201247542 六、發明說明： 【發明所屬之技術領域】. 一本f明係與混凝污泥回收鋁鹽之技術有關’更詳 而5之疋指一種使用隔膜式電解法從混凝污泥中回收 紹鹽之方法與系統者。 【先前技術】 按，習知淨水廠混凝程序通常會加入鋁系混凝 dJ ’因此，排出之淨水污泥中會含有A丨（〇H)3固體物。 由於銘為兩性物質，習知含紹污泥U鹽回㈣π 外乎進行污泥之酸化或驗化程序，相關方法及處理設 備之技術如中華民國第1316510號、第1300058號、 第1325847號、第Μ3〇2575號等專利所示。 一般而言，當酸化ΡΗ<2及鹼化ΡΗ>12時，會產 生最佳的鋁鹽回收效率，傳統酸化程序多採用無機酸 —硫酸或鹽酸溶液，鹼化程序係採用氫氧化鈉溶液， 不過具腐蝕性的強酸及強鹼操作時會產生相當的危險 性。 【發明内容】 本發明之主要目的即在提供一種使用隔膜式電解 法從混凝污泥中回收鋁鹽之方法與系統，其利用隔膜 電解所產生強酸水、強鹼水技術，可便利地移除、回 收/于/尼中的紹鹽’且操作時無危險性者.。 緣是，為達成前述之目的，本發明係提供一種使 4 201247542 用1W膜式電解法從混凝污泥中回收鋁鹽之方法，其步 發至少包3有隔膜式電解：係將含結之混凝污泥與氯 二匕鈉溶液分別置於一電解槽之陰、陽極槽内，該陰、 陽極槽係以^子膜相隔，並充份混合該陰 '陽極槽 内之混凝污/尼與氯化納溶液以進行電解程序，而可產 生強酸性及強驗性電解水，並可於該陰、陽極槽内分 別形成酸化與驗化混凝+ ^ 双化此喊々泥之反應，用以可分別獲致 3 A1之酉夂液與含A1(〇H)4.之驗液；及固液分離：利 用材過慮别述酸液及鹼液而分別收集+遽液及 AKOHV濾液，留滞於該渡材之酸、驗性污泥則加以 混合形成中性污泥，再另行妥善處理。 進一步地’隔膜式電解之步财，係、將等量的含 銘之混凝污泥加人氣化納溶液再進行電解程序。 進一步地，隔膜式電解之步驟中，該質子膜係固 態電解質構成。 進一步地，隔膜式電解之步驟中，該陽極槽係產 生PH<2之強酸性電解水，該陰極槽係產生ρΗ〉η 的強驗性電解水。 進-步地，隔膜式電解之步驟中，該陽極槽内之 陽極不斷產生_子而與混凝污泥中 成Al3+，該陰極槽内之陰極係不斷產生OH·離子：盘 污泥中ai(oh)3反應生成ak〇h)4_。 ” 進-步地，固液分離之步驟中’該濾材係不織布。 201247542 此外，本發明更提供一種使用隔骐式電解法從混 凝污泥中回收鋁鹽之系統’包含有一電解槽，包含連 通之一陰極槽與一陽極槽，該陰、陽極槽内分別設有 一濾材及位於濾材内之陰、陽極；一質子膜，阻隔該 陰極槽與一陽極槽；及數閥門，分別連通該陰、^極 槽。 進一步地，該質子膜係固態電解質構成。 進一步地，各該濾材概呈袋狀’該陰、陽極係伸 入遽材。 進一步地，各該閥門係分別連通陰、陽極槽與濾 材内部。 " 【實施方式】 以下’兹舉本發明二較佳實施例，並配合圖式做 進一步之詳細說明如後： 。月4閱各圖所不，本發明一較佳實施例使用隔膜 式電解法從混凝污泥中回收鋁鹽之方法1〇〇，係使用 系.，先10進行’该系統i 〇包含有一電解槽12、一質 子膜14與數閥門丨6。 該電解槽包含連通之一陰極槽22與一陽極 ^ 錢㉟極槽22、24内分別設有-;慮材26、 27及位於濾材26、27内之陰、陽極、％。各該濾 材26 27概呈袋狀’係不織布材質。該陰極28係鋅 鈦材質之陰極’ @陽極3()係石墨材質之陽極。該 6 201247542 陰、陽極28、30並連接一古，ώ _ ^ _ 接直〜電源供應器32。 5亥貝子膜14，設置於$ + Μ 又罝於5亥電解槽12内並阻隔陰極 槽㈣極槽24,係固態電解質構成。 各該閥門1 6、丨7、丨s 2? , 19，係分別連通該陰、陽 極槽22、24與濾材26、27之内部。 Γ拌陰、、陽極槽22、24内更分別延伸設有一 :二 6(連接攪拌機），各該攪拌棒34、36 係分別伸入濾材26、27内部。 :么本^明°亥方法1 〇〇之第一步驟係隔膜式電解 ϋ®定濃度且等量之含紹混凝污泥與氣化納 (NaCl)溶液分別加入該陰、陽極槽22、μ之濾材 26、27内’再驅動各該攪拌棒％％，以攪拌、充份 此:此破污泥與氣化鋼溶液’繼而打開該直流電源供 應器32以進行電解程序，而可產生強酸性及強驗性電 解水，並可於該陰、陽極槽内分別形成酸化與驗化混 凝污泥之反應，俾強酸性電解水與污泥作用可生成 A1溶液（氣化鋁溶液），而強鹼性電解水與污泥作 用可生成Al(OH)4·溶液（鋁酸鈉溶液）（陽極3〇不斷 產生Η離子與混凝污泥中A〗（〇H)3反應生成A】3—，陰 極28不斷產生OH·離子與污泥中A丨（〇h)3反應生成 Al(OH)，）。 本發明該方法1 00之第二步驟係固液分離丨2〇 :係 關閉各該直流電源供應器32與攪拌棒34、36，再打 201247542 =^玄間㈣、19,以分別收集經各該濾材127 =慮^ +渡液及A1_V渡液，待链鹽濾液回收* :::閉各該閥門18、19’再打開各該閥門“、二 排放被各據材26、27留滞之酸m亏泥，經日八士 成中性污泥，再另行妥善處理。 此。调 以下係本發明該方法1 〇〇之實例： 進行該隔膜式電解110步驟時，可先取二 混凝污泥加入4_ml水，再分置2 :納當電解質’啟動各該攪拌棒34、36以物：， ”以5 ο V進行電解i 8 〇分鐘，定時取樣測p H值。 結果由圖三可知，初期該陽極3〇之pH值隨時間 、込下降，50分鐘後pH<2 ;而初期該陰極28之pH ，時，快速升高，8〇分鐘後pH>i2。基此，顯示 、陽極28、3G的酸、驗度都可達到紹鹽適溶的階 段0 而由圖四可知，該陰、陽極槽22、24確實可酸化、 驗化含銘污泥’且铭溶出量隨電解時間增加。 奸而進行該固液分離120之步驟後，該陽極槽24内 .歪過濾材27過濾後測得濾液之鋁濃度為726.8mg/L·， ^ '合出鋁罝為13·7 g/Kg (as A】203)。該陰極槽22内 7 °慮材26過遽後測得濾、液之銘漠度為465.9mg/L， 污泥洛出鋁量為8·8 g/Kg (as Α】2〇3)。剩餘之酸、鹼 8 201247542 其PH值為6.7 以上結果列於201247542 VI. Description of the invention: [Technical field to which the invention pertains] A technique related to the recovery of aluminum salts from coagulated sludge is more detailed and 5 refers to the use of a diaphragm electrolysis process from a coagulated sludge. The method and system for recovering salt. [Prior Art] According to the conventional water purification plant coagulation process, aluminum coagulation dJ is usually added. Therefore, the discharged purified water sludge will contain A丨(〇H)3 solid matter. Since the name is amphoteric substance, the conventional U-salt sludge U (salt) is used to carry out the acidification or verification procedure of the sludge, and the related methods and processing equipment technologies are as shown in the Republic of China No. 1316510, No. 1300058, No. 1325847, No. 3, 2,575 and other patents are shown. In general, when acidified bismuth <2 and alkalized bismuth > 12, the best aluminum salt recovery efficiency is produced. The conventional acidification procedure mostly uses a mineral acid-sulfuric acid or hydrochloric acid solution, and the alkalization procedure uses a sodium hydroxide solution. However, corrosive strong acids and strong bases can cause considerable risks. SUMMARY OF THE INVENTION The main object of the present invention is to provide a method and system for recovering aluminum salt from a coagulated sludge by using a diaphragm electrolysis method, which utilizes strong acid water and strong alkaline water technology generated by diaphragm electrolysis, and can be conveniently moved. In addition to, recycling / in the middle of the salt in the salt and the operation is not dangerous. The reason is that, in order to achieve the above object, the present invention provides a method for recovering aluminum salt from coagulated sludge by 1 201247542 by 1W membrane electrolysis, which has at least 3 membrane electrolysis: The coagulated sludge and the sodium bismuth dichloride solution are respectively placed in the anode and the anode tank of an electrolyzer, and the anion and anode tanks are separated by a membrane, and the concrete in the anode tank is fully mixed. /Ni and sodium chloride solution for electrolysis process, which can produce strong acid and strong electrolyzed water, and can form acidification and test coagulation in the cathode and anode tank respectively. The reaction is used to separately obtain the sputum of 3 A1 and the test liquid containing A1 (〇H) 4. and solid-liquid separation: separately collecting the sputum and the AKOHV filtrate by using the acid and the lye The acid and the test sludge remaining in the ferry are mixed to form a neutral sludge, which is then disposed of separately. Further, in the case of the diaphragm type electrolysis, an equal amount of the coagulated sludge containing the ingot is added to the gasification nano-solution and the electrolysis process is carried out. Further, in the step of diaphragm electrolysis, the proton membrane is composed of a solid electrolyte. Further, in the step of the diaphragm type electrolysis, the anode tank system generates a strong acidic electrolyzed water of pH < 2, which produces a potent electrolyzed water of ρ Η η. Further, in the step of diaphragm electrolysis, the anode in the anode tank continuously generates _ sub and forms Al3+ with the coagulated sludge, and the cathode system in the cathode tank continuously generates OH· ions: (oh)3 reaction produces ak〇h)4_. In the step of solid-liquid separation, the filter medium is non-woven. 201247542 In addition, the present invention further provides a system for recovering aluminum salt from coagulated sludge using a barrier electrolysis method, comprising an electrolytic cell, including Connecting a cathode tank and an anode tank, wherein the cathode and the anode tank are respectively provided with a filter material and a cathode and an anode located in the filter medium; a proton membrane blocking the cathode tank and an anode tank; and a plurality of valves respectively connected to the cathode Further, the proton film is composed of a solid electrolyte. Further, each of the filter materials is in a bag shape, and the anode and the anode are extended into the coffin. Further, each of the valves is connected to the anode and the cathode. <Embodiment> [Embodiment] The following is a description of the preferred embodiment of the present invention, and further detailed description with reference to the following figures: A method for recovering an aluminum salt from a coagulated sludge using a diaphragm electrolysis method is to use a system. First, the system i 〇 includes an electrolytic cell 12, a proton membrane 14 and a plurality of valves 丨6. Electricity The tank includes a cathode tank 22 and an anode 35 poles 22, 24 respectively provided; a material 26, 27 and a cathode, an anode, and a % located in the filter material 26, 27. The bag is made of non-woven material. The cathode 28 is a zinc-titanium cathode ' @ anode 3 () is an anode of graphite material. The 6 201247542 cathode and anode 28, 30 are connected to an ancient, _ _ ^ _ straight ~ Power supply 32. 5 haibei sub-film 14, set in $ + Μ and 罝 in the 5 hai electrolytic cell 12 and block the cathode tank (four) pole slot 24, which is composed of solid electrolyte. Each of the valves 1 6, 丨 7, 丨 s 2?, 19, respectively, connecting the inside of the cathode and anode tanks 22, 24 and the filter materials 26, 27. The mixing tanks and the anode tanks 22, 24 are respectively extended with one: two 6 (connecting mixer), each of which The stirring rods 34 and 36 are respectively inserted into the inside of the filter materials 26 and 27. The first step of the method is to use a diaphragm type electrolytic ϋ® concentration and an equal amount of mixed coagulating sludge and gas. A solution of sodium (NaCl) is added to the filter medium 26, 27 of the cathode and anode tanks 22, respectively, and the % of the stir bar is further driven to stir and fill the mixture: The sludge and the gasification steel solution' then turn on the DC power supply 32 to perform an electrolysis process, which can generate strong acid and strong electrolyzed water, and can form acidification and verification coagulation in the cathode and anode tanks respectively. The reaction of sludge, the strong acidic electrolyzed water and sludge can produce A1 solution (vaporized aluminum solution), and the strong alkaline electrolyzed water and sludge can produce Al(OH)4·solution (sodium aluminate solution) (Anode 3 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 〇 OH),). The second step of the method 100 of the present invention is a solid-liquid separation 丨2〇: the DC power supply 32 and the stirring rods 34 and 36 are turned off, and then 201247542 = ^ 玄 (4), 19, respectively, to collect the respective The filter material 127 = considers the + liquid and the A1_V liquid, and the chain salt filtrate is recovered. *:: Each of the valves 18, 19' is opened again, and the two discharges are left behind by the respective materials 26, 27. The acid m is deficient in the mud, and the neutral sludge is converted into a neutral sludge, and then properly disposed of. The following is an example of the method of the present invention: 1. When the diaphragm electrolysis 110 step is performed, the second coagulation can be taken first. The mud is added with 4_ml of water, and then divided into 2: the nano-electrolyte 'starts each of the stirring rods 34, 36 with the object:," electrolyzes at 5 ο V for 8 minutes, and the sample is periodically sampled to measure the p H value. As a result, as shown in Fig. 3, the pH of the anode 3 初期 was decreased with time and enthalpy, and the pH was < 2 after 50 minutes, and the pH of the cathode 28 was initially increased rapidly, and the pH was > i2 after 8 minutes. Therefore, the acidity and the degree of the display, the anodes 28 and 3G can reach the stage 0 of the salt-soluble solution. As can be seen from Fig. 4, the cathode and anode tanks 22 and 24 can be acidified and verified to contain the sludge. The amount of dissolved dissolved increases with the electrolysis time. After the step of performing the solid-liquid separation 120, the aluminum concentration of the filtrate in the anode tank 24 after filtration of the filter material 27 was 726.8 mg/L·, ^ 'the aluminum bismuth was 13·7 g/Kg. (as A) 203). In the cathode tank 22, after 7° of the material 26 is over-twisted, the filtration and liquid infiltration degree is 465.9 mg/L, and the sludge aluminum output is 8·8 g/Kg (as Α) 2〇3). Remaining acid and base 8 201247542 Its pH value is above 6.7.
性污泥經混合調勻後 表一。 由上可知，本發明使用隔膜式電解法從混凝污泥中 紹鹽之方法與系統’係採用隔膜電解水的方式， =曹：以固態電解質構成之質子膜相隔，致使電 解過私產生之電解水可達到更酸、更 酸性電解，H<2和陰極槽產製的= P > 12同牯酸化及鹼化含鋁污泥，且極 不斷產生H+離子與污泥中A糊3反應生成八丨3+，牌 :因：析出的還原電位明顯大於氫的析出電位因此J '“呂無法在陰極表面析出，只有氫還原析出產生⑽_ :子與污泥：A1(0H)3反應生成零H)4•，進而收集 蛋槽的Al3+溶液與陰極槽的Α1(ΟΗ)4-溶液達到回收 曰義的目的，且操作時無危險性，甚具實用價值，·緣 疋本發明確時符合發明專利之要件，袭依法提出申 201247542 請0 【圖式簡單說明】 圖一係本發明一較佳實施例之流程圖。 圖二係本發明一較佳實施例之系統圖。 圖三係本發明之陰、陽極pH值隨電解時間變化 圖。 圖三係本發明之污泥I呂溶出量（g/Kg as Al2〇3)隨 電解時間之變化圖 【主要元件符號說明】 系統10 電解槽12 質子膜14 閥門16 陰極槽22 陽極槽24 濾材26、27 陰、陽極28、30 直流電源供應器32攪拌棒34、36方法100 隔膜式電解11 〇固液分離120 10The sludge is mixed and mixed. Table 1 It can be seen from the above that the method and system for using the diaphragm type electrolysis method to extract salt from the coagulated sludge adopts the method of electrolyzing water by the diaphragm, = Cao: the proton membrane formed by the solid electrolyte is separated, resulting in electrolysis. Electrolyzed water can achieve more acid, more acidic electrolysis, H < 2 and cathode tank production = P > 12 with acidification and alkalization of aluminum-containing sludge, and extremely constant production of H + ions and sludge A paste 3 reaction Generate gossip 3+, card: Because: the precipitation reduction potential is significantly larger than the hydrogen precipitation potential, so J '" Lu can not be precipitated on the cathode surface, only hydrogen reduction precipitation occurs (10) _: sub-sludge and sludge: A1 (0H) 3 reaction Zero H)4•, and then collecting the Al3+ solution of the egg tank and the Α1(ΟΗ)4-solution of the cathode tank to achieve the purpose of recovery, and the operation is non-hazardous, and has practical value. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a flow chart of a preferred embodiment of the present invention. FIG. 2 is a system diagram of a preferred embodiment of the present invention. The pH values of the cathode and the anode of the invention change with the electrolysis time Figure 3 is a graph showing the change of sludge I lysate (g/Kg as Al2〇3) according to the present invention with electrolysis time [Description of main components] System 10 Electrolyzer 12 Proton membrane 14 Valve 16 Cathode tank 22 Anode Tank 24 filter material 26, 27 cathode, anode 28, 30 DC power supply 32 stir bar 34, 36 method 100 diaphragm type electrolysis 11 tamping liquid separation 120 10