用的陽離子交換膜31、33為相同材質及厚度的膜，其縱橫尺寸及配置位置和實施例1所使用的第2陰離子交換膜40相同。除此之外以和實施例1同樣的方式處理被處理水，並獲得處理水。[Comparative Example 2]
The second
[評價1] 針對實施例1及比較例1、2，各別實施約500小時之連續運轉後，測定處理水中之總碳酸濃度(CO2 、H2 CO3 、HCO3 - 及CO3 2- 之濃度合計值)，並測定處理水的比電阻。結果如表1所示。總碳酸濃度係表示從濃縮室擴散至脫鹽室後，未完全去除而滲漏到處理水中之碳酸的濃度的指標。比電阻值則不限於碳酸，也包含其他離子，為處理水純度的的指標。[Evaluation 1] For Example 1 and Comparative Examples 1 and 2, the total carbonic acid concentration (CO 2 , H 2 CO 3 , HCO 3 - and CO 3 2-) in the treated water was measured after continuous operation for approximately 500 hours. The total value of the concentration), and measure the specific resistance of the treated water. The results are shown in Table 1. The total carbonic acid concentration is an index indicating the concentration of carbonic acid that has not been completely removed and leaked into the treated water after it diffuses from the concentration chamber to the desalination chamber. The specific resistance value is not limited to carbonic acid, but also includes other ions, which is an indicator of the purity of the treated water.
和比較例1、2相比，實施例1之碳酸的滲漏少，處理水純度高。Compared with Comparative Examples 1 and 2, the leakage of carbonic acid in Example 1 is less, and the purity of the treated water is high.
[表1]
[實施例2] 如下般變更條件，除此之外以和實施例1同樣的方式處理被處理水，並獲得處理水。 ・供給水及被處理水：2段RO(逆滲透膜)透過水，導電率4.0~4.5μS/cm ・施加電流值：1.0A。[Example 2] The conditions were changed as follows, except that the water to be treated was treated in the same manner as in Example 1, and treated water was obtained. ・Supply water and treated water: 2-stage RO (reverse osmosis membrane) permeable water, conductivity 4.0~4.5μS/cm ・Applied current value: 1.0A.
[實施例3]
使用異質陰離子交換膜作為第2陰離子交換膜40。該陰離子交換膜(異質)之縱橫尺寸及配置位置與實施例2所使用的第2陰離子交換膜40相同。又，該陰離子交換膜(異質)之厚度為580μm。除此之外以和實施例2同樣的方式處理被處理水，並獲得處理水。[Example 3]
A heterogeneous anion exchange membrane is used as the second
[比較例3]
使用雙極膜替換第2陰離子交換膜40。該雙極膜之縱橫尺寸及配置位置與實施例2所使用的第2陰離子交換膜40相同。又，雙極膜係以其陰離子交換膜部面向第2小脫鹽室27側的方式進行配置。雙極膜使用包含陰離子交換膜部與陽離子交換膜部之整體厚度為220μm者。除此之外以和實施例2同樣的方式處理被處理水，並獲得處理水。[Comparative Example 3]
The second
[評價2]
針對實施例2、3及比較例3，各別實施約500小時之連續運轉後，測定處理水中之總碳酸濃度、比電阻及鈉濃度，並測定電壓(陽極11與陰極12之間的電壓)、電流分配率。結果如表2所示。表中，「電流分配率 上」及「電流分配率 下」係分別如下般定義。
(電流分配率 上) = (流通於設置有第2陰離子交換膜40或雙極膜之區域的電流值)/(總電流值)，
(電流分配率 下) = (流通於陽離子交換膜33之未重疊有第2陰離子交換膜40或雙極膜之區域的電流值)/(總電流值)。[Evaluation 2]
For Examples 2, 3 and Comparative Example 3, after performing continuous operation for about 500 hours, respectively, the total carbonic acid concentration, specific resistance and sodium concentration in the treated water were measured, and the voltage (voltage between
電流分配率係將使用作為陰極12之陰極板以對應於上述區域的方式分成上下二個，分別以電流計測定上下陰極板中流通的電流值，並計算求得各電流值相對於施加的總電流值之比例。The current distribution rate is to divide the cathode plate used as the
和比較例3相比，實施例2之電流分配率之上下差小，處理水中的鈉濃度低，處理水之比電阻高。亦即，和比較例3相比，實施例2之脫鹽室內部之陽離子樹脂層中，電流分配較多，陽離子之去除良好，處理水之純度高。於實施例3中該傾向更大，處理水中的鈉濃度低，處理水之比電阻最高。如前所述，據認為異質膜由於具有部分不存在離子交換基之不活潑區域，故水解離反應不易進行，更會抑制電流集中於上側流通所致。Compared with Comparative Example 3, the current distribution rate of Example 2 is small, the sodium concentration in the treated water is low, and the specific resistance of the treated water is high. That is, compared with Comparative Example 3, the current distribution in the cation resin layer inside the desalination chamber of Example 2 is greater, the removal of cations is good, and the purity of the treated water is high. In Example 3, the tendency is greater, the sodium concentration in the treated water is low, and the specific resistance of the treated water is the highest. As mentioned above, it is believed that the heterogeneous membrane has some inactive regions where there are no ion exchange groups, so the hydrolysis reaction is not easy to proceed, and it is caused by preventing the current from being concentrated on the upper side.
[表2]
另外，依據本發明之結構，當脫鹽室內的被處理水進入陽離子交換膜33與陰離子交換膜40之間的界面時，該被處理水所含的弱酸成分會通過陰離子交換膜40而從該界面輕易地去除。另一方面，如比較例3般使用雙極膜替換陰離子交換膜40之結構，當脫鹽室內的被處理水進入陽離子交換膜33與雙極膜之間的界面時，將該被處理水所含的陰離子成分從該界面去除係為困難。原因乃陰離子成分的移動受到陽離子交換膜33與雙極膜的陽離子交換膜部兩者的阻止所致。結果陰離子會滲漏到處理水中造成水質的降低。In addition, according to the structure of the present invention, when the treated water in the desalination chamber enters the interface between the
例如圖10(b)所示，當陰離子及陽離子(圖中標記為「C+
A-
」)進入陽離子交換膜33與陰離子交換膜40之間的界面時，陰離子(圖中標記為「A-
」)會通過陰離子交換膜40而移動到脫鹽室23，並輕易被脫鹽室23內部的陰離子交換樹脂捕捉。陽離子(圖中標記為「C+
」)會通過陽離子交換膜33而從該界面被去除。另一方面，如圖10(a)所示，使用雙極膜50替換陰離子交換膜40之結構，雖然從陽離子交換膜33與雙極膜50之間的界面，陽離子(C+
)會通過陽離子交換膜33而被去除，但陰離子(A-
)既不會通過雙極膜50也不會通過陽離子交換膜33。結果，陰離子會從例如該界面的端部(圖10中沿紙面上下方向之上端)排出，並直接滲漏到處理水中。For example, as shown in Figure 10(b), when anions and cations (marked as "C + A - " in the figure) enter the interface between the
11‧‧‧陽極
12‧‧‧陰極
21‧‧‧陽極室
22‧‧‧濃縮室
23‧‧‧脫鹽室
23’‧‧‧脫鹽室
24‧‧‧濃縮室
24’‧‧‧濃縮室
25‧‧‧陰極室
26‧‧‧第1小脫鹽室
27‧‧‧第2小脫鹽室
31‧‧‧陽離子交換膜(CEM)
32‧‧‧第1陰離子交換膜(AEM)
32’‧‧‧第1陰離子交換膜(AEM)
33‧‧‧陽離子交換膜(CEM)
33’‧‧‧陽離子交換膜(CEM)
34‧‧‧陰離子交換膜(AEM)
36‧‧‧中間離子交換膜(IIEM)
40‧‧‧第2陰離子交換膜(AEM)
40’‧‧‧第2陰離子交換膜(AEM)
50‧‧‧雙極膜
50a‧‧‧陰離子交換膜部
50c‧‧‧陽離子交換膜部
51‧‧‧陰離子交換樹脂11‧‧‧
[圖1]係顯示本發明之EDI裝置的一形態之概略結構之剖面示意圖。 [圖2]係顯示圖1所示之裝置中，重複數N為2時的例之概略結構之示意剖面圖。 [圖3]係顯示本發明之EDI裝置的另一形態之概略結構之示意剖面圖。 [圖4]係顯示本發明之EDI裝置的又一形態之概略結構之示意剖面圖。 [圖5]係顯示本發明之EDI裝置的又另一形態之概略結構之示意剖面圖。 [圖6]係顯示本發明之EDI裝置的又再另一形態之概略結構之示意剖面圖。 [圖7](a)、(b)係用以說明本發明的機制之概念圖。 [圖8]係用以說明在陽離子交換膜與陰離子交換膜重疊的界面中的水解離機制之另一概念圖。 [圖9]係用以說明在雙極膜中的水解離機制之概念圖。 [圖10](a)、(b)係用以說明陰離子及陽離子從二片膜重疊的界面排出的狀況之概念圖。[Fig. 1] is a schematic cross-sectional view showing a schematic structure of one form of the EDI device of the present invention. [Fig. 2] A schematic cross-sectional view showing the schematic structure of an example when the number of repetitions N is 2 in the device shown in Fig. 1. [Fig. [FIG. 3] A schematic cross-sectional view showing the schematic structure of another form of the EDI device of the present invention. [FIG. 4] A schematic cross-sectional view showing the schematic structure of another form of the EDI device of the present invention. [FIG. 5] A schematic cross-sectional view showing the schematic structure of yet another form of the EDI device of the present invention. [FIG. 6] A schematic cross-sectional view showing the schematic structure of yet another form of the EDI device of the present invention. [Figure 7] (a) and (b) are conceptual diagrams for explaining the mechanism of the present invention. [Figure 8] is another conceptual diagram for explaining the mechanism of hydrolysis at the interface where the cation exchange membrane and the anion exchange membrane overlap. [Figure 9] is a conceptual diagram to illustrate the hydrolysis mechanism in the bipolar membrane. [Fig. 10] (a) and (b) are conceptual diagrams for explaining the discharge of anions and cations from the interface where two membranes overlap.
11‧‧‧陽極 11‧‧‧Anode
12‧‧‧陰極 12‧‧‧Cathode
21‧‧‧陽極室 21‧‧‧Anode Room
22‧‧‧濃縮室 22‧‧‧Concentration Room
23‧‧‧脫鹽室 23‧‧‧Desalination Room
24‧‧‧濃縮室 24‧‧‧Concentration Room
25‧‧‧陰極室 25‧‧‧Cathode Chamber
31‧‧‧陽離子交換膜(CEM) 31‧‧‧Cation exchange membrane (CEM)
32‧‧‧第1陰離子交換膜(AEM) 32‧‧‧The first anion exchange membrane (AEM)
33‧‧‧陽離子交換膜(CEM) 33‧‧‧Cation Exchange Membrane (CEM)
34‧‧‧陰離子交換膜(AEM) 34‧‧‧Anion Exchange Membrane (AEM)
40‧‧‧第2陰離子交換膜(AEM) 40‧‧‧Second Anion Exchange Membrane (AEM)
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TW200922881A (en) * | 2007-11-23 | 2009-06-01 | Ind Tech Res Inst | Electro-deionization water purification system |
| CN101454067A (en) * | 2006-06-02 | 2009-06-10 | 通用电气公司 | Method and apparatus for shifting current distribution in electrodeionization systems |
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| CN100345615C (en) * | 2005-09-12 | 2007-10-31 | 张贵清 | Electric deionisation method and apparatus for producing superpure water using bipolar membrane |
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| EP2578543B1 (en) | 2010-06-03 | 2017-03-01 | Organo Corporation | Electric device for production of deionized water |
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