201206838 六、發明說明： 【發明所屬之技術領域】 本發明是有關於一種廢水處理方法及其裝置’且特別是有 關於一種廢水處理高效率、低成本，且能有效地解決色度問題 的廢水回收處理方法及其系統。 【先前技術】 『染整』屬國内傳統產業中數量相當龐大且重要的產業， 由於其製程中須耗費大量的用水’故亦屬於高耗水型的產業之 •一，而為了因應水資源不足、水價調整與廢水排放費等相關政 策的實施，業者乃大量投入各種防污及回收處理設備，期能達 到正常放流與廢水回收再利用之目的。 由於染整工業需使用多種染料'界面活性劑與化學助劑’ 因此染整廢水具有高色度、水質變化大及生物難分解有機物的 特性，致使染整廢水必須併用生物與化學程序來處理’以降低 廢水中的 BOD ( Biochemical Oxygen Demand ’ 生化需氧量）、 籲 COD ( Chem i ca 1 Oxygen Demand，化學需氧量）、SS (懸浮固體） 與色度。 國内多數染整廠以往對於廢水處理方法’如第1圖所示’ 大致上是將收集的染整廢水先截方後，輸送入調節池中進行PH 調整，接著在進行生物處理（活性汸泥與生物沉澱），再送入 沉墊池中’然後進行化學處理合併加氯脫色，最後在形成放流 水排出，所以以往的處理方法，主要是以活性污泥及化學混凝 為主要處理程序，但上述兩種方式都會產生大量的污泥，這些 201206838 污泥所含水份極高，只能以蒸餾方式進行脫水，相當耗費能 源、增加成本，且處理後的放流水中仍含有極高的色度，無法 通過目刖放流水標準色度ADMI值（American Dyestuff Manufactures Institute)的標準，因此，染整廢水中的脫色 技術已成為業界注目的環保課題。 而目前已知染整廢水色度的去除方式不外乎電化學法、化 學混凝、NaOCl法、Fenton法、薄膜過濾法（R〇)…等方式， 其中電化學法是經由電解作用產生水和金屬氧化物，以吸附廢 • 水中污染物形成膠羽，再配合高分子凝集劑加速沉降作用去除 水中固體粒子’但此法除了須先控制廢水的PH值之外，且氧 化還原的操作時間緩慢，不利於處理高流量的染整廢水。201206838 VI. Description of the Invention: [Technical Field] The present invention relates to a wastewater treatment method and apparatus thereof, and particularly relates to a wastewater which is highly efficient, low-cost, and capable of effectively solving chromaticity problems Recycling treatment method and system thereof. [Prior Art] "Dyeing and finishing" is a very large and important industry in the traditional industries in China. Because it requires a lot of water in the process, it is also a high-water-consuming industry. In order to cope with the shortage of water resources, The implementation of relevant policies such as water price adjustment and wastewater discharge fees has resulted in a large number of anti-fouling and recycling treatment equipment, which can achieve the purpose of normal discharge and waste water recycling. Because the dyeing and finishing industry needs to use a variety of dyes 'surfactants and chemical additives', the dyeing and finishing wastewater has high chroma, large changes in water quality and the characteristics of biologically difficult to decompose organic matter, so that dyeing and finishing wastewater must be treated with biological and chemical procedures. To reduce BOD (Biochemical Oxygen Demand ' in the wastewater, COD (Chem i ca 1 Oxygen Demand), SS (suspended solids) and color. In most domestic dyeing and finishing plants, the wastewater treatment method 'as shown in Figure 1' is roughly the first to collect the dyeing and finishing wastewater, then transport it into the conditioning tank for pH adjustment, and then carry out biological treatment (activity 汸Mud and biological precipitation), and then sent to the sinking tank pool 'then chemical treatment combined with chlorination decolorization, and finally discharged in the formation of discharge water, so the previous treatment methods, mainly based on activated sludge and chemical coagulation as the main treatment procedures, However, both of these methods produce a large amount of sludge. These 201206838 sludges have extremely high water content and can only be dehydrated by distillation. This is quite energy-intensive and costly, and the treated discharge water still contains extremely high color. The degree of ADMI (American Dyestuff Manufactures Institute) standards cannot be met. Therefore, the decolorization technology in dyeing and finishing wastewater has become an environmentally important issue in the industry. At present, it is known that the color removal of dyeing and finishing wastewater is no more than electrochemical method, chemical coagulation, NaOCl method, Fenton method, membrane filtration method (R〇), etc., wherein the electrochemical method generates water through electrolysis. And metal oxides, in order to adsorb waste • Contaminants in water to form rubber feathers, and then use polymer agglomerating agent to accelerate sedimentation to remove solid particles in water', but this method must control the pH value of wastewater, and the operation time of redox Slow, it is not conducive to the treatment of high-flow dyeing and finishing wastewater.
NaOCl法是直接對經過生物與混凝處理後的廢水池中加入 次氣酸納，俾利用其氣成份來除色，但是由於次氣酸納的添加 量僅以人工來控管，所以對於刻量的控制上須相當小心，劑量 不足將造成放流水色度過高，添加劑過量則不符成本，且餘氣 φ 將造成環境的毒害。The NaOCl method directly adds sub-gas sulphate to the wastewater pool after biological and coagulation treatment, and uses its gas component to remove color. However, since the amount of sub-gas sulphate is only controlled manually, it is The amount of control must be very careful. Insufficient dosage will cause the color of the discharged water to be too high, and the excess of the additive will not be cost, and the residual gas φ will cause environmental poisoning.
Fenton法則是利用Fe2+催化仏〇2反應以產生0H (Hydroxyl Radical)自由基，而形成具有氧化及混凝的能力’ 用以去除染整廢水中的色度，故此法特別適合處理尚C00且 難生物分解的有機廢液，但此法卻需在強酸性壞境中才能發揮 氧化作用，且會產生大量的鐵冷泥，因鐵〉5泥的脫水性不佳’ 還需要經過後續的電解還原處理’所以也成為應用時的一大缺 點。 薄膜過滤法（R0)是目前業界公認對於回收水品質最好的〔 201206838 處理方法之一，其是利用逆滲透膜來去除水中的有機物及色 度，其COD與色度的去除率可高達90%以上，但因染整廢水 中的懸浮物質（SS)極高，若無搭配良好的前處理來實施，薄 膜很容易產生濃度極化現象，產生氧化結晶，甚或表面結垢、 堵塞而喪失過濾過果，所以此法的設備及操作成本較高，更重 要的是，此法的濃縮廢水無法再次以逆滲透膜來處理，成為相 當棘手的問題。 此外，尚有採用Fenton法搭配二氧化鈦（Ti〇2)，或是利 • 用電場或結晶技術來提升處理效果，及降低化學污泥產量，但 這些方式都只是著重在對於廢水中「染整色度的去除」，對於 處理程序後所產生的濃縮污水（泥），至今仍沒有一有效率且符 合操作成本的處理方法，使得染整業在環保改善成本負荷上愈 來愈高，故如何積極藉由清潔生產及污染防治技術來兼顧經濟 與環保，降低生產成本，提高產業競爭力，已成為目前相關產 業迫切努力之目標。 I 【發明内容】 本發明之目的，即在提供一種廢水處理效率高、成本低， 不僅能有效地解決色度問題，且可對濃縮廢水進行再處理的廢 水回收處理方法及其系統。 根據本發明所提出之一種廢水回收處理方法，包含以下步 驟： 步驟（A):將染整廢水唧引入一前處理槽内。 S! 步驟（B):在該前處理槽内加入一吸附劑，使該吸附劑與 染整廢水進行快速混合，以輔助對於染整廢水的脫色及過濾， 5 201206838 該前處理槽内具有一第一過濾裝置，該第一過濾裝置包含有至 少一親水性的多孔薄膜。 步驟（c):使輔助脫色後的廢水通過該第一過濾裝置的過 濾處理，以降低水中的色度及懸浮固體含量。 步驟（D):將通過該第一過濾裝置過濾處理後的水液輸送 至一 R0過濾單元内，並施以進行R〇薄膜過濾程序，使透析過 R0薄膜的淨水匯送至一回收槽内，以供再利用。 步驟（E):將經過R0過濾單元所排放出的濃縮廢水再導引 入第一過’慮裝置中，§亥第一過遽' 裝置包含有至少一疏水性的 多孔薄m。 步驟（f):對該第二過濾裝置内的濃縮廢水施以微細氣泡 化混合處理，使濃縮廢水與氣體能均勻混合成乳白霧化狀態的 工作液體。 步驟（G):在該疏水性薄膜的產水側施以負壓吸引，使高 含氣量的工作液體中的水蒸氣能輕易地通過該疏水性薄膜，藉 以除去工作液體中的殘餘色度及懸浮微粒，以獲得符合排玫標 準的放流水。 依照上述本發明所提出之廢水回收處理方法，其中，在步 驟（β)中’在該前處理槽中所添加的吸附劑可為矽藻土、活性 石反或沸石粉末。 依照上述本發明所提出之廢水回收處理方法，其中，在步 驟（Ε)之前，更具有在經過R〇薄膜過濾處理後的濃縮廢水中， 添加入脫色劑。 依照上述本發明所提出之廢水回收處理方法，其中，在步 201206838 驟（G)後’更具有對產出放流水後的高濃度污泥通過一脫水處 理。 依照上述本發明所提出之廢水回收處理方法，其中，在步 驟（F)中’在對濃縮廢水進行微細氣泡化混合時，所泵送入的 氣體是經過預先高溫加熱，使混合後的工作液體具有一定溫度。 依照上述本發明所提出之廢水回收處理方法，其中，該工 作液體的加熱溫度為攝氏30°c〜60°c。 依照上述本發明所提出之廢水回收處理方法，其中，在步 驟（G)，更具有對通過該疏水性薄膜的水蒸氣分子施以冷凝處 理，以使水蒸氣凝結成放流水的作業程序。 根據本發明所提出之一種廢水回收處理系統，包含一前處 理槽、一第一過濾裝置 '一叨過濾單元、一回收槽、一第二過 濾裝置、一微細氣泡化裝置以及一回收槽。該前處理槽，用以 容裝預定容量的染整廢水。該第一過濾裝置，裝設在該前處理 槽内，具有一水平設置的中央管、複數個水密地套穿在該中央 管上的親水性的多孔薄膜，且前述親水性薄膜是與該中央管形 成連通，使透析入前述親水性薄膜内的水液能匯送至該中央管 中。該RG過料το，接設在該第—過濾裝置的中央管出水端。 該回收槽，設置在該R0過渡單元一側，用以將通過該肋過遽 單元的乾淨水液匯集回收再制^該第二韻裝置，接設在該 R0過遽單it的I缩廢水排放管路上，該第二過濾裝置具有—承 接濃縮廢水賴H直穿樞在該殼體巾央的產水管及複 數個等間隔且水平排列的疏水性的多孔薄膜。該微細氣泡化裝 置’裝設在該第二魏裝置的側邊，具有—對應該殼體的氣體^ 7 201206838 供應器’以對該殼體内的濃縮廢水泵送入加壓氣體，促使濃縮 廢水成為乳白霧化狀態的工作液體。該回收槽，接設在該第二 過遽裝置的產水管出水口上。 依照上述本發明所提出之廢水回收處理系統，其中，該第 一過濾裝置的親水性薄膜為UF薄膜。 依照上述本發明所提出之廢水回收處理系統，其中，更包 3有一預加熱裝置，使混合後的工作液體具有一定的溫度。 依照上述本發明所提出之廢水回收處理系統，其中，更包 含有一負壓元件，該負壓元件是與該第二過濾裝置的產水管連 通，以對於疏水性薄膜產水側形成真空吸力。 因此，本發明先利用吸附劑來輔助對於染整廢水的脫水與 過濾，然後以親水性薄膜進行R0膜的前置過濾，降低R0膜污 堵與結垢的情形，且經過R0處理所排出的濃縮廢水經過微細氣 泡處理後，再利用疏水性薄膜進行固液分離，使得放流水的色 度、B0D肖C0D值皆能達到目前排放標準，而採用疏水性薄膜 加上旋轉方式亦能有效地延長操作週期，使濃縮廢水中的水份 能排出，不僅快速有效率，且能降低加藥與操作成本。 【實施方式】 參照第2圖及第3圖，本發明廢水回收處理方法及其系統 的第一實施例，包含以下步驟： 步驟（A).將染整廢水匯集後引人-前處簡1()内待處理。 步驟（B):在該前處理添加入適量的_吸附劑2〇。 在本實施例中，該吸附劑20可為矽藻土、活性碳或沸石粉末， 並使該吸㈣I 2G㈣整廢錢行快速混合，俾彻料附劑 8 201206838 20來吸_絲水中的色料及料微粒，以伽對於染整廢水 的脫色及過遽效果。此外，該前處理槽1()内具有—第—過滤裂 置3〇，請㈣第4圖，該第—過縣置30是採半沉降式地橫 向設置在該前處理槽10中，並具有—水平設置的中央管Fenton's rule is to use Fe2+ to catalyze the 仏〇2 reaction to produce 0H (Hydroxyl Radical) free radicals, and to form the ability to oxidize and coagulate' to remove the chromaticity in the dyeing and finishing wastewater. Therefore, this method is particularly suitable for the treatment of C00 and difficult. Biodegradable organic waste liquid, but this method needs to be oxidized in a strong acid environment, and will produce a large amount of iron cold mud. Because of the poor dehydration of iron>5 mud, it needs to undergo subsequent electrolytic reduction. Processing 'has also become a major drawback when applied. The membrane filtration method (R0) is recognized by the industry as one of the best quality methods for recycling water [201206838 treatment method. It uses reverse osmosis membrane to remove organic matter and chromaticity in water, and its COD and chromaticity removal rate can be as high as 90. More than %, but because the suspended matter (SS) in the dyeing and finishing wastewater is extremely high, if it is not carried out with a good pretreatment, the film is prone to concentration polarization, resulting in oxidative crystallization, or even surface fouling, clogging and loss. The fruit is filtered, so the equipment and operation cost of this method are high, and more importantly, the concentrated wastewater of this method cannot be treated again by the reverse osmosis membrane, which becomes a very difficult problem. In addition, the Fenton method is used in combination with titanium dioxide (Ti〇2), or the use of electric field or crystallization technology to improve the treatment effect and reduce the production of chemical sludge, but these methods only focus on the dyeing and finishing of the wastewater. The removal of the degree", the concentrated sewage (mud) produced after the treatment process, there is still no efficient treatment method that meets the operating cost, so that the dyeing and finishing industry is getting higher and higher in environmental protection and cost load, so how to be active By taking into account the economy and environmental protection, reducing production costs and improving industrial competitiveness through clean production and pollution prevention technologies, it has become the urgent goal of relevant industries. I SUMMARY OF THE INVENTION The object of the present invention is to provide a waste water recovery treatment method and system thereof which have high wastewater treatment efficiency and low cost, can not only effectively solve the chromaticity problem, but can reprocess concentrated wastewater. A wastewater recovery treatment method according to the present invention comprises the following steps: Step (A): introducing the dyeing and finishing wastewater into a pretreatment tank. S! Step (B): adding an adsorbent to the pretreatment tank to rapidly mix the adsorbent with the dyeing and finishing wastewater to assist in decolorization and filtration of the dyeing and finishing wastewater, 5 201206838 The pretreatment tank has a A first filtration device comprising at least one hydrophilic porous membrane. Step (c): passing the auxiliary decolorized wastewater through the filtration treatment of the first filtering device to reduce the color and suspended solid content in the water. Step (D): transporting the water solution filtered by the first filtering device to a R0 filter unit, and applying a R〇 membrane filtration program to send the purified water of the dialyzed R0 film to a recovery tank. For reuse. Step (E): The concentrated waste water discharged through the R0 filter unit is redirected into the first over-treatment device, and the first pass device comprises at least one hydrophobic porous thin m. Step (f): applying a fine bubble mixing treatment to the concentrated wastewater in the second filtering device to uniformly mix the concentrated wastewater and the gas into a working liquid in a milky white atomization state. Step (G): applying a vacuum suction on the water-producing side of the hydrophobic film, so that water vapor in the high-gas working liquid can easily pass through the hydrophobic film, thereby removing residual chromaticity in the working liquid and The particles are suspended to obtain a discharge water that meets the standard of the rose. According to the above-described wastewater recovery treatment method of the present invention, the adsorbent added in the pretreatment tank in the step (β) may be diatomaceous earth, activated stone or zeolite powder. According to the above-described waste water recovery treatment method of the present invention, before the step (Ε), the decolorizing agent is added to the concentrated wastewater which has been subjected to the R〇 membrane filtration treatment. According to the above-described waste water recovery treatment method of the present invention, after the step 201206838 (G), the high-concentration sludge after the discharge of the discharged water is subjected to a dehydration treatment. According to the above-described wastewater recovery treatment method of the present invention, in the step (F), when the concentrated wastewater is subjected to fine bubble mixing, the pumped gas is heated by a high temperature in advance to make the mixed working liquid Has a certain temperature. According to the above-described wastewater recovery treatment method of the present invention, the heating temperature of the working liquid is 30 ° C to 60 ° C. According to the above-described waste water recovery treatment method of the present invention, in the step (G), the operation procedure of applying condensation treatment to the water vapor molecules passing through the hydrophobic film to condense the water vapor into the discharged water is further provided. A wastewater recovery treatment system according to the present invention comprises a front treatment tank, a first filtration unit, a filtration unit, a recovery tank, a second filtration unit, a microbubble unit and a recovery tank. The pretreatment tank is for containing a predetermined capacity of dyeing and finishing wastewater. The first filtering device is disposed in the pretreatment tank, and has a horizontally disposed central tube, a plurality of hydrophilic porous membranes that are watertightly sheathed on the central tube, and the hydrophilic film is associated with the central portion The tubes are in communication such that the aqueous solution dialyzed into the hydrophilic film can be transferred to the central tube. The RG material το is connected to the water outlet end of the central pipe of the first filter device. The recovery tank is disposed on one side of the R0 transition unit for collecting and recovering the clean water liquid passing through the rib passing unit, and the second rhyme device is connected to the I-shrinking wastewater of the R0 In the discharge line, the second filtering device has a water-producing pipe that receives the concentrated wastewater and directly penetrates the center of the casing, and a plurality of equally spaced and horizontally arranged hydrophobic porous films. The microbubble device 'installed on the side of the second Wei device has a gas corresponding to the casing ^ 201206838 supplier 'to pump the pressurized gas into the concentrated waste water in the casing to promote concentration The wastewater becomes a working liquid in a milky white atomization state. The recovery tank is connected to the water outlet of the water pipe of the second passing device. According to the wastewater recovery treatment system of the present invention described above, the hydrophilic film of the first filtration device is a UF film. According to the wastewater recovery treatment system of the present invention described above, further comprising a preheating means for causing the mixed working liquid to have a certain temperature. According to the wastewater recovery treatment system of the present invention described above, further comprising a negative pressure member connected to the water production pipe of the second filtration device to form a vacuum suction force to the water-producing side of the hydrophobic film. Therefore, the present invention firstly utilizes an adsorbent to assist dehydration and filtration of the dyeing and finishing wastewater, and then pre-filters the R0 film with a hydrophilic film to reduce fouling and fouling of the R0 film, and is discharged through the R0 treatment. After the concentrated wastewater is treated by micro-bubbles, the hydrophobic film is used for solid-liquid separation, so that the chromaticity of the discharged water and the B0D Xiao C0D value can reach the current emission standard, and the hydrophobic film and the rotating method can be effectively extended. The operation cycle enables the water in the concentrated wastewater to be discharged, which is not only fast and efficient, but also can reduce the dosing and operating costs. [Embodiment] Referring to Figures 2 and 3, a first embodiment of the wastewater recovery treatment method and system thereof of the present invention comprises the following steps: Step (A). Bringing the dyeing and finishing wastewater together to attract people - front simple 1 () pending processing. Step (B): Adding an appropriate amount of adsorbent 2〇 to the pretreatment. In this embodiment, the adsorbent 20 may be diatomaceous earth, activated carbon or zeolite powder, and the liquid (4) I 2G (four) whole waste money is quickly mixed, and the color is attached to the liquid in the water. The material and the material particles are used for the decolorization and over-twisting effect of the dyeing and finishing wastewater. In addition, the pretreatment tank 1() has a -first filter split 3〇, please (4) FIG. 4, the first pass county 30 is semi-depositioned laterally disposed in the pretreatment tank 10, and Central tube with - horizontal setting
複數個水密地㈣在該巾央t31上的親水性的多孔薄膜（在本 實施例是為UF膜），且前述親水性薄膜犯是與該中央管μ形 成連通，使透析人前述親水性薄膜32内的水液馳送至該中央 管31中（該第-過渡裝置3〇的親水性薄膜⑽與中央管以的 結構是與公告第1318133號專利相類似，此不再多加賛述）。 步驟⑹：利用外部的一加壓栗浦33驅動廢水，使輔助脫 色後的廢水通過該第-魏裝置3Q的親水性_ 32過滤處 理’以降低水液中的色度及懸浮固體含量（Suspend s〇i id， SS) ’在此步驟中，透析過親水性薄膜32的水液是通過該中央 管31而被匯送至-收集槽40中等待後續處理，此外，該前處 理槽10内經過輔助脫色與過濾處理後的污泥則被排出，並經過 一污泥濃縮脫水處理，濃縮脫水後的污泥則可直接排出外界掩 埋，而脫水處理後的水份則再被抽送回該前處理槽1()内以形 成循環處理。 步驟（D):將抽送至該收集槽4〇内，且除去大部份染整色 料的水液輸送至一 R0過濾單元5〇内，以進行R〇薄膜過濾的處 理程序，此時透析過R〇薄膜產水端的乾淨水液是被匯送至一回 收槽51内，以供回收再利用。 步驟（E):將經過⑽過濾單元5〇所排出的濃縮廢水液先 加入一脫色劑後再導引入一第二過濾裝置6〇中，在本實施例 9 [、i 201206838 中’所添加入的脫色劑為NaOCl，藉以除去濃縮廢水中的殘餘 色度，該第二過濾裝置60是接設在該R0過濾單元50的濃縮廢 水排放管路52上’並具有一承接濃縮廢水的圓柱狀殼體61、 一垂直穿枢在該殼體61令央的產水管62，複數個等間隔且水 平排列的疏水性的多孔薄膜（Hydr〇ph〇bic p〇r〇us Membrane)， 前述疏水性薄膜63是由兩層的薄膜材料在邊緣施以密接封 合，且是呈扁囊狀且水平地設置在該殼體61内，並且疏水性薄 膜63内部的產水側是與該產水管62形成通連。 步驟（F):利用一微細氣泡化裝置7〇，將氣體打入該第二 過渡裝置6G的殼體61内’以進行微細氣泡化混合處理，該微 細就泡化裝置7G具有-對應該殼體61的氣體供應器71，以對 該殼體61内的濃縮廢水吹送人加黯體，促使濃水與氣體 ㈣W +成為乳白霧化狀態的工作液體8〇 ’此工作液體刖 内的水分子會因為大量曝氣而變得更細微化，相對得所產生的 蒸氣量將因此而提高。此外，該第二過濾單元6〇的產水管62 • 會在該氣體供應器71曝氣的同時，利用一外部減速機（圖未示） 的傳動下產生钱，並-體帶動套設在該產水管62外周上的疏 水性薄膜63形成轉動，用以增加與工作液體8〇的搜摔作用， 除了能提高漠縮廢水與與氣體的混合效果之外，也具有對疏水 性薄膜63產生擾動的效果，以避纽水性_ 63表面積料 塞，進而提高薄膜使用週期。而呈水平排列的疏水性薄膜⑽亦 有助於與飽合水蒸氣的工作液體8〇的接觸，以防止工作液體 内的氣泡直接逸出殼體6i外，降低產水效率。 步驟（G):在該疏水性薄膜⑽的產水側_—負麼元件= 10 201206838 90 (真空泵浦）施以負壓吸引，此時由於疏水性薄膜63只允許 水蒸氣分子通過其表面細小的孔洞631，因此，請參閱第6圖， 呈高含氣量的工作液體80中的水蒸氣便能輕易通過該疏水性 薄膜63的孔洞631，藉以分離工作液體80中的水分子與固體 懸浮微粒，而通過疏水性薄膜63的水蒸氣在產水側便會被冷凝 (可藉由在產水管62中導入冷空氣）成水體，並在該負壓元件 90唧引之下吸入該產水管62中，進而獲得符合排放標準的放 流水，此放流水可直接以由產水管62排出，或另外柚送至一容 • 器64内作儲置利用。 步驟（H):必要時，對產出放流水後的污泥通過一蒸發罐 100進行蒸餾脫水處理，使脫水後的乾燥污泥能直接進行掩埋 處理。 依據上述第一實施例之本發明廢水回收處理方法及其系 統，本發明在步驟（F)時，對濃縮廢水進行微細氣泡化混合時， 所泵送入的加壓氣體係經過一預加熱裝置110的預先高溫加 ^ 熱，使混合後的工作液體80具有一定的溫度，在本實施例中， 工作液體80的加熱溫度是以攝氏30°C〜60°C為最佳，一方面 是配合疏水性薄膜63的耐熱操作溫度條件，另一方面也能加速 工作液體80内水蒸氣的產生，使得放流水的產出能大幅地增 加。 因此，本發明先利用吸附劑20來輔助對於染整廢水的脫色 與過濾，然後以親水性薄膜進行RO膜的前置過濾，降低RO膜 污堵與結垢的情形，且經過RO處理所排出的濃縮廢水經過微細 氣泡處理後，再利用疏水性薄膜進行固液分離，使得放流水的 11 201206838 色度、BOD與COD值皆能達到目前排放標準，而採用疏水性薄 膜加上旋轉方式亦能有效地延長操作週期，使濃縮污水中的水 份能被排出，不僅快速有效率，且能降低加藥與操作成本。 如上所述，相較於以往廢水處理方法的問題，本發明之廢 水回收處理方法及其系統，具有以下功效及優點： 一、 本發明在R0薄膜過濾、程序前，先利用吸附劑20來輔 助對於染整廢水的脫水與過濾，然後以親水性薄膜32進行R0 膜的前置過濾，能降低R0膜污堵與結垢的情形，再將工作液體 # 80經過疏水性薄膜63的處理後，便能產出放流水，故能提高 染整廢水的回收處理效率。 二、 本發明將原本不能再處理的R0濃縮廢水，先經過微細 氣泡化處理之後，而形成帶有高濃度飽合水蒸氣的工作液體 80，並藉由疏水性薄膜63的設置，而使工作液體80中的水蒸 氣能輕易地通過疏水性薄膜，如此一來，便能將原本濃縮廢水 中的水液與固體分離，以產生二次脫色與過濾效果的高級化處 ^ 理，使放流水能真正地達成排放標準。 三、 本發明所採用的微細氣泡化處理搭配疏水性薄膜63， 加上疏水性薄膜63同步旋轉的動作，使得第二過濾裝置60内 的疏水性薄膜63不易積垢，而打入濃縮廢水内的氣體，更對於 工作水體形成強烈的擾動效果，防止膜面的產生污堵與濃度極 化現象之問題，更能延長操作的使用壽命性，降低成本。 四、 由於工作液體80的水份可在第二過濾裝置60的處理 下，產生脫水效果，因此由第二過濾裝置60所排出的污泥水份 含量低，可大幅降低後續蒸餾處理的時間與成本，且本發明只fa plurality of water-tight (4) hydrophilic porous films (UF film in this embodiment) on the towel center t31, and the hydrophilic film is in communication with the central tube μ to make the hydrophilic film of the dialyzer The water in the liquid 32 is sent to the central tube 31 (the structure of the hydrophilic film (10) of the first-transition device 3 and the central tube is similar to that of the publication No. 1318133, which is not mentioned more). Step (6): driving the wastewater with an external pressurized Lipu 33, so that the auxiliary decolorized wastewater is filtered by the hydrophilicity of the first Wei apparatus 3Q to reduce the color and suspended solid content in the aqueous solution (Suspend) S〇i id, SS) 'In this step, the aqueous solution dialyzed through the hydrophilic film 32 is sent to the collection tank 40 through the central tube 31 for subsequent processing, and further, the pretreatment tank 10 passes through The sludge after auxiliary decolorization and filtration treatment is discharged and subjected to a sludge concentration and dehydration treatment. The concentrated and dehydrated sludge can be directly discharged to the outside for burial, and the dehydrated water is pumped back to the pretreatment. Inside the tank 1 () to form a loop process. Step (D): pumping the liquid to the collection tank 4, and removing most of the dyed liquid to the R0 filter unit 5 to perform the R〇 membrane filtration process. The clean water flowing through the water producing end of the R〇 film is sent to a recovery tank 51 for recycling. Step (E): adding the concentrated waste water discharged through the (10) filtration unit 5〇 to a decolorizing agent, and then introducing it into a second filtering device 6〇, which is added in the embodiment 9 [, i 201206838] The decoloring agent is NaOCl, thereby removing the residual color in the concentrated wastewater. The second filtering device 60 is connected to the concentrated wastewater discharge line 52 of the RO filter unit 50 and has a cylindrical shape for receiving concentrated wastewater. a housing 61, a water-producing pipe 62 vertically pivoted in the casing 61, and a plurality of equally spaced and horizontally arranged hydrophobic porous films (Hydr〇ph〇bic p〇r〇us Membrane), the aforementioned hydrophobicity The film 63 is sealed by a two-layer film material at the edges, and is in the form of a flat capsule and horizontally disposed in the casing 61, and the water-producing side inside the hydrophobic film 63 is the water-producing pipe 62. Form a connection. Step (F): using a microbubble device 7〇 to drive a gas into the casing 61 of the second transition device 6G to perform a microbubble mixing treatment, the microbubble device 7G having a corresponding shell The gas supplier 71 of the body 61 blows the concentrated waste water in the casing 61 to the human body, and promotes the concentrated water and the gas (4) W + to become the working liquid of the milky white atomization state. It will become more subtle due to a large amount of aeration, and the amount of vapor generated will be increased accordingly. In addition, the water supply pipe 62 of the second filter unit 6 will generate money under the transmission of an external reducer (not shown) while the gas supply 71 is aerating, and the body is driven over the body. The hydrophobic film 63 on the outer circumference of the water producing pipe 62 is formed to rotate to increase the collision with the working liquid. In addition to improving the mixing effect of the desert water and the gas, it also has a disturbance to the hydrophobic film 63. The effect is to avoid the on-water _ 63 surface area plug, which in turn increases the film life cycle. The horizontally arranged hydrophobic film (10) also contributes to the contact with the working liquid of the saturated water vapor to prevent the bubbles in the working liquid from directly escaping outside the casing 6i, thereby reducing the water production efficiency. Step (G): applying a vacuum suction on the water-producing side of the hydrophobic film (10) - negative element = 10 201206838 90 (vacuum pumping), at which time the hydrophobic film 63 allows only water vapor molecules to pass through the surface thereof. The hole 631, therefore, referring to Fig. 6, the water vapor in the high-gas working liquid 80 can easily pass through the hole 631 of the hydrophobic film 63, thereby separating the water molecules and the solid aerosol in the working liquid 80. The water vapor passing through the hydrophobic film 63 is condensed on the water producing side (which can be introduced into the water producing pipe 62) into a water body, and is sucked into the water producing pipe 62 under the suction of the negative pressure member 90. In this way, the discharge water that meets the discharge standard is obtained, and the discharge water can be directly discharged from the production water pipe 62, or the other grapefruit is sent to a container 64 for storage and utilization. Step (H): If necessary, the sludge after the discharge of the discharged water is subjected to distillation dehydration treatment through an evaporation can 100, so that the dried sludge after dehydration can be directly subjected to burying treatment. According to the wastewater recycling treatment method and system of the present invention according to the first embodiment, in the step (F), when the concentrated wastewater is subjected to fine bubble mixing, the pumped pressurized gas system passes through a preheating device. The pre-high temperature heating of 110 causes the mixed working liquid 80 to have a certain temperature. In the present embodiment, the heating temperature of the working liquid 80 is preferably 30 ° C to 60 ° C. On the one hand, it is matched. The heat-resistant operating temperature conditions of the hydrophobic film 63, on the other hand, also accelerate the generation of water vapor in the working liquid 80, so that the output of the discharged water can be greatly increased. Therefore, the present invention firstly utilizes the adsorbent 20 to assist the decolorization and filtration of the dyeing and finishing wastewater, and then pre-filters the RO membrane with a hydrophilic film to reduce the fouling and scaling of the RO membrane, and is discharged by the RO treatment. After the concentrated wastewater is treated by micro-bubbles, the hydrophobic film is used for solid-liquid separation, so that the 2012 20123838 color, BOD and COD values of the discharged water can reach the current emission standard, and the hydrophobic film can also be rotated. Effectively extend the operating cycle so that the water in the concentrated sewage can be discharged, which is not only fast and efficient, but also reduces dosing and operating costs. As described above, the wastewater recycling treatment method and system thereof of the present invention have the following effects and advantages compared with the problems of the conventional wastewater treatment method: 1. The present invention utilizes the adsorbent 20 to assist the R0 membrane filtration and the procedure. For the dehydration and filtration of the dyeing and finishing wastewater, the pre-filtering of the R0 film by the hydrophilic film 32 can reduce the fouling and scaling of the R0 film, and then the working liquid #80 is treated by the hydrophobic film 63. The discharge water can be produced, so the recovery efficiency of the dyeing and finishing wastewater can be improved. 2. In the present invention, the R0 concentrated wastewater which can not be reprocessed is first subjected to microbubble treatment to form a working liquid 80 with a high concentration of saturated water vapor, and is operated by the arrangement of the hydrophobic film 63. The water vapor in the liquid 80 can easily pass through the hydrophobic film, so that the water in the originally concentrated waste water can be separated from the solid to generate secondary decolorization and filtration effects, so that the discharged water can be discharged. Can truly meet emission standards. 3. The microbubble treatment used in the present invention is combined with the hydrophobic film 63, and the hydrophobic film 63 is synchronously rotated, so that the hydrophobic film 63 in the second filtering device 60 is less likely to be fouled and is driven into the concentrated wastewater. The gas also has a strong disturbing effect on the working water body, preventing the problem of fouling and concentration polarization of the membrane surface, and further prolonging the service life and reducing the cost. 4. Since the moisture of the working liquid 80 can be dehydrated by the treatment of the second filtering device 60, the sludge discharged from the second filtering device 60 has a low moisture content, which can greatly reduce the time of subsequent distillation treatment. Cost, and the invention only f
L 201206838 需要在濃縮廢水中加入少量的脫色劑來進行殘餘脫色，所以可 以降低加藥成本，減少餘氣的環境毒害問題。 惟以上所述者，僅為本發明之一個實施例而已，當不能以 此限定本發明實施之範圍，即大凡依本發明申請專利範圍及發 明况明内容所作之簡單的等效變化與修飾，皆應仍屬本發明專 利涵蓋之範圍内。 【圖式簡單說明】L 201206838 A small amount of decolorizing agent needs to be added to the concentrated wastewater for residual decolorization, so the cost of dosing can be reduced and the environmental poisoning problem of residual gas can be reduced. However, the above is only one embodiment of the present invention, and is not intended to limit the scope of the present invention, that is, the simple equivalent changes and modifications made by the scope of the invention and the invention. All should remain within the scope of the invention patent. [Simple description of the map]
第1圖係為一方塊流程圖’說明以往染整廢水的處理流程。 第2圖係為一方塊流程圖，說明本發明廢水回收處理方法 一較佳實施例的處理流程。 第3圖係為一系統結構圖，說明本發明廢水回收再利用的 處理系統各總成裝置及管路分布情形。 第4圖係為一剖視圖，說明本發明的第一過濾裝置的剖面 結構。 $ 5圖係為-剖視圖’說明本發明的第二過濾裝置的剖面 結構。 ^第6圖係為一固液分離示意圖，說明本發明的濃縮廢水在 丄過U細^化處理後的工作液體，可釋放出大量飽合水蒸氣 並通過疏水性薄膜而形錢流水的狀態。 【主要元件符號說明】 〇 前處理槽 0 第—過濾裝置 20 吸附劑 31 中央管Fig. 1 is a block diagram showing the processing flow of the dyeing and finishing wastewater in the past. Figure 2 is a block flow diagram illustrating the process flow of a preferred embodiment of the wastewater recovery process of the present invention. Fig. 3 is a system structural diagram showing the distribution of each assembly device and piping of the treatment system for recycling and reuse of the wastewater of the present invention. Figure 4 is a cross-sectional view showing the cross-sectional structure of the first filtering device of the present invention. The Fig. 5 is a cross-sectional view showing the sectional structure of the second filtering device of the present invention. ^Fig. 6 is a schematic diagram of solid-liquid separation, illustrating the working liquid of the concentrated wastewater of the present invention after being subjected to the treatment of the finely pulverized U, which can release a large amount of saturated water vapor and form a state of flowing water through the hydrophobic film. . [Main component symbol description] 〇 Pretreatment tank 0 No. - Filter unit 20 Adsorbent 31 Central tube
LSI 13 201206838 32 ..·· 親水性薄膜 33 加壓聚浦 40 .. 收集槽 50 RO過濾單元 51 回收槽 52 排放管路 60 第二過濾裝置 61 殼體 62 產水管 63 疏水性薄膜 631 孔洞 64 容器 70 微細氣泡化裝置 71 氣體供應器 80 工作液體 90 負壓元件 100 蒸發罐 110預加熱裝置LSI 13 201206838 32 ..··· Hydrophilic film 33 Pressurized polyfluid 40 .. Collection tank 50 RO filter unit 51 Recovery tank 52 Discharge line 60 Second filter unit 61 Housing 62 Water production line 63 Hydrophobic film 631 Hole 64 Container 70 Microbubble device 71 Gas supply 80 Working liquid 90 Negative pressure element 100 Evaporation tank 110 preheating device