、發明說明： 【發明所屬之技術領域】 本發明是有關於一種產製純水及礙物質水的方法，特 別是指一種可提高生產效率的從深層海水產製逆滲透水及 礦物質水之高效能製造方法》 【先前技術】 隨著各國的人口成長與工商業的蓬勃發展，用水需求 也快速增加’在傳統水源開發的成本與技術難度都逐漸增加 ，及水資源供需嚴重不均衡的情形下，各國皆致力於尋找新 水源與開發新技術。其中’由於海水是一種幾乎可無限供水 且不受乾旱影響的水源’加上不會嚴重破壞當地生態，近來 各先進國家常採用海水淡化技術來辅助增加水資源供給量， 自1960年以來，全世界應用海水淡化技術開發的水源量也 逐年增加中，海水淡化這種取之不盡用之不竭、又經濟又環 保的供水方式’已成為世界許多水資源匮乏或不易開發新水 源的地區的一個重要水源。 海水淡化主要疋利用能源將海水分離成二部分，一部 分是含鹽極低的淡水（Fresh water)，另一部分則為含有高鹽 量的鹵水（Brine)，以此達到淡化的目的。在商業應用上，淡 化技術主要分為蒸餾法與薄膜法，淡化技術發展至今，在產 水率、耗能率、結垢、薄膜奇命延長等問題上都有突破發展 ’在應用上，由於薄膜技術日益精進，價格相對越來越低， 而逐漸成為海水淡化處理的主流。 參閱圖1，而從深層海水產製純水及礦物質水的現有製 程主要包含下列步驟： 步驟101 d菜層海水以砂遽或超過滤（uitramtration ’簡稱為UF)初步濾除雜質。 步驟1〇2疋k供一逆滲透（Reverse Osmosis，簡稱為 RO)過濾設備過濾經步驟1〇1初步處理的海水，進行離子的 過濾分離。 步驟103是將經該逆滲透過濾設備處理後的R〇透過水 (permeate)用來產製包裝為飲用水。 步驟104是將經該逆滲透過濾設備處理後的R〇濃縮水 (concentrate)回收作為電透析（Electr〇dialysis，簡稱為ED)的 原料水。 步驟105是提供一電透析設備處理R〇濃縮水以產製出 礦物質水。 雖然該現有製程已可從海水中產製飲用水與礦物質水 ，而能辅助增加供水來源，但實際上仍存有下列缺失有待改 善： 一、砂濾或超過濾只能濾除海水中的雜質，並無法濾 除多價位的離子，由於海水中的鈣離子、鎂離子及硫酸根離 子等多價位離子的離子半徑較大，且容易發生沉殿，造成 RO濾臈的結垢問題，進而導致該現有製程的R〇透過水產 量無法增大，此外，沉澱結垢的問題還會降低包裝飲用水的 產量及品質’使該現有製程相對具有產水效率較低及產品品 質較差的缺失β 二、由於砂濾或超過濾的過濾效果有限，較容易造成 1325848 R0濾膜的結垢與堵塞問題，並會因此縮短R〇濾膜的使用 壽命，而增加RO濾膜的更換頻率與消耗量，使該現有製程 的製造成本大為提高。 三、由於海水中原本就含有大量鈉離子，在未經其他 適當前處理的情況下，直接以該R〇過濾設備處理而獲得的 該RO濃縮水中也相對含有較高濃度的鈉離子，當以電透析 設備濾除鈉離子時’需要花費較高的成本，同樣使該現有製 程具有生產成本較高的缺點。 雖然目前水處理技術發展已達可應用的階段，但為節 約能源、降低生產成本與達到永續水資源的理想，仍有持續 開發新製程、新技術以均衡供水的需求。 【發明内容】 因此’本發明的目的是在提供一種可提高飲用水的產 量與品質’並能增加生產效率與降低生產成本的從深層海 水產製逆滲透水及礦物質水之高效能製造方法》 於是，本發明從深層海水產製逆滲透水及礦物質水之 高效能製造方法，包含有下列步驟： (a) 以砂濾或超過濾濾除深層海水的雜質； (b) 調整經步驟（a)處理的深層海水的酸鹼值（PH值）與總溶 解性固體濃度（Total dissolved solids，簡稱為TDS)， 以獲得一具有適當酸鹼值與總溶解性固體濃度的第一 調整液； (c) 提供一第一奈過濾（Nanofiltration，簡稱為NF)設備過 濾該第一調整液，以分別獲得一第一奈過濾透過水’ 8 及一第一奈過濾濃縮水； (d) 調整該第一奈過濾透過水的酸驗值與總溶解性固體遭 度’以獲得一具有適當酸鹼值與總溶解性固體濃度的 第二調整液； (e) k供一逆渗透過遽設備過據該第二調整液，以分別獲 得一逆滲透透過水’及一逆滲透濃縮水； (0調整該步驟（c)中所形成的該第一奈過濾濃縮水的酸驗 值與總溶解性固體濃度’以獲得一具有適當酸鹼值與 總溶解性固體濃度的第三調整液，·及 (g)對該第三調整液進行陰、陽離子電透析，以分別形成 一高濃度陰離子水、一高濃度陽離子水，及一礦物質 水。 藉此，本發明在進行逆滲透過濾之前，先以奈過濾處 理，以分別將海水中的鈣、鎂離子濃縮於該第一奈過濾濃 縮水中，及使該鈉離子濃縮於該第一奈過濾透過水中，而 可減少結垢進而增加該R0過濾設備的使用壽命，及降低該 電透析設備的分離負載而增加產水效能，使本發明之製造 方法除了可提高生產效率與降低成本外，還可増加逆滲透 水與礦物質水的品質與產量，而具有處理成效較佳的特性 與優點。 【實施方式】 本發明從深層海水產製逆滲透水及礦物質水之高效能 製造方法的前述以及其他技術内容、特點與功效，在以下 配合參考圖式的一較佳實施例的詳細說明中，將可清楚地 B25848 明白》 在本發明被詳細描述之前，要注意的是，以下的說明 内容中，分別以UF表示超過濾、NF表示奈過濾、R〇表示 逆滲透、ED表示電透析，及TDS表示總溶解性固體濃度。 參閱圖2與圖3,本發明從深層海水產製逆滲透水及礦 物質水之向效能製造方法一較佳實施例包含有下列步驟， 步驟201是對深層海水的初步處理，即以砂濾或超過 遽遽除深層海水的雜質’其所採用的深層海水是指2〇〇公 尺以下，陽光照射不到的深海水域之海水。 步驟202將經步驟2〇1處理的深層海水引導至一第一 調整槽31調整其酸鹼值與總溶解性固艎濃度，以獲得一具 有適當酸鹼值與總溶解性固體濃度的第一調整液41。 步驟203是提供一第—NF過濾設備32將鈣、鎂硫 酸根等多價離子從該第一調整液41中分離出來，以分別獲 得一第一 NF透過水42，及一含有較高濃度之鈣、鎂、硫 酸根等多價離子的第一 NF濃縮水43 ^ 步驟204是提供一第二NF過濾設備33再次將鈣、鎂 、硫酸根等多價離子從該第一 NF濃縮水43分離出來，以 分別獲得一第二NF透過水44，及一含有更高濃度之鈣、 鎂、硫酸根等多價離子的第二NF濃縮水45。 步驟205是提供—第二調整槽34，並將通過該枣一 nf 過濾設備32與該第二NF過濾設備33的第一、第二nf透 過水42、44導入該第二調整槽34，以調整其酸鹼值與總溶 10 1325848 解性固體漠度，並獲得一具有適當酸驗值與總溶解性固體 濃度的第二調整液46。 步驟206是提供一第三NF過濾設備35再進一步過濾 該步驟205中所形成的該第二調整液46,並將殘留於第二 調整液46中的鈣、鎂、硫酸根等多價離子再分離出來，以 分別獲得一第三NF透過水47，及一含有高濃度的鈣、鎂 、硫酸根等多價離子的第三NF濃縮水4S。 步驟207是提供一 R〇過濾設備36過濾通過該第三NF 過據設備35的第三NF透過水47 ’以分別獲得一 r〇透過 水49，及一 R〇濃縮水50。由於在該第三NF透過水47中 的約、鎂、硫酸根等多價離子已被前述步驟的第一 '第二 、第二NF過濾設備32、33、35濾除’該r〇過濾設備36 主要只需濾除單價的鈉離子且不易發生沉搬結垢的情形， 所以該RO透過水49的水量可以相對增大，及該R〇過濾 設備36所用的r〇濾膜的使用壽命也可以延長。 該RO過濾設備36的操作參數主要有進料壓力、透過 水回收率與分離膜材質，在該較佳實施例中，前述操作參 數的較佳範圍分別為：該進料壓力較佳為設定在7〇〇 psi〜1200 psi的範圍，該透過水回收率較佳為設定在2〇 %〜80 %的範圍，所採用的分離膜材質可以使用醋酸纖維膜 ’也可以選用由芳香族聚醯胺類所製成的薄膜，此外，該 RO過濾設備36的模組型式則可以依使用需求選用管式 (Tubular)模組、螺管式（Spiral w〇und)模組或板框式 and-frame)模组。 11 1325848 其中’將R0透過水49分流為一供直接收集的第一 r〇 分液491、一回流至該步驟202以配合形成該第一調整液 41的第二R0分液492、一回流至該步驟205以配合形成該 第一調整液46的第二R〇分液493 ’及一回流至步驟208 的第四RO分液494。 步驟208是提供一第三調整槽37,並將該第二NF濃 縮水45、第三NF濃縮水48與該第四RO分液494引導至 該第三調整槽37調整其酸鹼值與總溶解性固趙濃度，以獲 得一具有適當酸鹼值與總溶解性固體濃度的第三調整液51 〇 步驟209是提供一電透析組合體38對該第三調整液51 進行陰、陽離子電透析，以分別形成一高濃度陰離子水52 、一高濃度陽離子水53，及一礦物質水54。 該電透析組合體38包括依序相連接的一陰離子膜電透 析設備381，及一陽離子膜電透析設備382,該陰離子膜電 透析設備381以特殊陰離子膜將二價的硫酸根離子從該第 三調整液51中分離出來，以分別獲得一具低硫酸根離子濃 度的第一電透析透過水55,與高硫酸根離子濃度的該陰離 子水52，而該陽離子膜電透析設備382是以特殊陽離子膜 將納離子從該第一電透析透過水55中分離出來，以分別獲 得低納離子濃度、低硫酸根離子濃度、但高鈣離子濃度與 高鎖離子濃度的該礦物質水54,及高鈉離子濃度的該陽離 子水53»其中’該礦物質水54進一步被分流為一供直接收 集的第一礦物質分液541，及一供回流並進入該步驟2〇8的[Technical Field] The present invention relates to a method for producing pure water and material water, and more particularly to a method for producing reverse osmosis water and mineral water from deep seawater which can improve production efficiency. High-efficiency manufacturing method 【Previous technology】 With the population growth of various countries and the vigorous development of industry and commerce, the demand for water is also increasing rapidly. 'The cost and technical difficulty of traditional water source development are gradually increasing, and the situation of water supply and demand is seriously uneven. Countries are committed to finding new sources of water and developing new technologies. Among them, “Since seawater is a water source that can be almost infinitely supplied and is not affected by drought”, it will not seriously damage the local ecology. Recently, advanced countries often use desalination technology to help increase water supply. Since 1960, The amount of water developed by the world's application of desalination technology has also increased year by year. The inexhaustible, economical and environmentally-friendly water supply method of desalination has become the world's region where many water resources are scarce or difficult to develop new water sources. An important source of water. Desalination mainly uses energy to separate seawater into two parts, one is fresh water with very low salt content, and the other is high-salt brine (Brine) to achieve desalination. In commercial applications, desalination technology is mainly divided into distillation method and thin film method. The development of desalination technology has been made up to date, and there have been breakthroughs in the problems of water production rate, energy consumption rate, scaling, and prolonged film life. The technology is becoming more sophisticated, the price is relatively lower and lower, and it has gradually become the mainstream of desalination. Referring to Figure 1, the existing process for producing pure water and mineral water from deep seawater mainly comprises the following steps: Step 101: The seawater of the vegetable layer is initially filtered by sand mash or ultrafiltration (uitartration hereinafter referred to as UF). Step 1〇2疋k is used for a reverse Osmosis (RO) filtration device to filter the seawater initially treated in step 1〇1 for ion filtration separation. In step 103, the R〇 permeate treated by the reverse osmosis filtration device is used to produce a package for drinking water. In step 104, the R〇 concentrated water treated by the reverse osmosis filtration device is recovered as raw material water for electrodialysis (hereinafter referred to as ED). Step 105 is to provide an electrodialysis apparatus for treating R〇 concentrated water to produce mineral water. Although the existing process can produce drinking water and mineral water from seawater, and can help increase the source of water supply, there are still some defects to be improved: 1. Sand filtration or ultrafiltration can only filter impurities in seawater. It is impossible to filter out multi-valent ions, because the ionic radius of multivalent ions such as calcium ions, magnesium ions and sulfate ions in seawater is large, and it is easy to cause sinking, which causes scaling problems of RO filter, which leads to The R〇 permeate water production of the existing process cannot be increased. In addition, the problem of sedimentation and scaling will also reduce the yield and quality of the packaged drinking water, which makes the existing process relatively low in water production efficiency and poor in quality. Due to the limited filtration effect of sand filtration or ultrafiltration, it is easy to cause scaling and clogging of the 1325848 R0 membrane, which will shorten the service life of the R 〇 membrane and increase the frequency and consumption of the RO membrane replacement. The manufacturing cost of the existing process is greatly increased. 3. Since the seawater originally contains a large amount of sodium ions, the RO concentrated water obtained by directly treating the R〇 filtration device does not contain a relatively high concentration of sodium ions without other appropriate pretreatment. When the electrodialysis device filters out sodium ions, it requires a relatively high cost, which also makes the existing process have the disadvantage of high production cost. Although the current development of water treatment technology has reached an applicable stage, in order to save energy, reduce production costs and achieve sustainable water resources, there is still a need to continuously develop new processes and new technologies to balance water supply. SUMMARY OF THE INVENTION Therefore, the object of the present invention is to provide a high-performance manufacturing method for producing reverse osmosis water and mineral water from deep seawater while providing a production and quality that can improve the production and quality of drinking water and increase production efficiency and production cost. Therefore, the high-performance manufacturing method for producing reverse osmosis water and mineral water from deep seawater comprises the following steps: (a) filtering sand impurities or ultrafiltration to remove impurities in deep seawater; (b) adjusting steps (a) The pH value of the treated deep seawater and the total dissolved solids (TDS) to obtain a first conditioning solution having an appropriate pH value and total dissolved solids concentration. (c) providing a first nanofiltration (NF) device to filter the first conditioning liquid to obtain a first nanofiltration filtered water 8 and a first negative filtered concentrated water; (d) adjusting The first nanofiltration filter passes the acid value of the water and the total dissolved solids degree to obtain a second conditioning liquid having a suitable pH value and total dissolved solids concentration; (e) k for a reverse osmosis percolating device According to the second adjusting liquid, respectively, obtaining a reverse osmosis permeate water and a reverse osmosis concentrated water; (0 adjusting the acid value and total solubility of the first neat filtered concentrated water formed in the step (c); a solid concentration 'to obtain a third adjustment liquid having an appropriate pH value and a total dissolved solid concentration, and (g) performing an anion and a cationic electrodialysis on the third adjustment liquid to form a high concentration anion water, a high-concentration cation water, and a mineral water. Therefore, the present invention is first treated by filtration under reverse osmosis filtration to separately concentrate calcium and magnesium ions in seawater in the first-negative filtered concentrated water. And concentrating the sodium ion in the first nanofiltration through water, thereby reducing fouling and increasing the service life of the RO filter device, and reducing the separation load of the electrodialysis device to increase water production efficiency, and manufacturing the invention In addition to improving production efficiency and reducing costs, the method can also add the quality and yield of reverse osmosis water and mineral water, and has the characteristics and advantages of better treatment results. The foregoing and other technical contents, features and effects of the high-performance manufacturing method for producing reverse osmosis water and mineral water from deep seawater will be clearly clarified in the following detailed description of a preferred embodiment with reference to the drawings. B25848 Understandment Before the present invention is described in detail, it should be noted that in the following description, UF indicates superfiltration, NF indicates neva filtration, R〇 indicates reverse osmosis, ED indicates electrodialysis, and TDS indicates total dissolution. The solid concentration of the deep seawater is as follows: That is, sand filtration or impurities that exceed deep seawater's use. The deep seawater used is the seawater below 2 square meters, which is not covered by sunlight. Step 202 directs the deep seawater treated by step 2〇1 to a first adjustment tank 31 to adjust its pH value and total dissolved solid concentration to obtain a first pH having a suitable pH value and a total dissolved solid concentration. Adjustment liquid 41. Step 203 is to provide a first NF filter device 32 to separate polyvalent ions such as calcium and magnesium sulfate from the first adjustment liquid 41 to obtain a first NF permeate water 42 and a higher concentration. a first NF concentrated water of calcium, magnesium, sulfate or the like, and a first NF concentrated water 43 ^ Step 204 is to provide a second NF filtering device 33 to separate the multivalent ions of calcium, magnesium, sulfate and the like from the first NF concentrated water 43 again The second NF permeate water 44 and a second NF concentrated water 45 containing a higher concentration of calcium, magnesium, sulfate and the like are respectively obtained. Step 205 is to provide a second adjustment slot 34, and introduce the first and second nf permeating waters 42, 44 through the jujube-nf filter device 32 and the second NF filter device 33 into the second adjustment slot 34, The pH value and the total dissolved 10 1325848 cleavable solid indifference were adjusted, and a second conditioning liquid 46 having an appropriate acid test value and total dissolved solids concentration was obtained. In step 206, a third NF filtering device 35 is further provided to further filter the second adjusting liquid 46 formed in the step 205, and the polyvalent ions such as calcium, magnesium, sulfate and the like remaining in the second adjusting liquid 46 are further Separated to obtain a third NF permeate water 47, and a third NF concentrated water 4S containing a high concentration of polyvalent ions such as calcium, magnesium, sulfate, and the like. Step 207 is to provide an R〇 filtering device 36 to filter the third NF permeating water 47' passing through the third NF passing device 35 to obtain a r〇 permeating water 49 and an R〇 concentrated water 50, respectively. Since the multivalent ions of about magnesium, sulfate, and the like in the third NF permeate water 47 have been filtered by the first 'second and second NF filter devices 32, 33, 35 of the foregoing step', the r〇 filter device 36 mainly needs to filter out the monovalent sodium ions and is less prone to sinking and scaling. Therefore, the amount of water flowing through the water 49 can be relatively increased, and the service life of the r〇 filter used in the R〇 filtering device 36 is also Can be extended. The operating parameters of the RO filter device 36 mainly include feed pressure, permeate water recovery rate and separation membrane material. In the preferred embodiment, the preferred ranges of the operating parameters are: the feed pressure is preferably set at In the range of 7 〇〇 psi to 1200 psi, the permeate water recovery rate is preferably set in the range of 2% to 80%, and the separation membrane material used may be a cellulose acetate membrane or an aromatic polyamine. The film made by the class, in addition, the module type of the RO filter device 36 can be selected from the Tubular module, the Spiral w〇und module or the plate-framed and-frame according to the requirements of the use. ) Module. 11 1325848, wherein 'the R0 permeate the water 49 to be a first r〇 liquid 491 for direct collection, and a flow back to the step 202 to match the second R0 liquid 492 forming the first adjustment liquid 41, and a reflow to The step 205 is to match the second R 〇 liquid 493 ′ forming the first conditioning liquid 46 and the fourth RO liquid 494 flowing back to the step 208 . Step 208 is to provide a third adjustment tank 37, and guide the second NF concentrated water 45, the third NF concentrated water 48 and the fourth RO liquid separation 494 to the third adjustment tank 37 to adjust the pH value and total Solubility concentration to obtain a third conditioning solution having a suitable pH value and total dissolved solids concentration 51 〇 Step 209 is to provide an electrodialysis assembly 38 for anion and cation electrodialysis of the third conditioning solution 51 To form a high concentration of anionic water 52, a high concentration of cationic water 53, and a mineral water 54, respectively. The electrodialysis assembly 38 includes an anion membrane electrodialysis device 381 connected in sequence, and a cationic membrane electrodialysis device 382 that uses a special anion membrane to divalent sulfate ions from the first The three adjusting liquids 51 are separated to obtain a first electrodialysis permeate water 55 having a low sulfate ion concentration, and the anion water 52 having a high sulfate ion concentration, and the cationic membrane electrodialysis device 382 is special The cation membrane separates the nano ions from the first electrodialytic permeate water 55 to obtain the mineral water 54 having a low nano ion concentration, a low sulfate ion concentration, but a high calcium ion concentration and a high lock ion concentration, respectively, and The high sodium ion concentration of the cationic water 53» wherein the mineral water 54 is further split into a first mineral fraction 541 for direct collection, and a reflux for the step 2〇8
i S 12 1325848 第三調整槽37的第二礦物質分液542，且該第二礦物質分 液542會配合該第二NF濃縮水45、第三NF濃縮水48與 該第四R0分液494形成該第三調整液51。 較佳地’該陰離子膜電透析設備381與該陽離子膜電 透析設備382的主要操作參數包含電流、電壓與導電度， 且其較佳電流範圍為70 A〜2 A、較佳電壓範圍為80 V-10V ’及較佳導電度範圍為7〇 mS/cm〜5 mS/cm。 值得說明的是，在進入該第一、第二、第三NF過濾設 備32、33、35進行奈過濾前，先在該第一、第二、第三調 整槽31、34、37將PH值與總溶解性固體濃度調整至預定 的範圍再行過濾’則可獲得較佳的過濾效果，在該較佳實 施例中，該第一、第二、第三調整液41、46、51的PH值 的較佳調整範圍是PH3.0〜PHI 1.0，而其總溶解性固體濃度 的較佳調整範圍為5.0 g/L〜70.0 g/L。該等調整液41、46、 51的PH值可藉由習知方法進行調整，例如可以添加硫酸 、硝酸、鹽酸、氫氧化鈉、氫氧化鉀等物質來調整該等_ 整液41、46、51的PH值。而總溶解性固逋濃度則可以第 二、第三NF濃縮水45、48、第二、第三、第四R0分液 492、493、494、第二礦物質分液542相調配，並配合實施 蒸爾法、蒸發法、R〇濃縮方式、·ED濃縮方式、r〇逆滲透 水稀釋法等方法來調整。 在該較佳實施例申，步驟203、步驟204與步驟206中 所用的第一、第二、第三NF過濾設備32、33、35是以該 第一 '第二、第三調整液41、46、51的酸鹼值與總溶解性 13 i325848 固體濃度，配合調整該等NF過濾設備32、33、35的操作 參數來控制離子分離的比例與效果，所需調整的操作參數 主要為：進料壓力與透過水的回收率，其中，進料壓力較 佳為設定在50 psi〜750 psi的範圍，而透過水回收率較佳為 設定在10 %〜60 %的範圍。但不應以此限制該等nf過濾設 備32、33、35的操作參數範圍，可依實際對產品的規格與 要求進行調整。 此外’該第一、第二、第三NF過濾設備32、33.、35 皆包括至少一個相連接排列的奈過濾膜管，當該第一第 一、第二NF過濾設備32、33、35内裝設有多數支奈過濾 膜官時，該等奈過濾膜管可以並聯方式相連接，也可以串 聯方式相連接，雖然不同的排列連接方式會使離子的分離 效果不同’但仍可達到濾除多價離子的功能。其中，並聯 的濾除率與單管過濾膜管的濾除率差不多，但是藉由將多 數支過濾膜管並聯連接可增加處理的水量，而可提高製程 的生產效率。而將該等膜管串聯連接時，則由於通過該等 膜管的過濾路徑增長而可大幅提高濾除率與提升產水品質 ，但所處理的水量會與只用單支過濾膜管的水量差不多。 其中’作為進料水的深層海水原水的酸鹼值範圍是在 PH6.0〜pH8 〇，而該深層海水原水中各成份離子的濃度如下 * 氣離子（mg/L): 18,000〜23,0〇〇 納離子（mg/L) : 8,000〜1〇,〇〇〇 _ 離子（mg/L) : 300〜600 14 1325848 4040)進行逆滲透，以獲得一可供包裝飲用的R〇透過水。 以下分別在特定的RO進料壓力與回收率下比較該實驗 組與該對照組的產水量與濾除率，以進一步說明藉由本發 明製程的設計確實可提高產水效率與水質。 (實驗結果〉i S 12 1325848 The third mineral separation liquid 542 of the third adjustment tank 37, and the second mineral liquid separation liquid 542 cooperates with the second NF concentrated water 45, the third NF concentrated water 48 and the fourth R0 liquid separation 494 forms the third conditioning liquid 51. Preferably, the main operational parameters of the anion membrane electrodialysis apparatus 381 and the cationic membrane electrodialysis apparatus 382 include current, voltage and conductivity, and preferably have a current range of 70 A to 2 A, preferably a voltage range of 80. V-10V' and preferred conductivity range from 7 〇 mS/cm to 5 mS/cm. It is worth noting that before entering the first, second, and third NF filtering devices 32, 33, and 35 for filtering, the PH values are first applied to the first, second, and third adjusting grooves 31, 34, and 37. A preferred filtration effect can be obtained by adjusting the total dissolved solids concentration to a predetermined range and filtering. In the preferred embodiment, the pH of the first, second, and third conditioning liquids 41, 46, 51 The preferred range of values is from pH 3.0 to PHI 1.0, and the preferred range of total dissolved solids is from 5.0 g/L to 70.0 g/L. The pH values of the adjusting liquids 41, 46, and 51 can be adjusted by a conventional method. For example, substances such as sulfuric acid, nitric acid, hydrochloric acid, sodium hydroxide, potassium hydroxide, or the like can be added to adjust the liquids 41, 46, The pH of 51. The total dissolved solid concentration can be blended with the second and third NF concentrated waters 45, 48, the second, third, and fourth R0 liquids 492, 493, 494, and the second mineral liquid separation 542. The steaming method, the evaporation method, the R〇 concentration method, the ED concentration method, and the r〇 reverse osmosis water dilution method are used to adjust. In the preferred embodiment, the first, second, and third NF filtering devices 32, 33, and 35 used in steps 203, 204, and 206 are the first 'second and third adjusting liquids 41, 46, 51 pH value and total solubility 13 i325848 solid concentration, with adjustment of the operating parameters of these NF filtration equipment 32, 33, 35 to control the proportion and effect of ion separation, the required adjustment of the operating parameters are mainly: The feed pressure and the recovery rate of permeate water, wherein the feed pressure is preferably set in the range of 50 psi to 750 psi, and the permeate recovery rate is preferably set in the range of 10% to 60%. However, the operating parameter ranges of the nf filtering devices 32, 33, and 35 should not be limited by this, and the specifications and requirements of the products can be adjusted according to actual conditions. Furthermore, the first, second and third NF filter devices 32, 33., 35 each comprise at least one neat filter tube arranged in series, when the first first and second NF filter devices 32, 33, 35 When most of the filter membranes are installed in the interior, the membrane membrane tubes can be connected in parallel or in series. Although different arrangements of the membranes can separate the ions, the filtration can still be achieved. In addition to the function of multivalent ions. Among them, the parallel filtration rate is similar to that of the single-tube filtration membrane tube, but by connecting a plurality of filtration membrane tubes in parallel, the amount of water to be treated can be increased, and the production efficiency of the process can be improved. When the membrane tubes are connected in series, the filtration rate of the membrane tubes can be increased to greatly increase the filtration rate and improve the water production quality, but the amount of water to be treated is the same as the amount of water using only a single filtration membrane tube. almost. The pH value of the deep seawater raw water as the feed water is in the range of pH 6.0 to pH 8 〇, and the concentration of each component ion in the deep seawater raw water is as follows * Gas ion (mg/L): 18,000~23,0 Cannes (mg/L): 8,000~1〇, 〇〇〇_ ions (mg/L): 300~600 14 1325848 4040) Perform reverse osmosis to obtain a R〇 permeate water for packaging. The water production and filtration rates of the experimental group and the control group were compared under specific RO feed pressures and recovery rates, respectively, to further demonstrate that the water production efficiency and water quality can be improved by the design of the process of the present invention. (Experimental results)
表一-以相同回收率，不同進料壓力，所得到的逆滲透水產 水量。 進料壓力（psi) 800 900 1000 1100 1200 回收率（％) 20 產水量 (L/min) 對照組 UF->RO 1.42 2.12 3.03 3.71 4.24 實驗組 UF^NF^RO 3.69 4.21 4.75 5.54 6.06 產水董比值 實驗组/對照組 2.60 1.99 1.57 1.49 1.43 表二-以相同進料壓力，不同回收率，所得到的逆滲透水產 水量。 進料壓力（psi) 1000 回收率（％) 10 20 30 40 50 產水量 (L/min) 對照组 UF->RO 2.49 3.03 1.73 1.25 —— 實驗组 UF->NF-^RO —— 4.75 4.57 3.87 3.38 產水量比值 實驗組/對照組 —— 1.57 2.64 3.10 — 16 1325848 表三-以相同進料壓力，不同回收率所得到的逆滲透透過水 品質 進料壓力 (psi) 1000 回收率（％) 20 30 40 製程 對照组 UF-> RO 實驗组 UF^ NF-> RO 對照组 UF-> RO 實驗组 UF-> NF-> RO 對照组 UF-^ RO 實驗组 UF^ NF-^ RO 濾 除 率 /^S 硫睃鹽 99.62 99.98 98.98 99.97 98.41 99.92 Na 99.37 99.68 98.13 99.58 96.59 99.39 K 99.19 99.58 97.89 99.45 96.24 99.23 Ca 99.52 99.79 98.90 99.69 98.30 99.68 Mg 99.55 99.84 98.87 99.80 98.31 99.74 表四-以相同回收率，不同進料壓力所得到的逆滲透透過水 品質 進料壓力 (psi) 800 900 1000 1100 回收率（％) 20 製程 對照级 UF^ RO 實驗组 UF-> NF^ RO 對照组 UF-> RO 實驗 UF-^ NF^ RO 對照紅 UF-> RO 實驗紐 UF-> NF-> RO 對照鈒 UF^ RO 實驗組 UF-> NF-> RO 濾 除 率 S s.—✓ 硫酸鹽 99.05 99.95 99.49 99.98 99.62 99.98 99.68 99.92 Na 98.38 99.45 99.10 99.57 99.37 99.68 99.42 99.72 K 98.16 99.13 98.88 99.36 99.19 99.58 99.32 99.62 Ca 99.01 99.72 99.38 99.81 99.52 99.79 99.58 99.77 Mg 99.00 99.79 99.40 99.83 99.55 99.84 99.61 99.84Table 1 - The amount of reverse osmosis water produced by the same recovery rate and different feed pressures. Feed pressure (psi) 800 900 1000 1100 1200 Recovery (%) 20 Water production (L/min) Control group UF->RO 1.42 2.12 3.03 3.71 4.24 Experimental group UF^NF^RO 3.69 4.21 4.75 5.54 6.06 Water production Dong ratio experimental group / control group 2.60 1.99 1.57 1.49 1.43 Table 2 - The amount of reverse osmosis water produced by the same feed pressure and different recovery rates. Feed pressure (psi) 1000 Recovery (%) 10 20 30 40 50 Water production (L/min) Control group UF->RO 2.49 3.03 1.73 1.25 —— Experimental group UF->NF-^RO —— 4.75 4.57 3.87 3.38 Water production ratio experimental group / control group - 1.57 2.64 3.10 — 16 1325848 Table 3 - Reverse osmosis permeate water quality feed pressure (psi) with the same feed pressure and different recovery rate 1000 Recovery rate (% 20 30 40 Process control group UF-> RO experimental group UF^ NF-> RO control group UF-> RO experimental group UF->NF-> RO control group UF-^ RO experimental group UF^ NF -^ RO Filtration rate /^S Sulfurium salt 99.62 99.98 98.98 99.97 98.41 99.92 Na 99.37 99.68 98.13 99.58 96.59 99.39 K 99.19 99.58 97.89 99.45 96.24 99.23 Ca 99.52 99.79 98.90 99.69 98.30 99.68 Mg 99.55 99.84 98.87 99.80 98.31 99.74 Table 4 - The same recovery rate, reverse osmosis through different feed pressures. Water quality feed pressure (psi) 800 900 1000 1100 Recovery rate (%) 20 Process control level UF^ RO experimental group UF-> NF^ RO Control group UF -> RO Experiment UF-^ NF^ RO Control Red UF-> RO experiment New UF->NF-> RO control 鈒UF^ RO experimental group UF->NF-> RO filtration rate S s.—✓ Sulfate 99.05 99.95 99.49 99.98 99.62 99.98 99.68 99.92 Na 98.38 99.45 99.10 99.57 99.37 99.68 99.42 99.72 K 98.16 99.13 98.88 99.36 99.19 99.58 99.32 99.62 Ca 99.01 99.72 99.38 99.81 99.52 99.79 99.58 99.77 Mg 99.00 99.79 99.40 99.83 99.55 99.84 99.61 99.84
17 B25848 根據表一的數據顯示〖在相同的回收率（2〇%)之下，改 變進料壓力’則對照組與實驗組的產水量皆有隨著進料壓 力的增加而增多的趨勢’但在相同的回收率與進料屋力時 ’實驗組的產水量恆會大於對照組的產水量。同樣地，根 據表二的數據顯示：在相同的進料壓力（1〇〇〇 psi)下，若將 R〇透過水的回收率設定地越高，則對照組與實驗組的產水 量都有隨著回收率的增加呈現遞減的趨勢，但在相同的進 料壓力與回收率的條件下時，實驗組的產水量仍然都會大 於對照組的產水量，表示在以深層海水產製逆滲透水的過 程中，若在進行逆滲透前，加入先進行奈過濾的製程設計 ’確實有提高產水量的功效。 依表二的數據顯示：相同的進料壓力（1〇〇〇 Py)下若 將RO透過水的回收率設定地越高，則對照組所獲得的逆滲 透水中各離子的濾除率會有降低的傾向，但實驗組所獲得 的逆滲透水中各離子的濾除率幾乎不會受到回收率設定的 影響，而能穩定地維持在較高的濾除率水準（恆維持在>99% 的濾除率）上，且在相同的進料壓力與回收率時，實驗組的 濾除率恆大於對照組的濾除率。同樣地，依表四的數據顯 示：在相同的回收率（20%)之下，改變進料壓力，則對照組 所獲得逆滲透水中各離子的濾除率有隨著進料壓力的增加 而增進其濾除率的趨勢，但實驗組所獲得逆滲透水中各離 子的濾除率則是穩定地維持在較高的濾除率水準（恆維持 >99%的濾除率）上，且在相同的進料壓力與回收率時，實驗 組的滤除率也都會大於對照組的濾除率。表示本發明藉由 18 I325848 在製程中加入奈過濾的步驟，確實可提高逆滲透過濾透過 水中離子的據除率，而且即使改變進料壓力與回收率，所 得到的離子濾除率都能穩定地維持在大於99%的高標準上 ’進而使本發明相對現有製程可產製出具有較佳的水質的 飲用水。 綜合表一、表二、表三、表四的結果，顯然可以看出 在相同進料壓力與相同回收率的條件下，實驗組會比對照 組產製較多的水量’且所產製水中的各離子濾除率都可達 到99%以上，而具有較佳的水質，所以本發明製造方法的 製程設計確實有可提高產水量與產水品質的效果。 值得一提的是，在相同的單位電能下，現有製程的R〇 逆滲透水回收率是在20%〜30%，本發明製造方法則可將該 回收率提高至45%〜50%，而相對具有較高的效能。 歸納上述’本發明從深層海水產製逆滲透水及礦物質 水之高效能製造方法可獲致下述的功效及優點，故確實能 達到本發明的目的： 一、本發明在進行超過濾之後，先進行奈過濾，再進 行逆滲透的製程設計’使大部分的多價離子都在奈過濾的 階段就被遽除，到逆滲透階段時，只要再將單價的鈉離子 渡除就可產製RO透過水’可有效減少多價離子在逆滲透設 備的渡膜沉殺結垢的情形，並使R〇透過水的產水量相對增 多，並能減少多價離子污染R〇透過水的純度等問題，使本 發明的製造方法相對可達到較高的產水量（R〇透過水）與較 佳的產水品質。 19 1325848 二、 配合額外新增奈過滤的前置處理，有效阻擒多價 離子進入逆滲透過濾設備，而較不易在逆滲透啜備所用的 滤膜造成沉殿與堵塞問題’使逆滲透過濾設借的遽膜的使 用壽命可大幅延長，而可減少濾膜的更換頻率與消耗量， 使本發明的製造方法具有較節省製造成本的優點。 三、 深層海水經奈過濾後，被奈過濾設備濾除的奈過 濾濃縮水已將多價的鈣、鎂離子濃縮，使電透析設備在製 造礦物質水時，可以提高生產效率’同時，未被奈過濾設 備濾除的單價鈉離子則大多集中在逆滲透過濾濾除，進入 電透析設備的鈉離子相對較少，而可降低電透析設備分離 鈉陽離子的負載’同樣可使本發明的製造方法具有較高的 產水（礦物質水）效率與較節省電透析設備能源的優點》 惟以上所述者，僅為本發明之一較佳實施例而已，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 利範圍及發明說明内容所作之簡單的等效變化與修飾，皆 仍屬本發明專利涵蓋之範圍内。 【圖式簡單說明】 圖1是現有製程從深層海水產製純水及礦物質水的一 流程圖； 圖2是本發明從深層海水產製逆滲透水及礦物質水之 高效能製造方法一較佳實施例的一流程圖；及 圖3是該較佳實施例的一製程流程與配置示意圖。 20 132584817 B25848 According to the data in Table 1, it is shown that under the same recovery rate (2〇%), the feed pressure is changed, then the water production of both the control group and the experimental group increases with the increase of the feed pressure. However, in the same recovery rate and feed force, the water production of the experimental group will always be greater than that of the control group. Similarly, according to the data in Table 2, under the same feed pressure (1 psi), if the recovery rate of R〇 permeate water is set higher, both the control group and the experimental group have water production. As the recovery rate shows a decreasing trend, under the same feed pressure and recovery conditions, the water production of the experimental group will still be greater than the water production of the control group, indicating that the reverse osmosis water is produced in deep seawater. In the process of adding, before the reverse osmosis, the process design of adding the first filtration process does have the effect of increasing the water production. According to the data in Table 2, if the recovery rate of RO permeate water is set higher under the same feed pressure (1〇〇〇Py), the filtration rate of each ion in the reverse osmosis water obtained by the control group will be The tendency to decrease, but the filtration rate of each ion in the reverse osmosis water obtained by the experimental group is hardly affected by the recovery rate setting, and can be stably maintained at a high filtration rate level (constantly maintained at > 99%) The filtration rate of the experimental group was always greater than the filtration rate of the control group at the same filtration pressure and recovery rate. Similarly, according to the data in Table 4, under the same recovery rate (20%), changing the feed pressure, the filtration rate of each ion in the reverse osmosis water obtained by the control group increases with the feed pressure. The tendency of the filtration rate was improved, but the filtration rate of each ion in the reverse osmosis water obtained by the experimental group was stably maintained at a high filtration rate level (constant maintenance > 99% filtration rate), and At the same feed pressure and recovery rate, the filtration rate of the experimental group was also greater than the filtration rate of the control group. It is indicated that the step of adding the nanofiltration in the process by the 18 I325848 in the present invention can indeed improve the removal rate of ions in the reverse osmosis filtration through the water, and the ion filtration rate can be stabilized even if the feed pressure and recovery rate are changed. The ground is maintained at a high standard of greater than 99%, which in turn allows the present invention to produce drinking water having better water quality than existing processes. Based on the results of Table 1, Table 2, Table 3 and Table 4, it can be clearly seen that under the same feed pressure and the same recovery rate, the experimental group will produce more water than the control group' and produce water. The ion filtration rate of each ion can reach 99% or more, and has better water quality. Therefore, the process design of the manufacturing method of the present invention has an effect of improving water production and water quality. It is worth mentioning that under the same unit electric energy, the R 〇 reverse osmosis water recovery rate of the existing process is 20% to 30%, and the manufacturing method of the present invention can increase the recovery rate to 45% to 50%, and Relatively high performance. In summary, the above-mentioned high-efficiency manufacturing method for producing reverse osmosis water and mineral water from deep seawater can achieve the following effects and advantages, so that the object of the present invention can be achieved: 1. After the ultrafiltration is performed in the present invention, First, we carry out the filtration process of reverse osmosis, and then carry out the process design of reverse osmosis, so that most of the multivalent ions are removed at the stage of filtration, and when the reverse osmosis phase is used, the sodium ions of the monovalent ion can be removed. RO through water' can effectively reduce the scale of multi-valent ions in the membrane of reverse osmosis equipment, and increase the amount of water produced by R〇 through water, and can reduce the purity of multivalent ions, R〇 permeate water, etc. The problem is that the manufacturing method of the present invention can achieve a relatively high water yield (R 〇 permeate water) and a preferred water quality. 19 1325848 Second, with the additional pre-treatment of the new filter, effectively blocking the multi-valent ions into the reverse osmosis filtration equipment, and it is not easy to cause the sinking and clogging problems in the membrane used in reverse osmosis preparation. The service life of the entangled enamel film can be greatly extended, and the frequency and consumption of the filter membrane can be reduced, so that the manufacturing method of the present invention has the advantage of saving manufacturing cost. 3. After the deep seawater is filtered by Nai, the filtered concentrated water filtered by the Nai filtration equipment has concentrated the multivalent calcium and magnesium ions, so that the electrodialysis equipment can improve the production efficiency when manufacturing mineral water. The monovalent sodium ions filtered by the nanofiltration equipment are mostly concentrated in reverse osmosis filtration, and the sodium ions entering the electrodialysis equipment are relatively small, and the load of separating the sodium cations from the electrodialysis equipment can be reduced. The method has the advantages of high water production (mineral water) efficiency and energy saving of the electrodialysis equipment. However, the above description is only a preferred embodiment of the present invention, and the present invention cannot be limited thereto. Scope, that is, the simple equivalent changes and modifications made by the present invention in the scope of the invention and the scope of the invention are still within the scope of the invention. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a flow chart of a conventional process for producing pure water and mineral water from deep seawater; FIG. 2 is a high-performance manufacturing method for producing reverse osmosis water and mineral water from deep seawater according to the present invention; A flowchart of the preferred embodiment; and FIG. 3 is a schematic diagram of a process flow and configuration of the preferred embodiment. 20 1325848
【主要元件符號說明】 31……第一調整槽 32……第一 NF設備 33……第二NF設備 34……第二調整槽 35……第三NF設備 36……R0過濾設備 37……第三調整槽 38……電透析組合體 381 •…陰離子膜電透析設備 382••…陽離子膜電透析設備 41……第一調整液 42……第一 NF透過水 43……第一 NF濃縮水 44……第二NF透過水 45……第二NF濃縮水 46……第二調整液 47……第三NF透過水 48……第三NF濃缩水 49……RO透過水 491…第一 R0分液 492…第二R0分液 493 ····第三R0分液 494 —第四R0分液 50……RO濃縮水 51……第三調整液 52……高濃度陰離子水 53……高濃度陽離子水 54……礦物質水 541 ····第一礦物質分液 542 ····第二礦物質分液 55......第一電透析透過水[Main component symbol description] 31...first adjustment slot 32...first NF device 33...second NF device 34...second adjustment slot 35...third NF device 36...R0 filter device 37... Third adjustment tank 38...electrodialysis assembly 381 •... anion membrane electrodialysis device 382••...cation membrane electrodialysis device 41...first adjustment liquid 42...first NF permeate water 43...first NF concentration Water 44...second NF permeate water 45...second NF concentrated water 46...second adjustment liquid 47...third NF permeate water 48...third NF concentrated water 49...RO permeate water 491...first R0 liquid separation 492... second R0 liquid separation 493 ···· third R0 liquid separation 494 — fourth R0 liquid separation 50...RO concentrated water 51...third adjustment liquid 52...high concentration anion water 53... High concentration of cationic water 54...mineral water 541 ····first mineral liquid separation 542 ····Second mineral liquid separation 55...first electrodialysis permeate water
21twenty one