201249527 六、發明說明： 【發明所屬之技術領域】 【_】 本發明係關於電氣式去離子水製造裝置，尤其關於除鹽室 構造。 孤 【先前技術】 【0002】 以往’已知有種去離子水製造裝置係使被處理水通過離 ΪΪί進行祕子。此種製造裝置巾，#離子交換體的離子交換 土釭和而除鹽性能降低時，必須藉由酸或鹼之藥 、 換基之再生。具體而言’必須進行藉由來自酸或 來^換離子交絲所吸_陰軒《騎子之處理。近年 述運轉上的缺點，已·出—種電氣私離子水製造f 置並貫用化，無須藥劑進行再生。 裝 【0003】 電氣式去離子水製造裝置係結合電泳法與電析法 :士式去籽水製造裝置之基本構成如下所^ 陽極室，配置於一側的濃縮室外側;以及g極室亥除鹽 ί 與ί 離室 表le裒置簡％為「去離子水製造裝 哪丁不 【0004】 係在成的去離子水製造裝置來製造去離子水時， Ϊ _加於分別設在陽極室及陰極室的雷^夕丄 下’使被處理水通過降趟玄。a酿—占— 兒極間之狀態 陰離子成分(cr，子交換體捕捉 捉陽離子成分(Na+，ca2+，Μ 23+#)纟）’，由陽離子交換體捕 Q，Mg專）。问時，在除鹽室内陰離子交 201249527 交界面產生水的解離反應，而產生氫離子 iiif，藉由在濃縮室流動的水來·。 離述’電4式去離子水製造裝置巾，氫離子與氫氧招 此，基ίίΐϊ 的再生劑(酸或驗)而連續發揮作用^ 運轉。本一員上述由樂劑所進行的離子交換體再生，而可連續 【0006】 出八ί去離子水製造裝置連續運轉時，處理水中的硬声 ，刀析出而產生碳酸域氫氧化料結垢。結垢尤 二 ΐίίΪίΐίΪ行分隔的陰離子交換膜的濃縮室側表面。又： 膜表面ΪΪΓ士 鹽室f包夹的濃縮室的陰離子交換 的陰離子交換膜表面成為驗性。二 有碳酸離子時，S碳;或; 電流難以流通。亦即，ίΐ二;;i :垢知的相同電流値’必須提高電壓，導致 ^ $生 ，些情況下濃縮室_電流密度也魏 Ί丄 =:產生通權上昇並且電阻以此ΐ 2 二去除滩子所必要的電流，導致處理二 的結垢侵入到離子細^ 所以’就抑制如上所述結垢產生的方法之—而言，有種提案 201249527 ίίί離子交換體填充於濃縮⑼。例如，專敝獻1揭示有一 祕她製造裝置’將特定構造的陰軒交換體配置於濃縮室 .^ 父換膜側_。依據此去離子水製造褽置，多孔性陰離子交 面麄促$ 〇Η~往漢縮水的擴散稀釋，而達到快速降低該表面 六·丄度。另—方面，硬度成分離子難以侵入到多孔性陰離子 =、體=部。其結果，。Η-與硬度成分離子減觸 減少，抑制結垢的析出貨累積。 叹曰 【0008】 内*2中揭示有—種去離子水製造裝置，在濃縮室 離二ίί水性不同的離子交換體層，且將透水性較小的 =姆面具有陰離 ，並含有多量硬度置到 =離子交換膜的濃縮室側表面，抑制結垢析出t積&水w 【先前技術讀】 【專利文獻】 【0009】 專利文獻1 :日本特開2001-225〇78號公報 專利文獻2 :日本特開2002-1345號公郝 【0010】 但是，去離子水製造裝置中，即使 响 交換體來避免結垢產生，也會產生與:=2至填充陰離子 以濃縮水所含的碳酸或矽酸為代表，@ ^不同的下述問題。 縮室與除鹽室進行分隔的離m膜成分通過對於濃 理水的純度降低。此種處理水的純度降^月直，得處 =體之情況表現得更為顯著。以下，以碳 【0011】 -般而言，陽離子交換膜係選擇性只讓陽離子穿透的離子交 ⑧ 201249527 換膜。其原理為，膜本身具有一（負）電荷，對於具〜 子施加反作用力來阻止穿透。另—方、二？电何的陰_ 水溶液中成為各離子種的形態，其位於平^能*石反)或石夕酸在 C02<^HC〇3_〇C〇32' ^201249527 VI. Description of the invention: [Technical field to which the invention pertains] [_] The present invention relates to an electric deionized water producing apparatus, and more particularly to a desalting chamber structure. [Prior Art] [0002] Conventionally, there has been known a deionized water producing apparatus for allowing a water to be treated to pass through a crucible. Such a manufacturing device, the ion exchange body of the ion exchanger, and the demineralization performance must be regenerated by acid or alkali. Specifically, it must be carried out by the acid or the exchange of ion-crossing wire. In recent years, the shortcomings of the operation have been made, and the production of electrical private ionized water has been used and it has not been regenerated. [0003] The electric deionized water manufacturing device is combined with the electrophoresis method and the electrolysis method: the basic structure of the stone-type seed water manufacturing device is as follows: the anode chamber is disposed on one side of the concentrated outdoor side; Desalination ί and ί 离 为 为 去 去 去 去 去 去 去 去 去 去 去 去 去 去 去 去 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 0004 The chamber and the cathode chamber are under the thunder, and the water to be treated passes through the descending sputum. A brewing-occupying - the state of the anion component (cr, the daughter exchange captures the cationic component (Na+, ca2+, Μ 23+) #)纟)', Q is captured by the cation exchanger, and Mg is used. When asked, the dissociation reaction of water is generated at the interface of the anion exchange 201249527 in the desalting chamber, and the hydrogen ion iiif is generated by the water flowing in the concentration chamber. · Departure 'Electrical 4 type deionized water manufacturing device towel, hydrogen ion and hydrogen oxygen, this is the continuous revitalizer (acid or test) and the continuous operation ^ operation. The above-mentioned ions by the agent The exchange body is regenerated, and it can be continuously [0006] When the manufacturing apparatus is continuously operated, the hard sound in the water is treated, and the knife is precipitated to cause scaling of the carbonic acid hydroxide hydroxide. The fouling is particularly concentrated on the side surface of the concentrating chamber of the anion exchange membrane. The anion exchanged anion exchange membrane surface of the concentrating chamber of the double clamp is inspective. When there are carbonate ions, S carbon; or; the current is difficult to circulate. That is, the same current 値 ' must be improved The voltage causes the voltage to be generated. In some cases, the concentration chamber _ current density is also WeiΊ丄 =: the right weight rises and the resistance is used to remove the necessary current from the beach, causing the scale of the treatment 2 to invade the ions. ^ So, in terms of the method of inhibiting the generation of scale as described above, there is a proposal 201249527 ίίί ion exchanger filled in the concentration (9). For example, the special offer 1 reveals that there is a secret she made the device 'will be a specific structure of Yin Xuan The exchange body is arranged in the concentrating chamber. ^ The parent is changing the membrane side _. According to the deionized water manufacturing device, the porous anion interface promotes the diffusion and dilution of the condensed water to the Han shrinkage, and the rapid reduction is achieved. On the other hand, it is difficult for the hardness component ions to intrude into the porous anion = and the body = part. As a result, the Η-and hardness component ions are reduced in contact, and the deposition of scale is suppressed. [0008] The invention discloses a deionized water manufacturing device, which is different from the aqueous ion exchange layer in the concentrating chamber, and has a lower permeability and a negative surface, and contains a large amount of hardness. = the surface of the concentrating chamber of the ion exchange membrane, and the inhibition of scale deposition, the product, and the water w. [Patent Document] [Patent Document 1] Patent Document 1: JP-A-2001-225〇78 Patent Document 2: Japanese Patent Laid-Open No. 2002-1345 [0010] However, in the deionized water production apparatus, even if the exchanger is exchanged to avoid scale formation, it will produce:==2 to fill the anion to concentrate the carbonic acid or cesium contained in the water. Acid is representative, @^ differs in the following questions. The m film component separated from the demineralization chamber by the condensing chamber is reduced in purity by the concentrated water. The purity of this treated water is reduced to a straight line, and the situation of the body is more pronounced. Hereinafter, carbon is used. [0011] In general, the cation exchange membrane system selectively exchanges only the cation-penetrating ion exchange 8 201249527. The principle is that the membrane itself has a (negative) charge, and a reaction force is applied to the stem to prevent penetration. Another - square, two? The form of each ion species in the aqueous solution _ _ _ _ _ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^ ^
Si〇2 ㊁ Si(0H)4<^Si(0H)30 一 【0012】 上述平衡狀態中，各離子種於全體中所佔比例係 =荷:^分未離子化，亦即在 【0013】 因此，即使欲在pH較低區域採用陽離子交換 ，也因為-電朗反個===== 此等为子將容易地通過陽離子交換膜。 斤 【0014】 ' 、 換膜3 °除鹽室D的陰極側隔著陽離子交 =在此，除鹽室D填充有陽離子交換體及陰交 填充有陰離子交換體。處理水通過除鹽排ί 【0015】 攸除鹽室D朝向濃縮室C2並與被處理 應產生的多量氫離子(Η+)，在陽離子 'fΛ /辰縮至C2填充有陰離子交換體，所以 子 子交換膜的濃縮室側表面— 低狀月縮室Ϊ表面成為氯離子(Η+)較多狀態(亦即ΡΗ Ϊ 酸亦_離子的形式受到濃縮室 ϊίΧ cf 子交換體内移動直到陽離子交換膜:面。 辰、％至C2的1%離子交換膜表面，碳酸或矽酸的 古 ρ變低。就結果而言，在ρΗ較低條件下不離子化的碳酸， 201249527 從陰離子交換體遊離之後失去電荷，將穿透陽離子交換膜而擴 至被處理水。 、 【0016】 冬又二圖7所示的去離子水製造裝置設有2個除鹽室(D1、D2)。 $女此〔又有夕數之除鹽至時，在濃縮水原本所含的碳酸或梦酸之 外，連被處理水所含的碳酸或矽酸也從除鹽室移動來濃縮室。所 =，濃縮室内令的碳酸或石夕酸之濃度上昇，往除鹽室混入所 二，水純度降低變得更加顯著。（财顯示為碳酸，但就树而言 【發明内容】 【0017】 )17] 水。本發明之目的在於可抑制結垢產生並且製造高純度的去離子 【_】 本發明的一態様係一種電氣式去離子水萝 ΪΪΞί與陽極室之間設有至少1個除鹽處理部 猶鹽處理部係由除鹽室及成對之濃縮㈣成，該 ，於該除鹽室的兩鄰並且填充有陰離子交換體，^心二、= 離子交換臈而分隔成：第丨 皿至係猎由 -者:以及第2小除鹽室二二===室的 第1小除财填充有陰離子交換體，除纟 ，3亥 最後所通過的離子交換體係陰離子交換體之理水 換體與陽離子交換體，填充於該第2小除趟室？ 2離子交 :陰極侧配置有雙極性膜以陰離子交換膜:與該陰 【0019】 在此除鹽室係分隔成2室，但離子的舉 — 室時基本上相同。 動，、除凰至未分隔的1 【0020】 201249527 λ、八様中，存在於陰極側的濃縮室之碳酸或矽酸等陰離子 孑二八；'丨：，過離子交換膜而往第2小除鹽室移動時，該陰離 /丨、|^二^β小除鹽室内的陰離子交換體所捕捉，並經由第1 二1侧的濃縮室。所以，存在於濃縮室的石炭酸或石夕 i並杏規二ϊΐ理水中。又，藉由雙極性膜來促進水的解離反 應並戶 '現電流密度的適恰分配。 [0021] 垢產生並製式去離子水製造裝置，可抑制結 【實施方式】 【0023】 (實施形態1) 態的ϋ純圖式5調本發明之電氣式去軒水製造裝置實施形 【0024】 …戶科賴紗_德構成圖。 陽搞的陪托—子尺衣置中，於具有陰極的陰極室E1與具有 極至E2之間，設有除鹽室D，以及由配置於㈣室1)兩 ==室C1、C2所構成的除鹽處理部。ΤΑ月中: 1濃縮ία至上=2之中鄰接於陽極室E2的濃縮室α稱為「第 C2」來⑤別於f極室E1的濃縮室C2稱為「第2濃縮室 【〇〇2^ 別僅係便於說明的區別。 八f:除鹽室D分隔成二個小除鹽室。具體而t，除趟室D ，成鄰接於第i濃縮室C1的第 聪而二S3 2濃縮室C2的第2小除趟室D|。J除並至D-1 ’以及鄰接於第 Γ0026] 換膜應1的内部藉由多數之離子交 成夕數之工間所形成，並隔著離子交蹲膜而相鄰接。從 201249527 陰2 依照順序說明各室的排列狀況時如下所述。亦即 著第1陰離子交換膜al而鄰接於第2濃縮室C2，第； ^ ^ =著第1陽離子交換膜Cl與第2小除鹽室D_2相鄰接。 ί ^ D_2隔著第2陰離子交換膜a2與第1小除鹽室 ί 除鹽室D_1隔著第3陰離子交換膜a3與第1濃縮 ^2相鄰^接。第1濃縮室C1隔著第2陽離子交賴e2與陽極室 [0027] 為「中間U ^ 弟除鹽室D_2的陰離子交換膜稱 僅係便於一與其_子交換膜進行區別。此種區別 【0028】 播冰陰Ϊί 3收容有陰極。陰極係由金屬的網狀體或者板狀體所 抗氯性能的材料，就立一^產與生/孔°因此’陽極宜採用具有 者以此等金屬包覆=材Γ吕’舉例如有翻、免、銀等金屬或 [0030] 陰極室Ε1及陽極室Ε2分別供仏 電極附近電解而產生氫離子及盘極f。使此寺電極水在 造裝置的電阻，陰極ίΓ及去離子水製 者，陰極室E1更宜填充有弱驗性陰離子交換。再 © 10 201249527 "ϋΓ單床鄉填充有_結缝生的_子交換體。 除鹽ί 放大圖。如圖2所示’第！小 陽離子交換體及陽離子交換體。具體而言， 二盆;:二二前段二置有陽離子交換體層而通“ 被處理水佑日子乂換版層。亦即，流入第2小除鹽室D_2的 之，在第2 ^序Ϊ過陽離子交換體層與陰離子交換體層。換言 声係Ρ離子Μ係以被處理水最後所通過的離子交換體 ▲層Γ ^“相順序疊層有陰軒交換體層與陽離子交換 【0033】 笛9再除鹽室Μ配置有雙極性膜。具體而言，係於 __陰離子交換體(陰離子交換體層)與第‘ 1 嘈^Cl之間配置有雙極性膜如。在此，雙極性膜係指陰 US，陽離子交換膜相貼合而—體化的離子交換膜，且具 :I,子乂換膜與陽離子交換膜的接合面極度促進水的解離反 ^ΐΪΪ °如圖2所示，雙極性膜4a U其陰離子交換膜2與陰離 子父換肢(陰離子交換體層)相向的方向配置。 【0034】 々再芩照圖1。圖1中，框架體1係一體顯示。其中，實際上係 每，房間具有分別的框架體，框架體彼此緊接設置。框架體1只 ，疋具有絕緣性且不會洩漏被處理水的材料即可，並無特別限 定’舉例可如有聚乙烯、聚丙烯、聚氣乙烯、、聚碳酸酯、 m-PPE(改性聚苯峋等樹脂。 【0035】 + 在此’為使本發明的理解更加容易，預先解說圖1所示的去 離子水製造裝置中被處理水及濃縮水的主要流動。被處理水通過 RO(Reverse Osmosis ’逆滲透)膜之後供往第1小除鹽室D-1，並通 11 201249527 、除鹽室叫。通過第1小除鹽室D-1的被處理水係供給至 =除鹽^ D_2，並於通過該小除鹽室D_2之後排出至系統外。 面”農縮水分別平行供給至第丨濃縮室α及第2濃縮室 【οοί】通過此咖室㈣出至系統外。 π 1 ία了如上所述地使被處理水及濃縮水流動而設有數個流道 TT1 了#、y〜L2。圖1中，去離子水製造裝置上方所示的流道 —n連接於被處理水的供給側，另—端連接於第1小除鹽 i子水製造裝置下方所示的流道1^，其一端連接於第 P至二1 ’另一端連接於第2小除鹽室D_2。去離子水製造 端連接於端連接於第2小除鹽室D·2 ’另一 【0037】 於濃m供ifri製造裝置上方所示的流道u3，其-端連接 途中分歧而分別連接於第i濃縮 別連接;。錄子水製造裝訂稍示的流道〔2分 室ci、第2濃縮室《，在途中匯流之後連接至 【0038】 另’雖省略圖不，但险;)¾它·ρ Ί π β 繁】明具有上述構成的去離子水製造裝置之動作及作用。 ί : ί=t 係_ 流 極水，並從未圖示的益道排出^至E2=未圖示的流道供給電 家有既定的直流電壓。 +水。再者’陽極、陰極之間施 【0040】 室 ⑧ 12 201249527 • f水通過第1小除鹽室m㈣程受到捕捉。並 室仏1執敝的陰離子成分往與第1小除i ίοοίΓ ㈣縮水制排出至系統外。 Μ ΐΐ ’,1 過第1小除鹽室D_1的被處理水，經由流道L1而# ^至弟2小除鹽室D_2。在此，如上所述，第2小除 =Si〇2 II Si(0H)4<^Si(0H)30 [0012] In the above equilibrium state, the proportion of each ion species in the whole system is = ion: ^ is not ionized, that is, in [0013] Therefore, even if cation exchange is to be employed in a lower pH region, it is easy to pass through the cation exchange membrane because it is a =====. [0014] ', the membrane side of the 3° demineralization chamber D is separated by a cation. Here, the desalting chamber D is filled with a cation exchanger and the anion is filled with an anion exchanger. The treated water passes through the desalting line. [0015] The salt removing chamber D is directed toward the concentrating chamber C2 and is subjected to a large amount of hydrogen ions (Η+) to be produced, and the cation 'fΛ/chen is reduced to C2 to be filled with an anion exchanger, so The concentrating chamber side surface of the sub-exchange membrane - the surface of the low-profile swell chamber becomes a state of more chloride ion (Η+) (that is, the form of ΡΗ 亦 亦 _ ions is moved by the concentrating chamber ϊ Χ 交换 sub-exchange to the cation Exchange membrane: surface. The surface of the 1% ion exchange membrane with 9%, % to C2, the ancient ρ of carbonic acid or citric acid becomes low. As a result, the non-ionized carbonic acid under the condition of lower ρΗ, 201249527 from the anion exchanger After the free, the charge is lost, and the cation exchange membrane is penetrated to be expanded to the treated water. [0016] The deionized water production apparatus shown in Fig. 7 of the winter and the second is provided with two desalting chambers (D1, D2). In addition to the carbon dioxide or the dream acid contained in the concentrated water, the carbonic acid or tannic acid contained in the treated water is also moved from the desalting chamber to the concentration chamber. The concentration of carbonic acid or linalic acid in the concentrated chamber is increased, and the concentration in the desalting chamber is mixed. The reduction in water purity becomes more remarkable. (The money is shown as carbonic acid, but in terms of trees [invention] [0017] 17] Water. The object of the present invention is to suppress scale generation and to produce high-purity deionization [_ The first aspect of the present invention is characterized in that at least one desalination treatment portion is provided between the electric deionized water and the anode chamber, and the salt treatment chamber is concentrated by the desalting chamber and the pair is concentrated (four). The two sides of the desalination chamber are filled with an anion exchanger, and the two are separated by the ion exchange enthalpy: the first dish to the hunter--: and the second small desalting chamber two two === the chamber 1 small depletion filled with an anion exchanger, in addition to sputum, 3 Hai finally passed the ion exchange system anion exchanger water exchange and cation exchanger, filled in the second small mites? 2 ion exchange: cathode The side is provided with a bipolar membrane to anion exchange membrane: and the cathode [0019], wherein the desalting compartment is divided into two chambers, but the ions are substantially the same in the chamber - moving, removing the phoenix to the undivided 1 0020] 201249527 λ, gossip, present in the concentrating chamber on the cathode side An anion such as carbonic acid or citric acid; 丨: when the ion exchange membrane is moved to the second small desalination chamber, the anion exchanger in the anion/丨, ^2^β small desalination chamber is captured. And passing through the concentrating chamber on the 1st and 1st sides. Therefore, it exists in the concentrating chamber of carbolic acid or shixi i and apricot syrup. In addition, the bipolar membrane promotes the dissociation reaction of water and the current [0021] The scale generation and preparation of the deionized water manufacturing apparatus can suppress the knot [Embodiment] [0023] (Embodiment 1) The state of the pure figure 5 adjusts the electric type of the invention Manufacturing device implementation form [0024] ... household Kolai yarn _ German composition map. The accompaniment of the mascot is centered, between the cathode chamber E1 having the cathode and the pole to E2, with the desalting chamber D, and by the chamber (1) 1) == chambers C1, C2 A desalination treatment unit. In the middle of the month: 1 Concentration ία up to 2 is equal to the concentrating chamber α of the anode chamber E2, which is called "C2". The concentrating chamber C2, which is different from the f-chamber E1, is called "the second concentrating chamber [〇〇2 ^ Don't just make it easy to explain the difference. Eight f: The desalting chamber D is divided into two small desalting chambers. Specifically, t, except for the diverticulum D, becomes adjacent to the i-th concentrating chamber C1, and the second S3 2 is concentrated. The second small mites room D| of the chamber C2 is diverged to D-1 'and adjacent to the Γ 0026.] The inside of the membrane change 1 is formed by a plurality of ionic intersections, and is interposed. The ion exchange film is adjacent to each other. From 201249527, the negative arrangement of each chamber is described in the following order, that is, the first anion exchange membrane a1 is adjacent to the second concentration chamber C2, and the ^^ = The first cation exchange membrane C1 is adjacent to the second small desalting compartment D_2. ί ^ D_2 is separated from the first small desalination compartment ί by the second anion exchange membrane a2, and the third anion exchange membrane a3 is interposed between the desalination compartment D_1 and The first concentration chamber 2 is adjacent to each other. The first concentration chamber C1 is separated from the second chamber by the second cation e2 and the anode chamber [0027], and the anion exchange membrane of the intermediate U ^ brother desalination chamber D_2 is said to be convenient for one. Sub-exchange Make a difference. This difference [0028] broadcast ice Ϊ ί 3 contains a cathode. The cathode is made of a metal mesh or a plate-like material that resists chlorine, and the material is produced and produced. It is preferable to use such a metal coating = material Γ ' 举 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 例如 阴极 阴极 阴极 阴极 阴极In order to make the electrode water of the temple in the resistance of the device, the cathode and the deionized water, the cathode chamber E1 is preferably filled with a weak anion exchange. © 10 201249527 "ϋΓ单床乡有有_结缝生_ sub-exchange body. De-salt ί magnified view. As shown in Figure 2 'the first small cation exchanger and cation exchanger. Specifically, two pots;: two second anterior two cation exchange layer and pass Handle the water to the day. That is, the second small desalination chamber D_2 flows into the second cation exchange layer and the anion exchanger layer in the second step. In other words, the sound system Ρ ion Μ is the ion exchange body ▲ layer 最后 finally passed by the treated water. “The phase sequence is laminated with the Yinxuan exchange body layer and the cation exchange [0033] The whistle 9 and the salt removal chamber are equipped with a bipolar membrane. Specifically, a bipolar membrane is disposed between the __ anion exchanger (anion exchanger layer) and the first 嘈^Cl. Here, the bipolar membrane refers to the yttrium US, and the cation exchange membrane is attached. And the ion exchange membrane of the body, and has: I, the joint surface of the sub-exchange membrane and the cation exchange membrane greatly promotes the dissociation of water. As shown in Fig. 2, the bipolar membrane 4a U has an anion exchange membrane 2 Arranged in the direction opposite to the anionic parent limb (anion exchanger layer). [0034] Referring again to Figure 1. In Figure 1, the frame body 1 is shown in one piece, wherein, in fact, each room has a separate frame body, The frame bodies are disposed next to each other. The frame body 1 only has a material that is insulating and does not leak the water to be treated, and is not particularly limited. For example, polyethylene, polypropylene, polyethylene, and polycarbonate may be used. Ester, m-PPE (modified polyphenyl hydrazine and other resins. [0035] 】 + Here, in order to make the understanding of the present invention easier, the main flow of the treated water and the concentrated water in the deionized water production apparatus shown in Fig. 1 is explained in advance. The treated water passes through the RO (Reverse Osmosis ' reverse osmosis) membrane. After that, it is supplied to the first small desalting chamber D-1, and is connected to 11 201249527, and the desalting chamber is called. The treated water supplied through the first small desalting chamber D-1 is supplied to = demineralized ^ D_2, and passes through the After the small demineralization chamber D_2 is discharged to the outside of the system, the surface shrinkage water is supplied to the third enrichment chamber α and the second enrichment chamber in parallel [οοί] through the coffee chamber (4) to the outside of the system. π 1 ία is as described above. The flow of water to be treated and the concentrated water are flowed to provide a plurality of flow paths TT1, #, y to L2. In Fig. 1, the flow path - n shown above the deionized water production apparatus is connected to the supply side of the water to be treated, and - The end is connected to the flow channel 1^ shown below the first small desalination i sub-water production device, and one end thereof is connected to the Pth to the second 1' and the other end is connected to the second small desalting chamber D_2. The deionized water manufacturing end is connected. Connected to the second small desalting chamber D·2 'the other end [0037] in the concentrated m for the flow shown above the equipment U3, the end-to-end connection is diverged and connected to the i-th concentrating connection respectively. The recording water is bound to the flow channel (2 sub-chamber ci, 2nd concentrating room ", connected to [0038] after confluence on the way 'Although the figure is omitted, it is dangerous;) 3⁄4 It·ρ Ί π β 繁繁] The operation and action of the deionized water producing apparatus having the above configuration. ί : ί=t _ Flow 极 极 , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , , + water. Furthermore, between the anode and the cathode [0040] Room 8 12 201249527 • f water is captured by the first small desalination chamber m (four). And the anion component of the chamber 1 is discharged to the outside of the system with the first small division i ίοοίΓ (4). Μ ΐΐ ', 1 The treated water passing through the first small desalting chamber D_1 passes through the flow path L1 and reaches the salt chamber D_2. Here, as mentioned above, the second small division =
ΪΚίΐΐ陽離子交賴層與陰離子交換體層。所以，供給至、 通過馳處财，首先通過陽料交換體層，其後 被严體層。此時’在通過陽離子交換體層的過程中， f處子成分_+，Ca2+，吨2+鞭賴捉。具體而 二ίϋ 室D_2内的陽離子交換體受到捕捉的陽離子I ‘二二广小除鹽tD_2隔著第1陽離子交換膜cl而相鄰接的 移動，與通人該第2濃縮室C2的濃縮水共同排出 【0042】 在、H2j、除鹽f M通過陽離子交換體層的被處理水， = 子交換體層的過程巾，陰離子成分(c「，c〇32-， fiC03 ’ SA等)再度受到捕捉。具體而言，在第2小 的陰離子交換體受到她着離子成分，往與第2D 2 隔者中間離子交換膜a2而相鄰接的第Η、除鹽室叫移ς 1小除鹽室D-1移動的陰離子成分，往與第】小除 a3曲而相鄰接的第1濃縮室C1 “，並與i人 忒弟1浪鈿至C1的濃縮水共同排出至系統外。 【0043】 以^本實施形態之去離子水製造裝置巾的去離子處理之流 私。但是，上述處理過程中，供給至第2濃縮室C2的濃縮水 的陰離子成分(碳酸或矽酸)的一部分通過第丨陽離子 第2小除鹽室D-2移動。碳酸或魏通過陽離子交換膜的原 如前所述。在此，從第2濃縮室C2往第2小除鹽室於移^的碳 13 201249527 ί或：或;二上擴散。亦 ===陽離體層=== ί，所兔酸或魏未受到陽離子交換體所捕 Ϊ搞第 子交換膜ei的陽極侧表面之中與陽離子 陽離子交換體層。但是，第G除=====而通過 方向疊層有陽料交触層與陰離子 ^7的通水 :交換體層的碳酸或魏，在下一段的陰“交斤二 ==往第1小除鹽室w移動。_第=2= 的=或:夕酸通過苐3陰離子交換膜幻而往第i漠縮室二_， 通人該第1濃縮室C1的濃縮水共_出至纟、餅以夕，， Ϊ::，的碳酸及術會擴散至被處理水中而使得處理水‘ 【0044】 層之;内的陽離子交換體層與陰離子交換體 =::=:==到第1陽離子交換膜以‘ 度降低，此點顯然不言而^。域的石厌酸或石夕酸，處理水的純 【0045】 依據目刖為止的說明，應可理解，口 所設的離子交換體之疊層體的最$ D-2内 上述效果。換言之，只f f離子父換體層即可獲得 所通過的離子交換體伟吟離早_^矛、皿至D-2的被處理水最後 士吾士 =于又換體係陰離子父換體即可獲得上述效果。所以， 離子交換，更前段的離子交換體層之種ί、g順 子交’亦可將陽離子交換體層與^離' 【0046^最末為陰父換體層的順序疊層4層以上。 再者，本實施形態之去離子水劁 給的第1小除鹽室W埴充5离^：2中，ΐ處理水最初供 ^ "凡有u離子父換體，被處理水其次供給 14 201249527 ^第2小除鹽室D_2依照順序疊層麵離子交換體與陰離 月二。所以，被處理水最初通過陰離子交換體。藉此從被處理中 去除陰離子成分，使得被處理水的pH上昇。 【0047】 再者，通過第1小除鹽室ΓΜ的被處理水供給至依照順 層有陽離子交換體與陰離子交換體的第2小除鹽室D_2。亦即，= J第上小除鹽室D-1内之陰離子交換體的被處理水，接著通 $子父換體’其次再錢過陰離子交換體。重點在於，依據本杏 構成’被處理水交互通過_子交換體與陽離子交換體二 ί ’陰離子交換體在被處理水的PH較低時對於陰離子成分 勺捕^能力較高’陽離子交換體在被處理水的pH較高時對於陽離 施^刀的捕捉此力較咼。所以，依據被處理水最初通過陰離子交 二其？交過陽離子交換體與陰離子交換體的本實施形態 冓成’藉由通過陰離子交換體而去除_子成分，ρΗ上昇的^ ^水接著通過陽料交频。所以，比平常更加促進陽離子交 離子去除反應。再者，藉由通過陽離子交換體而去 jT離千f分’ρΗ降低的被處理水接著通過陰離子交換體。所 =僅11平^更加促進陰離子交換體所致的去除陰離子反應。所以， 担加提升對於含有碳酸或魏的_子成分之絲能力，亦 度升對於轉该分之去除能力，卿更進—步提升處理水的純 【0049】 防上所述，依據本實施形態之去離子水製造裝置，在藉由 很細水所含的碳酸或矽酸的一部分通過離子交換膜並擴散至 處ί:::的二=理水的純度之效果外，還加上提升對於被 料反酸或矽酸等陰離子成分之去除能力，再者亦提升 里水所含的陽離子成分之去除能力。 -、人。兑明在除鹽室D配置雙極性膜4a的意義。去離子水製造 15 201249527 裝置中’藉由電而解離的水發揮出作為離子交換體再生劑之功 能，此點已如上述。在此，施加於去離子水製造裝置的電壓的大 部分係利用於水的解離反應。所以，為了實現在低電壓、高電流 雄、度下的運轉，宜促進水的解離反應。此點，在除鹽室D配置有 雙極性膜4a的本實獅態之麵子水製造裝置巾，促進水的解離 反應，可進行在低電壓、高電流密度下的運轉。 【0051】 …—个只她形悲之去離子水製造裝置中，促進水的解離/ 心之雙極⑽4a僅配置於第2小除鹽 離子交換膜(陽離子交換膜cl)之間。換言之，第2小除ΪΚίΐΐ cation intersection layer and anion exchanger layer. Therefore, the supply to, through the wealth, first through the cation exchange body layer, and then the body layer. At this time, in the process of passing through the cation exchanger layer, the f component _+, Ca2+, ton 2+ lashing. Specifically, the cation exchange body in the chamber D_2 is occluded by the cation I'2, the small and small salt-removing tD_2, which is adjacent to each other via the first cation exchange membrane cl, and is concentrated by the second concentrating chamber C2. Water together [0042] In H2j, desalting f M through the cation exchanger layer of treated water, = sub-exchange body layer process towel, anion component (c ", c〇32-, fiC03 'SA, etc.) is again captured Specifically, the second small anion exchanger receives the ionic component, and the second and the desalting chamber adjacent to the intermediate ion exchange membrane a2 of the second D 2 spacer are called the ς 1 small desalination chamber. The anion component moved by D-1 is discharged to the outside of the system together with the first concentrating compartment C1 adjacent to the 】 a a a a a 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。 。. [0043] The deionization treatment of the deionized water manufacturing apparatus of the present embodiment is carried out. However, in the above-described treatment, a part of the anion component (carbonic acid or citric acid) of the concentrated water supplied to the second concentrating compartment C2 is moved by the second cation cation second desalting compartment D-2. The original of carbonic acid or Wei through the cation exchange membrane is as previously described. Here, from the second concentrating compartment C2 to the second small desalting compartment, the carbon 13 201249527 ί or : or ; Also ===positive body layer === ί, the rabbit acid or Wei is not trapped by the cation exchanger. The anode side surface of the first exchange membrane ei is interposed with the cationic cation exchanger layer. However, the G is divided by ===== and the water flowing through the cation layer and the anion ^7 is laminated in the direction: the carbonic acid or Wei of the exchange layer, in the next section of the yin "====1 The demineralization chamber w moves. _ ======: The acid is exchanged through the 苐3 anion exchange membrane to the i-th contraction chamber _, and the concentrated water of the first concentrating chamber C1 is discharged to 纟, cake eve, Ϊ::, carbonic acid and surgery will spread to the treated water to make the treated water [0044] layer; the inner cation exchanger layer and anion exchanger =::=:== to the first The cation exchange membrane is reduced by 'degree. This point is obviously not to be said. The domain of analytic acid or linalic acid, the pure water of the treated water [0045] According to the instructions of the witness, it should be understood that the ion exchange of the mouth The effect of the body of the laminate in the most $ D-2. In other words, only the ff ion parent exchange layer can obtain the passed ion exchange body Wei Wei from the early _^ spear, the dish to D-2 of the treated water last Shi Wu Shi = can change the system anion parent swap to achieve the above effect. Therefore, ion exchange, the front of the ion exchange layer of the species ί, g straight branch can also The cation exchanger layer is stacked in a layer of 4 or more in the order of the 0046^, which is the last step of the vaginal replacement layer. Further, the first small desalting chamber W of the deionized water enthalpy of the present embodiment is filled with 5 :2, ΐ treatment water is initially supplied to ^ " where there is a u-ion parent swap, the treated water is second supplied 14 201249527 ^ The second small desalting chamber D_2 is laminated in the order of the surface ion exchanger and the yin-yellow moon. Therefore, The treated water is initially passed through the anion exchanger, whereby the anion component is removed from the treatment to raise the pH of the water to be treated. [0047] Further, the treated water supplied through the first small desalination chamber is supplied to the bedding layer. a second small desalting compartment D_2 having a cation exchanger and an anion exchanger, that is, a treated water of an anion exchanger in the upper small desalination chamber D-1, followed by a sub-family replacement The money is over the anion exchanger. The key point is that according to the apricot composition, the water to be treated is exchanged through the _ sub-exchanger and the cation exchanger, and the anion exchanger has the ability to capture the anion component when the pH of the treated water is low. Higher 'cation exchanger' at the pH of the treated water When the height is high, the force of capturing the cation is relatively high. Therefore, according to the embodiment in which the water to be treated is initially passed through the anion exchange, the cation exchanger and the anion exchanger are passed through the anion exchanger. When the _ subcomponent is removed, the water which rises by ρ 接着 is then cross-crossed by the cation. Therefore, the cation exchange ion removal reaction is promoted more than usual. Furthermore, by the cation exchanger, the jT is reduced by a fraction of 'f' The treated water is then passed through an anion exchanger. The =11 flat ^ further promotes the removal of the anion reaction by the anion exchanger. Therefore, the ability to increase the silk content of the _ subcomponent containing carbonic acid or Wei is also increased. In addition to the removal ability of this point, Qing further advances the purity of the treated water. [0049] According to the deionized water manufacturing apparatus of the present embodiment, the carbonic acid or tannic acid contained in the very fine water is used. Part of it passes through the ion exchange membrane and diffuses to the effect of the purity of the ί::: two = water, plus the ability to remove the anion component such as acid or citric acid. The removal capacity of the cationic component contained in the water. -,people. The meaning of the bipolar membrane 4a is arranged in the desalting compartment D. Deionized water production 15 201249527 The water dissociated by electricity in the apparatus functions as an ion exchanger regenerant, as described above. Here, most of the voltage applied to the deionized water producing apparatus is utilized for the dissociation reaction of water. Therefore, in order to achieve operation under low voltage and high current, it is desirable to promote the dissociation reaction of water. In this case, the surface water manufacturing device towel of the lion-like state in which the bipolar membrane 4a is disposed in the desalting compartment D promotes the dissociation reaction of water and can be operated at a low voltage and a high current density. [0051] In a device for the production of ionized water, the water dissociation/heart bipolar (10) 4a is disposed only between the second small desalting ion exchange membrane (cation exchange membrane cl). In other words, the second small division
交換離軒錢膜Gl及陰離子効 有雙極性膜。此點具有下述的意義。亦即，在I 去離造事符號之離子__本實施形態$ 漭孫中、’、水解離所必需的過電壓在各層產生不同作 離子成分的陽離子電流更為增加，而在去_ 子成分的去除量相對性增為^少:此點意指陰 【0052】 知隹子成为的去除置相對性減少 陰離^分的被g處;^中，多半為陽離子紛^ 去除陰離子成分及陽離丄所以’糾上記偏流可充： 望的分配。 刀換^之，上述偏流反而是較為； 【0053】 但是，亦可以i:性:::::巧亡設f雙極性膜之構成( ::可f得與上述相同的作用效果，:二=:藉由此_ 膜。 ◎離子父換體相接的部分)取代成雙軸 ⑧ 16 201249527 [0054] 又，使第2小除鹽室士 上時，只要在與各险離 円的離子交換體之疊層數為4層以 雙極性膜即可。 子讀體相接的各離子錢膜上分別設置 【0055】 (比較實驗1) 為確認本發明的效果，、隹/_ 個去離子賴造裝置，轉較實驗。亦即，準備4 的雙極性膜或者配置處不有‘、、相1所示㈣2小除鹽室D-2 【0056】 室的第2小除鹽 2與陰離子交換體(陰離子交陰離子交換膜 g水^^置與本貫施職之去離子水製造裝置具有相同的除 【0057】 一 示’該去離子水製造裝置(比較例i)的第2小除趟 室D-2未配置有雙極性膜。 丨示鹽 【0058】 室該去離子水製造裝置(比較例2)的第2小除鹽 至D-2刀別配置有弟1雙極性膜4a及第2雙極性膜4b。再者’第 1雙極性膜4a以其陰離子交換膜2與陰離子交換體(陰離子交換體 層)相向的方向配置，第2雙極性膜4b以其陽離子交換膜3與陽= 子父換體(陽離子交換體層)相向的方向配置。 【0059】 ^如圖3(d)所示，該去離子水製造裝置(比較例3)的第2小除鹽 室D-2只配置有圖3(c)所示的第2雙極性膜牝。 1 【0060】 本次的比較實驗中，實施例1及各比較例中共通的規格、通 水流量、供給水等條件如下所述以下。另，CER係陽離子交換體(陽 17 201249527 離子交換樹脂）、AER係陰離子交換體(陰離子交換樹脂)之簡稱。 •陰極室：尺寸100x300x4mm填充AER •陽極室：尺寸100x300x4mm填充CER •第1小除鹽室：尺寸l〇〇x30〇x8mm填充AER •第2小除鹽室：尺寸100x300x8mm填充AER/CER (疊層) •濃縮室：尺寸l〇〇x30〇x4mm填充AER •除鹽室流量：50L/h •濃縮室流量：5L/h •電極室流量：l〇L/hExchanged from the Xuan money film Gl and anion effect have a bipolar membrane. This point has the following meaning. That is, in the ion I remove the ion of the symbol __ this embodiment $ 漭 孙, ', the necessary overvoltage of hydrolysis to increase the cation current in each layer to produce different ion components, and in the _ sub The relative amount of the component is increased to a small amount: this point means that the yin [0052] is known to remove the relative reduction of the negative separation of the g; in the middle, most of the cations are removed to remove the anionic component and Yang Lie 丄 so 'correction of the bias can be filled: the distribution of hope. If the knife is replaced by ^, the above bias current is more; [0053] However, it can also be: i: sex::::: the composition of the bipolar membrane is set to be the same (the same effect as above): =: by means of the _ membrane. ◎ ion father replacement part of the joint) replaced by a double shaft 8 16 201249527 [0054] Moreover, when the second small desalination chamber is on, as long as the ions are separated from each other The number of layers of the exchanger is four layers of a bipolar membrane. Each ion film attached to the sub-reading body was separately provided [0055] (Comparative Experiment 1) In order to confirm the effect of the present invention, 隹/_ deionization devices were transferred to the experiment. That is, the preparation of the bipolar membrane of 4 or the arrangement does not have ',, phase 1 (4) 2 small desalting chamber D-2 [0056] The second small desalting 2 of the chamber and the anion exchanger (anion exchange anion exchange membrane) The g water is set to be the same as the deionized water manufacturing apparatus of the present application. [0057] The second small deuteration chamber D-2 of the deionized water producing apparatus (Comparative Example i) is not provided. Bipolar film. 丨 [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ Further, the first bipolar membrane 4a is disposed in a direction in which the anion exchange membrane 2 and the anion exchanger (anion exchanger layer) face each other, and the second bipolar membrane 4b is replaced by a cation exchange membrane 3 and a positive = sub-parent (cation) The exchange body layer is disposed in the opposite direction. [0059] As shown in FIG. 3(d), the second small desalination chamber D-2 of the deionized water production apparatus (Comparative Example 3) is only provided with FIG. 3(c). The second bipolar membrane 所示 shown. 1 [0060] In the comparative experiment of this time, the specifications, the flow rate of water, the supply water, and the like common to the first embodiment and the comparative examples. The following are the following. In addition, CER is a cation exchanger (Yang 17 201249527 ion exchange resin), AER anion exchanger (anion exchange resin). • Cathode chamber: size 100x300x4mm filled AER • Anode chamber: size 100x300x4mm filled CER • 1st small desalination chamber: size l〇〇x30〇x8mm filled AER • 2nd small desalination chamber: size 100x300x8mm filled AER/CER (stack) • Concentration chamber: size l〇〇x30〇x4mm filled AER • Salt chamber flow: 50L/h • Concentration chamber flow: 5L/h • Electrode chamber flow: l〇L/h
•電極室、除鹽室、濃縮室供給水：二段反〇穿透水5士ljlS/cm •施加電流値：3A 在以上條件之下使實施例1及比較例1〜3之去離子水製造裝 置分別連續運轉200小時，並測定運轉開始時與運轉開始起2〇〇 小時後的運轉電壓、處理水的水質及處理水中的矽酸濃度。測定 結果顯不於表1。 【0061】 【表1】 實施例1 比較例1 比較例2 比較例3 運轉電壓 [V] 一 運轉開始時 8.8 11.3 12.1 10.9 200小時後 16.2 121 16 18.9 處理水比電阻 [ΜΩ · cm] 運轉開始時 17.9 17.8 17.7 YL1 ~ 200小時後 18.2 1.44 17.6 0.95 矽酸濃度 [Pg/L] 運轉開始時 0.6 1.5 0.9 """H~ 200小時後 0.3 67 1.3 11 【0062】 (實施形態2) 〃以下參照圖式說明本發明的電氣式去離子水製造裝置之實施 形，的^他例。總而言之，本實施形態之去離子水製造裝置在陰 極室與陽極室之間設有多數之除鹽處理部，在此點之外，與實^ 形1之去離子水製造裝置具有共通的構成。所以，以下謹說明 與實施形態1之去離子水製造裝置不同的構成，並適當省略對於 ⑧ 18 201249527 共通構成的說明。 【0063】 圖4係本實施形態之去離子水製造裝置的概略構成圖。圖4 所示的去離子水製造裝置中，陰極室E1與陽極室E2之間設有2 個除鹽處理部。2個除鹽處理部之中，相對上位於陰極側的第工 處理部係由除鹽室D1以及配置於除鹽室D1兩鄰的成對之濃 縮，Cl、C2所構成。另一方面，相對上位於陽極側的第2除鹽處 理部，係由除鹽室D2以及配置於除鹽室D2兩鄰的成對之濃^室 Cl、C3所構成。 [0064] 柄/在以下的說明中’將構成第1除鹽處理部的除鹽室D1稱為「陰 側3lj，將構成第2除鹽處理部的除鹽室D2 #為「陽極 進行區別。又’將濃縮室ci稱為「第1漠縮室 濃縮室C35至巧7 :第2濃縮室C2」，濃縮室C3稱為「第3 【0065】」來進仃別。但是，此種區別僅係便於說明的區別。 小除Ξί ’陰極側除鹽室D1及陽極侧除鹽室D2分別分隔成二個 室之下的說明中，賴成陰極側除鹽室D1的二個小除鹽 除鹽室濃縮室C1相鄰接的小除鹽室稱為「陰極侧第1小 第2小^與第2氣縮室C2相鄰接的小除鹽室稱為「陰極側 室之中ΐ ;2」。又，將構成陽極側除鹽室D2的二個小除鹽 除鹽室第3濃f室相鄰接的小除鹽室稱為「陽極側第1小 第2小除聰上’與第1濃縮室C1相鄰接的小除鹽室稱為「陽極側 【0066】、现至D2_2」。此種區別亦當然僅係便於說明的區別。 從降沬 一 述。亦^極^ 3侧起_依照順序說明各室的排列狀況時，如下所 縮室C2结丢極至Η隔著第1陰離子交換膜al而鄰接於第2濃 2小除遵C2隔著第1陽離子交換膜el而與陰極側第 2 Dl·2 2 ^ 、，、陰極側弟1小除鹽ϋ： D1·!相鄰接，陰極側第i 19 201249527 ^除第3陰離子交換膜a3而與第1濃縮室ci相鄰 ί ㈣2轉子交無e2而麵極侧第2小 ί j /相接，陽極側第2小除鹽室D2_2隔著第4陰離子 陽Ϊ側第1小除鹽請]相鄰接。陽ί侧第= 接，第3:曲-5-陰離子交換膜a5而與第3 m縮室C3相鄰 接。’辰、”s至C3隔著第3陽離子交換膜c3而與陽極室E2相鄰 【0067】 第1〜第3遭縮室C1〜C3設來用於引進從陰極 ί2 # _陰離f成分或陽離子成分，^其釋放 離ΐ交換體辰1 2 3 4至C1〜〇以單床形態填充有抑制結垢產生的陰 【0068】 以1小除鹽室亦1及陽極側第1小除鹽室D2-1分別 木形祕充有陰離子交換體。又，陰極側第2小除鹽室D 側第2小除鹽室D2_2分別以多床形態填充有陰離子交換體 體’上陰極侧第2小除鹽室D1·2及陽極側第2小 t二：Γ陰-離交換體及陽離子幻奐體之具體填充形態係如 頁ef恶1中所說明。又，陰極側第2小除鹽室D1_2及陽極側 ^鹽t D2_2分別配置有雙極性膜如。雙極性膜^的具體位 置/、朝向係如實施形態1中所說明。 【0069】 ° 20 ⑧ 1 ΐ次’概略說明圖4所示的去離子水製造裝置的被處理水及 2 澴細水之主要流動。被處理水分別平行地供給至陰極側第丨 3 鹽室D1-1及陽極側第！小除鹽冑du，並通過此等小除:、 J·過陰極娜1小雜室DH及陽测第丨小除鹽室])2^ 4 处理水’在此等小除鹽室外匯流一次之後分流而分別平行地供給 至陰極側第2小雜室D1-2及陽極娜2小除齡D2_2，^ ，此等小除鹽室之後排出至系統外。另—方面，濃縮水分別 地供給至第1〜第3濃縮室C1〜C3，在通過此㈣縮室之後排出 201249527 至系統外。 【0070】 為了如上所述地使被處理水及濃縮水流動，設有數個流道 〜U3、L1〜L2。圖4中，去離子水製造裝置上方所示的流道识， 其一端連接於被處理水的供給側，另一端側在途中分歧而分別連 接於陰極侧第1小除鹽室D1-1與陽極侧第1小除鹽室。去 離子水製造裝置下方所示的流道L1，分別連接於陰極側第丨小除 鹽室D1-1與陽極侧第丨小除鹽室，並在途中匯流之後分歧'， 分別連接於陰極侧第2小除鹽室D1-2與陽極侧第2小除鹽室 ^>2-2。去離子水製造裝置上方所示的流道U2，分別連接於陰極側 第2小除鹽室D1-2與陽極侧第2小除鹽室ϋ2-2，在途中匯流而. 連接至被處理水的排出侧。 . 【0071】 圖4中去離子水製造裝置上方所示的流道^3，其一端連接於 濃縮水的供給側連接，另-端側在途中分歧，並分別連接於第; 濃縮室C卜第2濃縮室C2及第3濃縮室C3。去離子水势造裝置 了方ΐΐί流道U分別連接於第1濃縮室C1、第2濃縮室C2及 第3濃縮室C3，並在途巾n流之後連接至濃縮水 。 [0072] 故其^說明具有上述構成的去離子水製造裝置之動作及作用。 第乂〜第3濃縮室C1〜C3係從流道U3供給濃縮水，並從流道乙2 ΐ it ’陰極室E1及陽極室E2係從未圖賴流道供'給電極水， 道將電極水排出。再者’陽極，極之間施加有 【0073】 在以上的狀態下，從流道饥將被處理水平行地供給至 陽1側第1小除鹽室腿。供給的被處理 ! : 3—、HC〇3—、Si〇2等)在被處理水通過第 丨tit 的過程中受_捉。並且，在陰極側第1 小除鹽至m_1賴她的轉子成分，往與陰極側帛1小除趟室 21 201249527 D1-1隔著第3陰離子交顧a3而相祕 並與通入該第！濃縮室C1的濃縮水共同^至f至^多動， 面，在陽極· H、除鹽室瓜丨受_ 了方 極側第1小除鹽室咖隔著第5陰離子交換^ =刀論在與陽 濃縮室C3移動，並與通入該第農又曲5而相鄰接的第3 系統外。 、°哀弟3，辰^ C3的濃縮水共同排出至 【0074】 其次’通過陰極側第1小除鹽室DM及陽;Ί , ^ # 的被處理水，經由麵 1小除鹽室 及陽極側第2小除趟室5極側苐2小除鹽室叫 鹽室_及陽極極側第2小除 換體層與陰離子交換體層。所·；， 陽離^ 層，其後通過陰===離 換體:樹足t第2小除鹽室D1-2内的陽離子交 第];^鹽#室D1-2 隔著 該第W縮室C2的漠縮水^ 夕至卜C2/t，通入 側第2小除豳室D2 ?F出至糸沆外。另一方面，在陽極 往與陽極侧除2==1^體2==陽離子成分， 接的第1、*f縮玄η 隔者弟2 %離子父換膜c2而相鄰 動，並與通入該第1漠縮室C1的濃縮水共 [0075] (Cr ' C〇3- ^ HC〇3- ^ sS2™ 受到捕捉渺離^在、陰側$ 2姆鹽室D1_2的陰離子交換體 而Δ^：往與陰極側第2小除鹽室叫隔著中間 離子又_ a2而相鄰接的陰極側第】小除鹽室叫移動。往陰 22 ⑧ 201249527 '1 dm移__子成分’往與陰極 =至-1隔著第3陰離子交換膜a3而相鄰接 ^ 動，並盥诵入兮筮]、、f d fl牧日]弟1 /辰鈿至Cl移 “ 3亥弟1 /辰、^至C1的濃縮水共同排出至系統外。另 =’、在陽極侧第2小除鹽室D2韻陰離子交換體=== 子成分’往與陽極侧第2小除鹽室D2_2隔著中替丢 而相鄰接的陽托彳目，丨楚1 f ㈢離子父換膜a4 室D2 除鹽室职移動。往陽極側第1小除趟 々至D2切動的陰離子成分，往與陽極侧第ι 乐，二 该弟3祕室C3的濃縮水共同排出 ，、通入 【0076】 r =係本ΐΐ形態之隹子水製造裝置巾的去離子處理之产 二ty以本貫施形態之去離子水製造裝置的方式設有多數i 室t ί; +子水製造裝置中，圖4所示鄰接於除鹽 =碳酸或石夕酸之外，還有碳酸或石夕酸從陰極側除鹽室J 4rf D2 ^ 3 C3 t , 至該，辰&至C3的浪縮水所含的碳酸或石夕酸之外，還^ =極側除鹽室D2移動過來。碳酸或概從相鄰接的除趟^往二 ，移動過來的原理係'如實施形態！中所說明。所以，心‘ f C1、第3濃縮室C3巾，碳酸或魏的濃度高於其他濃 y 膜的量也增加。尤其，濃縮室α與陽極 【0077] ? , ，依據本實_態之構成，從第1濃縮室C1往陽極側第 =除孤室DM移動的碳酸或石夕酸’受到填充在該除脑室切2 的陰離子交換體所捕捉，並經由陽極側第1小除趟 ^ 3 C3 〇 極侧昂2小除鹽室D2,2移_碳酸或魏並未概至被處理水。 23 201249527 【0078】 除趟ί 態中’被處理水最初供給至的陰極側第i小 體:又，通過陰鹽室D2_1中填充有陰離子交換 咖的被處理水所二此1及陽極側第1小除鹽室 亦即，Μ “ / 豐層有陽離子交換體與陰離较換體。 其後再交換體，其次通過陽離子交換體， 中八===第2小除鹽室Di_2及陽测第2小除鹽室取2 ϊΐ 膜4a。所以，依據與實施形態1中說明的相 低電壓、高電流密度下進行運轉。再加上，可藉由 22】分地去除㈣子成纽麟子成分。 (實施形態3) 參照圖5說明本發明去離子水製造裝置之實施形態的並 實施形態之去離子水製造裝置的基本構成係 2的去離子水製造裝置共通。所以，以下僅說明與實 形悲2之去離子水製紗置之間的相違點，省略對於共通點之 說明。 .' ' 【0081】 如圖5 ^示’本實卿態之絲子水製造裝財，在陰極室 農縮室C2之間設有副降鹽室S1。副除鹽室§ι隔著第6 陰離子父巧a6而與陰極室E1相鄰接，並隔著第丨陰離子交換 第2濃縮室C2相鄰接，在室内以單床形態填充有陰離 【0082】 本實施形態之去離子水製造裝置中係從流道U1平行地將被 處理水供給至陰極侧第丨小㈣室D1_卜陽極侧第丨小除鹽室 24 ⑧ 201249527 * D2_1及副除鹽室S1。供給至副除鹽室si的被處理水，在通過該 3除鹽室S1的過程中，陰離子成分(α-，c〇32—，HC〇3-，Si〇2 等t到捕捉。叉到捕捉的陰離子成分往與副除鹽室S1隔著第J 陰，子交細al而相嶋㈣2濃職C2移動，並與通入該第 2」辰縮室C2的濃縮水共同排出至系統外。另一方面，通過副除鹽 ^ 1的被處理水，在與通過陰極侧第j小除鹽室D1]及陽極侧 =的被處理水匯流之後，供給至陰極側第2小除 侧第2小除鹽室D2_2。此後的被處理水之流動 =子的動作係如實卿態丨或實施縣2中所㈣，故省略說 【0083】 料’被處理水情含_離子或辦 換膜的表二冗反Γ硬Γ分在離抒 生在 ：：ίΡΗ^ ^果。Lb可f給碳酸等陰離子成分即能獲得 抑制結垢產生。以皿至在相祕的濃縮室供給陰離子成分， 【0084】 給往CSC 離子水製造裝”分別為:供 給往第3濃縮室C3的^要夹^要來自陰極側除鹽室D1，供 3陰離子交換膜a3或第5%自子㈣^除鹽室D2。所以，抑制第 但是，往最靠陰極心的膜面上之結垢產生。 少於往第】濃縮室C1及第弟3 ^室至cC32^f_f成分之供給量， 離子交細al的膜面上比第3 ^ ^贈H即為第1陰 膜面上更容易產生結垢^狀Ϊ 第5陰離子交 25 201249527 另一方面，在陰極室El盥第2、、f 子交換體的副除鹽室S1的本實施態$ = 陰離 從副除鹽室si往第2濃縮室C2製造裝置中，係 交編 第 再者，填充於副除鹽室S1的 生的ΟΪΓ而再生。所以，乂 士 離子父換體藉由陰極室E1產 將陰極室的所 形態之去離子水製造裝置中， 交換體的再生。 口 1而捨棄的0Ή有效利用於離子 [0087] 亦能高因，即使電位較低 ’降低去離子水製造裝ϊ的運轉= 態中’追加副除鹽室S1作為新的除 不 =置:Π;對減少濃縮室之數量::二 【〇〇3成本’亦有關於降低施加電壓及運轉費用。、置 本實施形態系說明在陰極 f里部之例’但除鹽處理部可係！個二可冗=個除鹽 亦可在圖1所示的陰極室 =3，上。例如， 的副除鹽室。一至E1舁弟2 —至C2之間設置上_成 【0089】 例有言:舉 驗性陰離子交換體、種類而 w孔ίί=體:例;::==性::,交，維' * 交換體之種類而言二酸陽離 性陽離子交換體等。 刃啡丁又谀肢、強酸 26 201249527 【圖式簡單說明】 [0022] 氣式去離子水製造裝置之實施形態的 圖1係顯示本發明的電 一例之概略構成圖。 圖2係，1_所示_鹽室之放大圖。 圖3係顯不⑻〜⑷係顯示實施例1及比較例卜3有無第2 小除鹽室的雙極性膜及配置狀態之示意圖。 圖4係顯不本發明的電氣式去離子水製造裝置之實施形態的 其他例之概略構成圖。 圖6係顯示濃縮水中的碳酸成分擴散至被處理水中的原理。 f 7係顯示處理水中的碳酸成分再擴散至被處理水中的原理 之示意圖。 【主要元件符號說明】 【0090】 1框架體 2陰離子交換膜 3陽離子交換膜 .4a第1雙極性膜 4b第2雙極性膜 El陰極室 E2陽極室 C1第1濃縮室 C2第2濃縮室 C3第3濃縮室 D除鹽室 D-1第1小除鹽室 27 201249527 D-2第2小除鹽室 D1陰極侧除鹽室 D1-1陰極侧第1小除鹽室 D1-2陰極侧第2小除鹽室 D2陽極側除鹽室 D2-1陽極侧第1小除鹽室 D2-2陽極側第2小除鹽室 al〜a6陰離子交換膜 cl〜c3陽離子交換膜 A陰離子交換體層 C陽離子交換體層 U1〜U3、L1〜L2流道 28 ⑧• Electrode chamber, demineralization chamber, and concentration chamber supply water: two-stage dialysis water penetration 5 士ljlS/cm • Applied current 値: 3A Deionized water of Example 1 and Comparative Examples 1 to 3 under the above conditions The manufacturing apparatus was continuously operated for 200 hours, and the operating voltage after the start of the operation and 2 hours after the start of the operation, the quality of the treated water, and the concentration of the citric acid in the treated water were measured. The results of the measurements are not shown in Table 1. [Table 1] Example 1 Comparative Example 1 Comparative Example 2 Comparative Example 3 Operating voltage [V] At the start of operation 8.8 11.3 12.1 10.9 After 200 hours 16.2 121 16 18.9 Treatment water specific resistance [ΜΩ · cm] Operation started Time 17.9 17.8 17.7 17.7 YL1 ~ 200 hours later 18.2 1.44 17.6 0.95 citrate concentration [Pg/L] 0.6 1.5 at the start of operation """H~ 200 hours later 0.3 67 1.3 11 [0062] (Embodiment 2) Hereinafter, an embodiment of the electric deionized water producing apparatus of the present invention will be described with reference to the drawings. In summary, the deionized water producing apparatus of the present embodiment has a plurality of demineralizing treatment portions between the cathode chamber and the anode chamber, and has a configuration common to the deionized water producing apparatus of the solid one. Therefore, the configuration different from the deionized water producing apparatus of the first embodiment will be described below, and the description of the common configuration of 8 18 201249527 will be omitted as appropriate. Fig. 4 is a schematic configuration diagram of a deionized water producing apparatus of the present embodiment. In the deionized water producing apparatus shown in Fig. 4, two desalination treatment sections are provided between the cathode chamber E1 and the anode chamber E2. Among the two desalination treatment units, the first processing unit on the cathode side is composed of a deionization chamber D1 and a pair of confinement disposed adjacent to the demineralization chamber D1, and Cl and C2. On the other hand, the second desalting treatment portion on the anode side is composed of a desalting chamber D2 and a pair of concentrated chambers Cl and C3 disposed adjacent to the desalting chamber D2. In the following description, the demineralization chamber D1 constituting the first demineralization treatment unit is referred to as "the female side 31j, and the desalting chamber D2 # constituting the second desalination treatment portion is referred to as "the anode is distinguished. In addition, the concentrating chamber ci is referred to as "the first deflation chamber concentrating chamber C35 to qiao 7: the second concentrating chamber C2", and the concentrating chamber C3 is referred to as "the third [0065]". However, this distinction is only for ease of explanation. In the description that the cathode side demineralization chamber D1 and the anode side desalination chamber D2 are separated into two chambers respectively, the two small desalination and desalination chambers concentrating chamber C1 adjacent to the cathode side desalination chamber D1 are adjacent. The small desalination chamber connected to the small demineralization chamber called "the first side of the cathode side and the second chamber of the second gas chamber C2" is called "the cathode side chamber." Further, the small desalting chamber adjacent to the third concentrated f chamber of the two small desalting desalination chambers constituting the anode side desalination chamber D2 is referred to as "anode side first small second small decontamination" and first The small desalting chamber adjacent to the concentrating chamber C1 is called "anode side [0066], now to D2_2". This difference is of course only a distinction that is easy to explain. From the hail. In the case of the arrangement of the respective chambers, the following condensed chamber C2 is connected to the first anion exchange membrane a1 and is adjacent to the second rich 2 1 The cation exchange membrane el is adjacent to the second Dl·2 2 ^ on the cathode side, the small demineralization 阴极 on the cathode side, D1·!, and the i i 19 201249527 on the cathode side, except for the third anion exchange membrane a3. Adjacent to the first concentrating chamber ci 四 (4) 2 rotors are not e2 and the surface side is 2nd small ί j /, the anode side 2nd small desalting chamber D2_2 is separated by the 4th anion yang side first small desalination ] adjacent. The yang side is connected to the third, and the third sigma-5-anion exchange membrane a5 is adjacent to the third m condensing chamber C3. '辰,' s to C3 are adjacent to the anode chamber E2 via the third cation exchange membrane c3. [0067] The first to third contractions C1 to C3 are provided for introduction from the cathode ί2 # _ Or a cationic component, which is released from the oxime exchange body 1 2 3 4 to C1 〇 〇 in a single bed form filled with a scale that inhibits scale generation [0068] 1 small desalination chamber 1 and the anode side 1 small division The salt chamber D2-1 is filled with an anion exchanger, respectively, and the second small desalination chamber D2_2 on the D side of the second small desalination chamber on the cathode side is filled with an anion exchange body on the cathode side in a multi-bed form. 2 small desalting chamber D1 · 2 and anode side 2 small t 2: the specific filling pattern of the sputum-ion exchange body and the cationic phantom body is as described in the page ef. 1. In addition, the cathode side is the second small division. A bipolar membrane is disposed in each of the salt chamber D1_2 and the anode side salt d D2_2. The specific position/direction of the bipolar membrane is as described in the first embodiment. [0069] ° 20 8 1 ΐ The main flow of the treated water and the 2 澴 fine water in the deionized water production apparatus shown in Fig. 4. The treated water is supplied in parallel to the cathode side 丨3 salt chamber D1-1 On the anode side! Small demineralization 胄du, and through these small divisions:, J. over the cathode 1 small compartment DH and positive measurement of the small demineralization chamber]) 2 ^ 4 treatment of water 'in this small division After the salt is recirculated once, it is separately supplied to the cathode side second small compartment D1-2 and the anode na 2 small diurnal D2_2, ^, and these small demineralization chambers are discharged to the outside of the system. The water is supplied to the first to third concentrating chambers C1 to C3, respectively, and is discharged to the outside of the system after passing through the (4) condensing chamber. [0070] In order to flow the water to be treated and the concentrated water as described above, a plurality of streams are provided. In the flow path of the upper side of the deionized water producing apparatus, one end is connected to the supply side of the water to be treated, and the other end side is connected to the cathode side, respectively. The small desalination chamber D1-1 and the anode side first small desalination chamber. The flow channel L1 shown below the deionized water production device is connected to the cathode side third small desalination chamber D1-1 and the anode side third. Demineralization chamber, and divergence after convergence on the way', connected to the second small desalting chamber D1-2 on the cathode side and the second small desalination on the anode side Room ^>2-2. The flow path U2 shown above the deionized water production apparatus is connected to the second small desalination chamber D1-2 on the cathode side and the second small desalination chamber ϋ2-2 on the anode side, on the way. Connected to the discharge side of the treated water. [0071] The flow path ^3 shown above the deionized water production apparatus in Fig. 4 has one end connected to the supply side of the concentrated water and the other end side on the way. Divided into, and connected to the first; the concentrating chamber C, the second concentrating chamber C2, and the third concentrating chamber C3. The deionized water potential device is connected to the first concentrating chamber C1 and the second concentrating chamber C2, respectively. The third concentrating chamber C3 is connected to the concentrated water after the flow of the towel n. [0072] Therefore, the operation and action of the deionized water producing apparatus having the above configuration will be described. The third to third concentrating chambers C1 to C3 supply concentrated water from the flow path U3, and supply the electrode water from the flow channel B 2 ΐ it 'the cathode chamber E1 and the anode chamber E2 from the unillustrated flow channel. The electrode water is drained. Further, the anode is applied between the poles. [0073] In the above state, the horizontal line is supplied from the flow hunger to the first small desalination chamber leg on the male side. The supply is processed! : 3—, HC〇3—, Si〇2, etc.) is captured during the process of passing the treated water through the 丨tit. Further, on the cathode side, the first small demineralization to m_1 depends on her rotor component, and the cathode side 帛1 is slightly smaller than the cathode chamber 21 201249527 D1-1, and the third anion is treated via the third anion, and the ! Concentrated water in the concentrating chamber C1 is combined to f to ^ hyperactive, surface, in the anode · H, demineralization chamber, _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ It moves outside the third concentrating chamber C3 and is adjacent to the third system adjacent to the first cultivar. , ° ° brother 3, Chen ^ C3 concentrated water discharged to [0074] Secondly, through the cathode side of the first small desalination chamber DM and Yang; Ί, ^ # of the treated water, through the face 1 small desalination room and On the anode side, the second small deuterium chamber 5 pole side 苐 2 small desalination chamber is called the salt chamber _ and the anode pole side is the second small division layer and the anion exchanger layer. ,;, 阳离^ layer, followed by Yin === exchange body: tree foot t second small desalting chamber D1-2 cation intersection]; ^ salt # chamber D1-2 across the first The shrinkage water of the C-reducing chamber C2 is eve to the C2/t, and the second small diverticulum D2?F of the access side is out to the outside. On the other hand, in the anode to the anode side, 2 = 1 ^ body 2 = = cation component, the first 1, * f 玄 η 隔 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 2 The concentrated water that is introduced into the first desert chamber C1 [0075] (Cr 'C〇3- ^ HC〇3- ^ sS2TM is subjected to an anion exchanger that captures the yttrium and the yt2 2 salt chamber D1_2 Δ^: to the second small desalination chamber on the cathode side is called the intermediate side of the cathode side _ a2 and adjacent to the cathode side of the small demineralization chamber called mobile. To the yin 22 8 201249527 '1 dm shift __ child The component 'adjacent to the cathode = to -1 is adjacent to the third anion exchange membrane a3, and is inserted into the 兮筮], fd fl 牧日] brother 1 / 辰钿 to Cl shift "3 Haidi 1 / Chen, ^ to C1 concentrated water is discharged to the outside of the system. Another = ', on the anode side of the second small desalination chamber D2 rhyme anion exchanger === subcomponent 'to the anode side of the second small desalination chamber D2_2 is connected to the Yangtuo eye by the middle of the drop, and the 1f (three) ion father replaces the membrane a4 chamber D2 in the desalination chamber. The first anion is removed from the anode to the D2. To the ι 乐 乐, with the anode side of the third secret room C3 concentrated water Discharge, and pass [0076] r = the deionization treatment of the scorpion water manufacturing device towel of the present invention is provided with a plurality of i chambers in the manner of the deionized water manufacturing device of the present embodiment; In the sub-water production apparatus, as shown in Fig. 4, in addition to desalting = carbonic acid or a lithic acid, there is also carbonic acid or a sulphuric acid from the cathode side demineralization chamber J 4rf D2 ^ 3 C3 t , to the chen & amp In addition to the carbonic acid or the sulphuric acid contained in the water shrinkage of C3, the bottom side of the salt removal chamber D2 is moved. The carbonic acid or the entangled enthalpy from the adjacent one is moved to the second principle. As described in the embodiment, the concentration of carbonic acid or Wei in the heart 'f C1 and the third concentrating chamber C3 is higher than that of the other concentrated y film. In particular, the concentrating chamber α and the anode [0077] ? According to the configuration of the actual state, the carbonic acid or the sulphuric acid which moves from the first concentrating compartment C1 to the anode side and the solute compartment DM is trapped by the anion exchanger filled in the ventricle 2 and passes through the anode side. The first small 趟 ^ 3 C3 〇 侧 昂 2 small desalination room D2, 2 shift _ carbonic acid or Wei did not reach the treated water. 23 201249527 [0078] In the ί state, the cathode side i-th body to which the water to be treated is initially supplied is: the processed water which is filled with the anion exchange coffee in the salt chamber D2_1, and the first small demineralization chamber on the anode side. , Μ " / The cation exchange body has a cation exchange body and a negative exchange body. Then the exchange body, followed by the cation exchanger, the middle eight === the second small desalination chamber Di_2 and the second small desalination chamber Take 2 ϊΐ film 4a. Therefore, the operation is performed in accordance with the phase low voltage and high current density described in the first embodiment. In addition, the (4) sub-components can be removed by 22]. (Embodiment 3) A deionized water producing apparatus of the basic configuration of the deionized water producing apparatus according to the embodiment of the present invention will be described with reference to Fig. 5. Therefore, the following only explains the contradiction between the de-ionized water-made yarn set of the actual sadness 2, and the description of the common point is omitted. . ' ' [0081] As shown in Fig. 5, the sub-salt chamber S1 is provided between the cathode chamber C2 and the cathode chamber. The sub-salt chamber § ι is adjacent to the cathode chamber E1 via the sixth anion parent a6, and is adjacent to the second concentrating chamber C2 via the second anion exchange, and is filled with an anion in a single bed form indoors. In the deionized water production apparatus of the present embodiment, the water to be treated is supplied in parallel from the flow path U1 to the cathode side, the second (four) chamber D1_b, the anode side, the small demineralization chamber, 24 8 201249527 * D2_1 and the sub Demineralization chamber S1. The treated water supplied to the sub-desalting chamber si, during the passage through the 3 desalting chamber S1, an anion component (α-, c〇32-, HC〇3-, Si〇2, etc. t to capture. The captured anion component is moved to the sub-desalination chamber S1 via the J-thin, the sub-division A1, and the (4) 2-concentration C2, and is discharged to the outside of the system together with the concentrated water that has passed through the second "Crevitation chamber C2". On the other hand, the water to be treated by the sub-desalting salt 1 is supplied to the second side of the cathode side and the second side of the cathode side after being merged with the water to be treated which passes through the j-th small desalination chamber D1] on the cathode side and the anode side. Small demineralization chamber D2_2. After that, the flow of treated water = sub-action is as follows: or the implementation of county 2 (4), so it is omitted [0083] material 'processed water contains _ ions or replace the membrane Table 2 is a verbose Γ Γ Γ : : : ::: 。 ^ ^ : : : : : : : : : L L L L L L L L L L L L L L L L L L L L L L L L L L L L L 0084] For the CSC ion water manufacturing equipment, respectively: the supply to the third concentrating chamber C3 is to be supplied from the cathode side demineralization chamber D1 for the 3 anion exchange. Membrane a3 or 5% self-small (four) ^ demineralization chamber D2. Therefore, the inhibition is caused by the scaling on the membrane surface closest to the cathode core. Less than the first concentrating chamber C1 and the third brother room 3 The supply amount of cC32^f_f component, the surface of the ion-crossing a1 is more likely to cause fouling than the 3rd ^H, which is the first anomaly surface. 5th anion exchange 25 201249527 On the other hand, The cathode chamber El盥2, the sub-desalination chamber S1 of the f-sub-exchange body, the present embodiment $= anion from the sub-desalination chamber si to the second concentration chamber C2 manufacturing apparatus, the second is filled, filled Regenerating in the raw helium of the sub-salt chamber S1. Therefore, the gentleman ion parent is regenerated by the cathode chamber E1 in the form of a deionized water producing device in which the cathode chamber is formed, and the exchange body is discarded. The effective use of the Ή 离子 [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ [ The number of concentrating chambers:: 2 [〇〇3 cost] also has to reduce the applied voltage and operating costs. The embodiment is described in the cathode f For example, the demineralization unit can be used. The second can be redundant. The salt removal can also be shown in the cathode chamber of Figure 1. For example, the demineralization chamber. One to E1, the second to the C2. Between the settings _ into [0089] Example: the test anion exchanger, type and w hole ίί = body: example;::== sex::, intersection, dimension ' * the type of exchanger Acid cation cation exchanger, etc. flavonoids and limbs, strong acid 26 201249527 [Brief Description of the Drawings] [0022] FIG. 1 of an embodiment of a gas deionized water producing apparatus shows an outline of an electric example of the present invention Make up the picture. Fig. 2 is an enlarged view of the salt chamber shown by 1_. Fig. 3 shows a schematic diagram showing the presence or absence of the bipolar film of the second small desalting compartment in the first embodiment and the comparative example 3, and the arrangement state. Fig. 4 is a schematic block diagram showing another example of the embodiment of the electric deionized water producing apparatus of the present invention. Fig. 6 is a view showing the principle that the carbonic acid component in the concentrated water is diffused into the water to be treated. The f 7 series shows a schematic diagram of the principle that the carbonic acid component in the treated water is re-diffused into the water to be treated. [Description of main component symbols] [0090] 1 frame body 2 anion exchange membrane 3 cation exchange membrane. 4a first bipolar membrane 4b second bipolar membrane El cathode chamber E2 anode chamber C1 first concentration chamber C2 second concentration chamber C3 3rd concentrating compartment D Desalting compartment D-1 1st small desalting compartment 27 201249527 D-2 2nd small desalting compartment D1 Cathode side desalting compartment D1-1 Cathode side 1st small desalting compartment D1-2 Cathode side Second small desalination chamber D2 anode side desalination chamber D2-1 anode side first small desalination chamber D2-2 anode side second small desalination chamber a1 to a6 anion exchange membrane cl~c3 cation exchange membrane A anion exchange layer C cation exchanger layer U1~U3, L1~L2 flow channel 28 8