201228944 六、發明說明： 【發明所屬之技術領域】 I本發明是有關於一種海水濃縮液及海水礦物質粉末的 衣備方法，特別是指—種利用海水為原料並經由電透析處 理、濃縮處理及分離處理來製備海水濃縮液及海水礦物質 粉末的製備方法》 ' 【先前技術】 近年來深層海水成為目前世界開發的主要重點，透過 深層海水的處理可萃取出豐富且潔淨Μ物質及微量元素， 可供現代人補^日常攝取礦物質的不^。深層海水之所以富 3礦物質’主要疋因為陽光不能穿透，光合作用無法發生， 使付無機營養鹽未被浮游植物消耗，和表層海水比較起來深 層海水有較高含量的無機#養鹽4於含有f富的無機營養 鹽’深層海水目前廣為被應用於保健飲料、食品、醫藥產品 及水產養瘦。 目前深層海水可經由蒸館法、逆滲透法或電透析法等 處理後可獲得純水、礦物質水及低鹽的海水濃縮液。該純水 可做為人類-般的飲用水，而礦物質水及低鹽的海水濃縮液 可做為補充人體所需之礦物質的來源。然，該蒸餾法需設備 體積龐大，且需於高溫的環境中進行；而該逆滲透法會無區 別地滤過水中所有的溶質及離子，所以不適合絲選擇性遽 除深層海水中的離子，且過程中會有海水渗出之現象，大幅 影響脫鹽水的水質，故目前僅適用來移除鈉離子的處理；而田 電透析法f耗用大量的電能’且隨著海水變淡水所造成的電 201228944 阻增加，電流強度無法提升而影響效能，此外，當海水所含 的總溶解固體量較高，若以該電透析法處理海水，則每噸水 耗費的電量會較該逆滲透法高，不符合經濟效益。再者，該 逆滲透法及電透析法是透過離子膜來達到分離海水中各礦物 質或淡化海水的方法，隨著長時間的使用，該離子膜會產生 結垢、堵塞和劣化等的現象’且不易製造出各種不同含量配 比之礦物質。 CN101121548 A公開號揭示一種採用低溫真空結晶方法 從海洋深層水有效提取高純度礦物質方法。該製法透過加熱 濃縮方式將深層海水進行濃縮分別分離出鈣鹽、鈉鹽、硫酸 鹽及含有鉀鹽及鎂鹽的混合鹽漿液，進一步將該混合鹽漿液 以水洗滌分別得到含有鎂鹽的溶液及鉀鹽，接著將含有鎂鹽 的溶液經由濃縮及過濾得到一高純度之含有鎂鹽的溶液。 然，該製法所得之鈣鹽含有難溶於水的硫酸鈣及碳酸鈣，而 會減少水溶性鈣鹽的取得，且其鈣鹽較無實用性不利於人體 吸收。 因此’以目前市場需求的趨勢來看，有必要發展出一 種製備方法，其能製備出低含量的硫酸根離子及鈉離子，且 含有高含量鎂離子與鈣離子之海水濃縮液，更進一步地能以 粉末型態存在之海水礦物質粉末。 【發明内容】 該冰層海水被應用於製造保健飲料、食品、醫藥等產 品時，必須先移除對人體健康有害的離子，如硫酸根離子及 鈉離子，此外，為了符合產品規格要求，所需離子含量比例 201228944 的調整也是必要的過程ϋ 了同時能達到硫酸根離子及201228944 VI. Description of the invention: [Technical field to which the invention pertains] I The present invention relates to a method for preparing a seawater concentrate and a seawater mineral powder, in particular to a seawater-based material and subjected to electrodialysis treatment and concentration treatment. And separation treatment to prepare seawater concentrate and seawater mineral powder preparation method ''[Prior Art] In recent years, deep seawater has become the main focus of the world development, and deep seawater treatment can extract rich and clean impurities and trace elements. , for modern people to make up ^ daily intake of minerals ^. The reason why the deep seawater is rich in 3 minerals is mainly because the sunlight cannot penetrate, the photosynthesis cannot occur, so that the inorganic nutrient salt is not consumed by the phytoplankton, and the deep seawater has a higher content of inorganic salt than the surface seawater. Deep seawater, which contains f-rich inorganic nutrient salts, is currently widely used in health drinks, food, pharmaceutical products and aquaculture. At present, deep seawater can be treated by steaming, reverse osmosis or electrodialysis to obtain pure water, mineral water and low-salt seawater concentrate. The pure water can be used as human-like drinking water, while mineral water and low-salt seawater concentrate can be used as a source of minerals needed to supplement the body. However, the distillation method requires a large volume of equipment and needs to be carried out in a high temperature environment; and the reverse osmosis method filters all the solute and ions in the water indiscriminately, so it is not suitable for the silk to selectively remove ions in the deep seawater. In the process, there will be seawater seepage, which greatly affects the water quality of desalinated water. Therefore, it is only suitable for the treatment of removing sodium ions. The field electrodialysis method f consumes a large amount of electric energy' and is caused by the freshwater water. The electric energy of 201228944 increases, the current intensity can not be increased and affects the efficiency. In addition, when the total dissolved solids content of seawater is high, if the seawater is treated by the electrodialysis method, the electricity consumption per ton of water will be higher than that of the reverse osmosis method. High, not in line with economic benefits. Furthermore, the reverse osmosis method and the electrodialysis method are methods for separating various minerals or desalinating seawater in seawater through an ion membrane, and the ionic membrane may cause scale, clogging, and deterioration with a long period of use. 'It is not easy to produce minerals of various content ratios. CN101121548 A discloses a method for efficiently extracting high-purity minerals from deep ocean water using a low-temperature vacuum crystallization method. The method comprises the steps of: concentrating the deep seawater by heating and concentrating to separate the calcium salt, the sodium salt, the sulfate salt and the mixed salt slurry containing the potassium salt and the magnesium salt, and further washing the mixed salt slurry with water to obtain a solution containing the magnesium salt. And a potassium salt, and then the solution containing the magnesium salt is concentrated and filtered to obtain a high-purity magnesium salt-containing solution. However, the calcium salt obtained by the method contains calcium sulfate and calcium carbonate which are hardly soluble in water, and the water-soluble calcium salt is reduced, and the calcium salt is not practically harmful to the human body. Therefore, in view of the current market demand trend, it is necessary to develop a preparation method capable of preparing a low content of sulfate ion and sodium ion, and containing a high concentration of magnesium ion and calcium ion seawater concentrate, further A seawater mineral powder that can be present in a powder form. SUMMARY OF THE INVENTION When the ice layer seawater is used in the manufacture of health drinks, foods, medicines, and the like, it is necessary to remove ions harmful to human health, such as sulfate ions and sodium ions, and in addition, in order to meet product specifications, The adjustment of the ion content ratio 201228944 is also a necessary process to achieve sulfate ion and
1 + + ϋ ’且㈣子與每離子含量高的需求，本案發明 人=由先將L;自水進行電透析處理以除去硫酸根離子，避 免&酸根離子與㈣成硫酸辦，進而於後續再經由濃縮處理 刀離處理時可減少軒離子的損失，並且依序可獲得不同的 =物質鹽及海水漠縮液，進—步的還可將該海水濃縮液經由 /辰縮處理獲得—具有水溶性特性的海水礦物質粉末。 制因此’本發明之第—目# ’即在提供—海水濃縮液的 衣備方法，肖方法製備出的海水濃縮液具有低含量的硫酸 離子及鈉離子且同時含有高含量的鈣離子及鎂離子。 於是，本發明海水濃縮液的製造方法係包含以 · / • :〇)對硬度範圍為13,88〇〜22，刪的濃縮滷水利用二 丢離子骧進行電透析處理，以得到一脫除硫酸根礦物質 艮基於s亥脫除硫酸根礦物質水的硬度為100，其中的硫酸 根離子濃度範圍為10Ppm以下； (b)對該步驟（a)之脫除硫酸根礦物質水施予一濃縮處理 及分離處理，取得一具有鎂離子濃度範圍大於15,4〇〇ppm 之過渡溶液及鈣鹽；及 (0對該步驟（b)之過渡溶液施予一濃縮處理及一分離處 王甲 取知一具有鎂離子濃度範圍大於99,〇〇〇ppm之海水濃 知百液及一鈉鹽與鉀鹽之混合物。 本發明之第二目的，即在提供一種海水礦物質粉末的 製備方法，該方法製備出的海水礦物質粉末具有低含量的 201228944 硫酸根離子及鈉離子且同時含有高含量的妈離子及鎂離 子，且該海水礦物質粉末為一水溶性礦物質粉末。 於是，本發明海水礦物質粉末的製備方法其係對一如 上所述之海水濃縮液的製備方法製得的海水濃縮液施予一 後置濃縮處理而製得。 本發明之功效在於：藉由二價陰離子膜進行電透析處 理先將硫酸根離子移除，關後續處料減少約離子的損 失。再者，、經由濃縮及分離處理可依序獲得不同的礦物質 鹽、不同礦物質含量配比的海水濃縮液及海水礦物質粉 末，且該等礦物質鹽及該海水礦物質粉末皆具有水溶性， 有利於人體吸收，故確實能達到本發明的功效。 【實施方式】 本發明中所述的硬度是指以感應偶合電漿原子發射光 。日法（ICP法）測得的硬度，而本案具體實施例是以一感應 偶合電毁原子發射光譜儀（ICP-OES)進行硬度的量測。 本發明海水濃縮液的製備方法包含以下步驟： (a) 對一硬度範圍為13,88〇〜22,〇〇〇的濃縮滷水利用二 價陰離子膜進行電透析處理，以得到一脫除硫酸根礦物質 水，基於該脫除硫酸根礦物質水的硬度為1〇〇，該硫酸根離 子濃度範圍為1 Oppm以下； (b) 對該步驟（a)之脫除硫酸根礦物質水施予一濃縮處理 及一分離處理，取得一具有鎂離子濃度範圍大於15,4〇〇ppm 之過渡溶液及鈣鹽；及 (c) 對該步驟（b)之第一溶夜施予一濃縮處理及一分離處 201228944 理，取得—具有鎂離子濃度範圍大於99,刪ppm之海水濃 縮液及一鈉鹽與鉀鹽之混合物。 較佳地’該步驟⑷的濃縮滷水是藉由先將海水經過前 處理取得一具有55〇〇以上之硬度的礦物f鹽水，再對該礦 物質鹽水施予一前置濃縮處理而製得的。 該前處理的方式並沒有特別的限制，目的在於減少海 水中的>5染物，其方式可採用一般的過遽方式及逆渗透方 式。該礦物質鹽水的硬度範圍為55〇〇〜7_，目的在於讓 鈣離子及鎮離子含置在一定範圍内，以利後續可獲得高轉 鎂含量之海水濃縮液或海水礦物質粉末。該前置濃縮處理 的方式並沒有特別的限制，可採用_般的低溫真空濃㈣ 式或冷床法’將該礦物質鹽水進行濃縮減少體積，目的在 於使後續電透析處理時可減少消耗的能量與時間。本發明 之一具體例中，該礦物質鹽水的硬度為9，100,且其中的硫 酸根離子濃度為4,563 ppm、鈉離子濃度為14,89〇 ppm、鉀 離子濃度為549 ppm、㈣子濃度為548 5啊及鎂離子濃 度為 1，843 ppm。 ^佳地’在該步驟⑷的濃縮滴水中’該硫酸根離子濃 又I巳圍為9，GGG ppm〜！！，〇〇() ppm、該鈉離子濃度範圍為 2〇,790ppm〜43，G3G ppm、該卸離子濃度範圍為⑷㈣〜 ι，8〇2順、該_子濃度範圍為防ppm〜M55 5 p㈣、 該鎮離子濃度範㈣2,849 ppm〜6,684 ppm及硬度範圍為 ’ 0 31，71G。本發明之一具體例中，在該步驟⑷的濃縮 滷水中’該硫酸根離子濃度$ 1〇,951 ppm、該鈉離子濃度 201228944 為37,028 ppm、該鉀離子濃度為yin ppm、該鈣離子濃度 為1,455.5 ppm、該鎂離子濃度為4，108 ppm及硬度範圍為 20，.892。 在該步驟（a)中，該濃縮滷水利用二價陰離子膜進行電 透析處理的主要目的在於將硫酸根離子移除，因為硫酸根 離子會與水中的鈣離子形成難溶於水的硫酸鈣而析出，使 得鈣離子含量減少，再者，當高含量的硫酸鹽存在於飲用 水中除了有苦溫味外，還會導致腹瀉對人體有害，故需先 除去硫酸根離子。且同時為了能夠使鈣離子生成的鹽類能 以易溶於水的氣化鈣為主以利人體吸收，故更需將硫酸根 離子移除避免形成難溶於水的硫酸辦。 較佳地’該二價陰離子膜是在一選擇性薄膜表面上塗 佈一高分子層（permselective p〇lymeric iayer)，而使其具有 移除二價陰離子的選擇性。其作用原理是利用立體排斥 (steric-repulsion)的方式，對於離子的大小不同或價數不 同，產生不同的輸送阻力，以達到具有移除二價陰離子選 擇性的效用。本發明之一具體例中，該二價陰離子膜由 Asahi Glass Engineering Co.，Ltd 公司製，其型號為1 + + ϋ 'and (four) sub- and high per ion content demand, the inventor of this case = by first L; from the water electrodialysis treatment to remove sulfate ions, avoid & acid ions and (four) into sulfuric acid, and then Subsequent treatment with a concentrated treatment knife can reduce the loss of Xuan ion, and sequentially obtain different = substance salt and seawater desertification liquid, and further obtain the seawater concentrate through the /-shrinking treatment - A seawater mineral powder having water-soluble properties. Therefore, the first method of the present invention provides a method for preparing a seawater concentrate, and the seawater concentrate prepared by the method has a low content of sulfate ions and sodium ions and contains a high content of calcium ions and magnesium. ion. Therefore, the method for producing a seawater concentrate according to the present invention comprises: ··· :〇) for a hardness range of 13,88〇22, and the concentrated brine is subjected to electrodialysis treatment using two ions, to obtain a sulfuric acid removal catalyst. The root mineral 艮 is based on shai, and the hardness of the sulphate mineral water is 100, wherein the sulfate ion concentration ranges below 10 Ppm; (b) the sulfated mineral water is removed from the step (a). Concentration treatment and separation treatment, obtaining a transition solution and a calcium salt having a magnesium ion concentration range of more than 15, 4 〇〇 ppm; and (0) applying a concentration treatment to the transition solution of the step (b) and a separation point A second object of the present invention is to provide a seawater mineral powder preparation method, which has a magnesium ion concentration range of more than 99, 〇〇〇ppm, and a mixture of a sodium salt and a potassium salt. The seawater mineral powder prepared by the method has a low content of 201228944 sulfate ion and sodium ion and contains a high content of mother ions and magnesium ions, and the seawater mineral powder is a water-soluble mineral powder. The invention discloses a method for preparing a seawater mineral powder, which is obtained by subjecting a seawater concentrate prepared by the method for preparing a seawater concentrate as described above to a post-concentration treatment. The effect of the invention is: by a divalent anion The membrane is subjected to electrodialysis treatment to remove the sulfate ion first, and the subsequent treatment reduces the loss of about ions. Further, through the concentration and separation treatment, different mineral salts and seawater with different mineral content ratios can be sequentially obtained. The concentrate and the seawater mineral powder, and the mineral salt and the seawater mineral powder are all water-soluble and are beneficial to the human body to absorb, so that the efficacy of the present invention can be achieved. [Embodiment] The hardness described in the present invention It refers to the hardness measured by the induction coupling of the plasma atom, the Japanese method (ICP method), and the specific embodiment of the present invention is the measurement of the hardness by an inductively coupled electric atomic emission atomic emission spectrometer (ICP-OES). The preparation method of the seawater concentrate comprises the following steps: (a) For a concentrated brine having a hardness ranging from 13,88 〇22 to 22, the concentrated brine of bismuth is electrodialyzed by a divalent anion membrane. Treating to obtain a sulfate-removing mineral water, the hardness of the sulfate-based mineral water is 1 〇〇, and the sulfate ion concentration ranges below 1 Oppm; (b) the step (a) Removing the sulfate mineral water and applying a concentration treatment and a separation treatment to obtain a transition solution and a calcium salt having a magnesium ion concentration range of more than 15,4 ppm; and (c) the step (b) A concentrated night treatment is applied to a concentration treatment and a separation point 201228944 to obtain a mixture having a magnesium ion concentration range greater than 99, a ppm seawater concentrate and a monosodium salt and a potassium salt. Preferably, the concentration of the step (4) is concentrated. The brine is obtained by first pretreating the seawater to obtain a mineral f brine having a hardness of 55 〇〇 or more, and then applying a preconcentration treatment to the mineral brine. The pretreatment method is not particularly limited, and the purpose is to reduce the <5 dye in the seawater by a general method of over-twisting and reverse osmosis. The mineral salt water has a hardness ranging from 55 〇〇 to 7 _, and the purpose is to set the calcium ion and the town ion content within a certain range, so as to obtain a seawater concentrate or seawater mineral powder with a high magnesium content. The method of the preconcentration treatment is not particularly limited, and the mineral salt water can be concentrated and reduced in volume by a low temperature vacuum concentration (four) or a cold bed method, in order to reduce the consumption in the subsequent electrodialysis treatment. Energy and time. In one embodiment of the present invention, the mineral salt water has a hardness of 9,100, and the sulfate ion concentration thereof is 4,563 ppm, the sodium ion concentration is 14,89 〇ppm, the potassium ion concentration is 549 ppm, and the (four) sub-concentration It has a concentration of 548 5 and a magnesium ion of 1,843 ppm. ^佳地' in the concentrated drip of the step (4) 'The sulfate ion is concentrated and the I 巳 is 9, GGG ppm~! ! , 〇〇 () ppm, the sodium ion concentration range is 2 〇, 790ppm~43, G3G ppm, the unloading ion concentration range is (4) (four) ~ ι, 8 〇 2 cis, the _ sub-concentration range is anti-ppm ~ M55 5 p (four) The town ion concentration range (4) 2,849 ppm~6,684 ppm and the hardness range is '0 31,71G. In one embodiment of the present invention, the sulfate ion concentration in the concentrated brine of the step (4) is 〇1,951 ppm, the sodium ion concentration 201228944 is 37,028 ppm, the potassium ion concentration is yin ppm, and the calcium ion concentration is It is 1,455.5 ppm, the magnesium ion concentration is 4,108 ppm, and the hardness range is 20,.892. In this step (a), the main purpose of the electrodialysis treatment of the concentrated brine using the dianion membrane is to remove the sulfate ions, because the sulfate ions form calcium-insoluble calcium sulfate with calcium ions in the water. Precipitation causes a decrease in calcium ion content. Furthermore, when high levels of sulfate are present in drinking water, in addition to bitterness and warmth, diarrhea is harmful to the human body, so it is necessary to remove sulfate ions first. At the same time, in order to enable the calcium-forming salts to be mainly soluble in water-soluble calcium to facilitate absorption by the human body, it is more necessary to remove the sulfate ions to avoid formation of water-insoluble sulfuric acid. Preferably, the divalent anion membrane is coated with a polymer layer on a surface of the selective film to impart selectivity for removal of the dianion. The principle of action is to use steric-repulsion to produce different transport resistances for different ion sizes or valences to achieve the effect of removing dianion selectivity. In one embodiment of the present invention, the dianion film is manufactured by Asahi Glass Engineering Co., Ltd.
Selemion ASV anion-exchange membrane。 為了獲得最佳的選擇性濾除效果，進料的壓力需加以 限定，壓力太低則會拖長處理的時間，且該離子膜的表層 孔隙度將不會處於最佳的選擇性濾除狀態；壓力太高則會 降低選擇性遽除離子的能力，且會使水產生電解現象，並 產生不必要的副產物。較佳地’該步驟（3)的電透析處理的 201228944 操作電壓範圍為5 V〜15 V。較佳地，該電透析處理的操作 電流範圍為小於10.5A。較佳地，該電透析處理的流速壓力 為lOOpsi。較佳地，該電透析處理的液體溫度範圍為小於 25°C，因為電透析膜本身有一個範圍的操作溫度，在範圍 外溫度操作會影響膜的使用壽命。本發明之一具體例中， 該電透析處理的操作電壓為12.5 V、操作電流為小於 10.5A、流速壓力為i〇〇pSi及液體溫度為25。〇。 較佳地，該步驟（a)的脫除硫酸根礦物質水的硬度範圍 為16,000〜20,000，且其中的鈉離子濃度範圍為32〇〇〇 ppm 〜40,000 ppm、該鉀離子濃度範圍為丨，28〇 ppm〜 ι，6〇〇 ppm '該鈣離子濃度範圍為Layppm、該鎂離 子濃度範圍為3,216 ppm〜4,020 ppm及該硫酸根離子濃度 範圍為473 ppm至591 ppm。基於該脫除硫酸根礦物質水的 硬度為100，該硫酸根離子濃度範圍為2 36〜3.7 ppm[計算 方式為（100/該脫除硫酸根礦物質水的硬度）χ各離子濃度 (ppm)]。本發明之一具體例中，在該步驟的脫除硫酸根 礦物質水中，該硫酸根離子濃度為532 ppm、該鈉離子濃度 為36,068 ppm、該鉀離子濃度為144〇 2 ppm、該鈣離子濃 度為1，403_5 ppm、該鎂離子濃度為3,618 ppm及硬度範圍 為18,704 ’且基於該脫除硫酸根礦物質水的硬度為1〇〇，該 硫酸根離子濃度為2.84 ppm。 經目前研究後發現，海水中的化學成分及含量與人體 血液中的化學成分及含量幾乎相同，若鎂離子與鈣離子含 量比例與海水相同（即鎂與|弓比例約3/1 )，則對於消費者使 201228944 用會較為方便並有助於人體大量吸收。較佳地，該步驟 的脫除硫酸根礦物質水的鎂鈣含量比例為2/1至10/1之 間。 該步驟（b)及（c)的濃縮處理方式並沒有特別的限制，較 佳地’該步驟（b)及（c)的濃縮處理方式是選自於低溫真空濃 縮方式或冷凍法。本發明之一具體例中，該濃縮處理方式 是採用低溫真空濃縮方式，透過降低濃縮處理方式的壓 力’可以降低§亥脫除硫酸根礦物質水及該過渡溶液的沸 點’好處是濃縮槽只需要將水加熱至50。(：〜70。(：，不需要 加熱到其彿點就可以使該脫除硫酸根礦物質水及該過渡溶 液中的水蒸發’這可以減少濃縮槽之蒸氣使用量，大幅降 低耗能；此外，控制溫度在50ec〜7〇°c則是為了避免過高 的溫度會使該脫除硫酸根礦物質水及該過渡溶液產生難溶 於水的熱固性礦物鹽類（如碳酸鈣及碳酸鎂），使得溶液中的 鈣離子及鎂離子含量減少。較佳地，該步驟（b)及（c)的濃縮 處理的操作壓力範圍為_6〇〇nimHg〜-700mmHg。較佳地， 該步驟（b)及（c)的濃縮處理的操作溫度範圍為5〇。^〜7(rc。 本發明之一具體例中，該濃縮處理的操作溫度範圍為6〇β(： 〜65 C及操作壓力範圍為_63〇mmHg〜-690mmHg。 該步驟（b)及（c)的分離處理方式並沒有特別的限制，以 能將液體與固體進行分離之方式即可。較佳地，該步驟卬） 及（c)的分離處理方式是選自於高速離心方式、減壓抽濾法 或重力過濾法。本發明之一具體例中，該步驟及的分 離處理方式是採用1¾速離心方式。 10 201228944 較佳地，該步驟（b)的過渡溶液的硬度範圍為57 573〜 101,219，且其中的鈉離子濃度範圍為118,3〇〇 ppm〜 135,000 ppm、該鉀離子濃度範圍為3,233 ppm〜7,〇7〇 ppm、邊#5離子濃度範圍為534 ppm〜1，05 5 ppm、該鎮離子 濃度範圍為13,080 ppm〜23，782 ppm。本發明之一具體例 中，在該步驟⑷的過渡溶液中，該鈉離子濃度為134,〇〇〇 ppm、該鉀離子濃度為3,739 ppm、該飼離子濃度為929 ppm、該鎂離子濃度為15,480 ppm及硬度範圍為67,338 5。 • 該步驟（b)之分離處理是要將鈣鹽從脫除硫酸根礦物質 水中分離出來，其目的在於避免其附著在濃縮槽上，經過 長時間的濃縮後形成鍋垢。 較佳地，該步驟（c)的海水濃縮液的硬度範圍為 355,372.3〜416,467.3，且其中的鈉離子濃度範圍為7,368 Ppm〜17,667 ppm、該鉀離子濃度範圍為8,961 4 ppm〜 25,32〇ppm、該鈣離子濃度範圍為41 8ppm〜57 9 ppm及該 鎂離子濃度範圍為84,678 ppm〜99，134 ppm。本發明之一具 • 體例中，在該步驟⑷的海水濃縮液中，該鈉離子濃度為 7,368 ppm、該鉀離子濃度為8,961 4 ppm、該鈣離子濃度為 41.8 ppm、§亥鎂離子濃度為99，134 及硬度範圍為 416,467.3。 該步驟（c)之分離處理是要將鈉鹽與鉀鹽之混合物從過 度命液中分離出來，該步驟的鈉鹽的移除目的在於人體 攝取過多的鈉離子時，會帶給腎臟額外的代謝負擔，更嚴 ㈣疋變成而血納症進而導致水腫、▲璧高及意識狀態等 201228944 問=，再加上目前的飲食文化過分地使用各種不同的調味 ^ 使件過量的鹽類被攝人，因此基於人體健康的考 篁#支先將鈉鹽移除。而該鉀鹽的移除目的在於鉀鹽可取 代氣化納做為代鹽，可提供給糖尿病患者使用。 較佳地，該步驟⑷中將過渡溶液施予一濃縮處理時， 因該㈣及鉀鹽在該過渡溶液中的溶解度不同，會依序先 形成納鹽析出而德墻細 傻、，.只鉀鹽才會析出，故於鈉鹽析出後，可 先進行-分離處理取得鈉鹽，再進一步濃縮及分離取得卸 鹽二該鉀鹽是否需移除可依後續所需之海水濃縮液的用途 疋本發月之具體例中，於.該步驟⑷中為同時獲得卸 鹽及鈉鹽的混合物。 車乂佳地’在该步驟（c)還進一步將該步驟⑼之辦鹽添加 至該海水濃縮液中，目的在於使該海水濃縮液可保留海水 所具有的飼鹽，同時增加海水濃縮液中的飼離子含量。添 加該約鹽時可先將該約鹽用水進行溶解稀釋後，再添加至 該海水濃縮液中形成-均相的溶液，以利後續使用。本發 明之-具體例中，在該步驟⑷的海水濃縮液中添加經稀釋 之弼鹽後，該納離子濃度為135.7ppm、該钟離子漢度為 亂4 ppm'該鈣離子濃度為542 1 ppm、該鎮離子濃度為 1800.1 ppm 及硬度為 8915.2。 為了方便與目前市售的礦泉水包裝水以及運動機能飲 料做比較（目前市售品多半是將硬度調整成1〇〇〜3〇〇)，故將 上述添加鈣鹽之海水濃縮液的硬度調整至1〇〇來界定各成 分的濃度含量範圍’其計算方式為（聊添加約鹽之海水濃 12 201228944 縮液的硬度）x各離子濃度（ppm)。較佳地，基於添加鈣鹽之 海水濃縮液的硬度為10〇，該鈉離子濃度範圍為以 下、s亥鎂離子濃度範圍為丨5ppm以上及該鈣離子濃度範圍 為5PPm以上。本發明之一具體例中，基於該添加鈣海 水濃縮液的硬度為1 〇〇，該鈉離子濃度為 i.52 ppm、該鈣離 子濃度為6.08 ppm及該鎂離子濃度為2〇 2 ppm。Selemion ASV anion-exchange membrane. In order to obtain the best selective filtration effect, the pressure of the feed should be limited. If the pressure is too low, the treatment time will be lengthened, and the surface porosity of the ionic membrane will not be in the optimal selective filtration state. If the pressure is too high, the ability to selectively remove ions will be reduced, and the water will be electrolyzed and unnecessary by-products will be produced. Preferably, the 201228944 operating voltage range of the electrodialysis treatment of the step (3) is 5 V to 15 V. Preferably, the electrodialysis treatment has an operating current range of less than 10.5A. Preferably, the electrodialysis treatment has a flow rate pressure of 100 psi. Preferably, the electrodialysis treatment has a liquid temperature range of less than 25 ° C because the electrodialysis membrane itself has a range of operating temperatures which may affect the useful life of the membrane. In one embodiment of the invention, the electrodialysis treatment has an operating voltage of 12.5 V, an operating current of less than 10.5 A, a flow rate pressure of i〇〇pSi, and a liquid temperature of 25. Hey. Preferably, the hardness of the sulfate-removing mineral water in the step (a) ranges from 16,000 to 20,000, and the sodium ion concentration ranges from 32 〇〇〇 ppm to 40,000 ppm, and the potassium ion concentration ranges from 丨, 28 〇 ppm~ ι, 6 〇〇 ppm 'The calcium ion concentration range is Layppm, the magnesium ion concentration ranges from 3,216 ppm to 4,020 ppm and the sulfate ion concentration ranges from 473 ppm to 591 ppm. The hardness based on the sulfate-removing mineral water is 100, and the sulfate ion concentration ranges from 2 36 to 3.7 ppm [calculated as (100 / hardness of the sulfate-free mineral water) χ each ion concentration (ppm) )]. In one embodiment of the present invention, in the sulfate-removing mineral water removal step of the step, the sulfate ion concentration is 532 ppm, the sodium ion concentration is 36,068 ppm, and the potassium ion concentration is 144〇2 ppm, the calcium ion. The concentration was 1,403_5 ppm, the magnesium ion concentration was 3,618 ppm, and the hardness range was 18,704 'and the hardness based on the sulfate-removing mineral water was 1 〇〇, and the sulfate ion concentration was 2.84 ppm. According to the current research, the chemical composition and content of seawater are almost the same as those of human blood. If the ratio of magnesium ion to calcium ion is the same as that of seawater (ie, the ratio of magnesium to | bow is about 3/1), then It is more convenient for consumers to use 201228944 and it will help the body to absorb a lot. Preferably, the ratio of magnesium to calcium in the sulfated mineral water removed in this step is between 2/1 and 10/1. The concentration treatment methods in the steps (b) and (c) are not particularly limited, and preferably the concentration treatment methods in the steps (b) and (c) are selected from a low-temperature vacuum concentration method or a freezing method. In one embodiment of the present invention, the concentration treatment method is a low-temperature vacuum concentration method, and the pressure of the concentration treatment method can be reduced to reduce the boiling point of the sulfuric acid mineral water and the transition solution. It is necessary to heat the water to 50. (:~70. (:, the water in the sulfate-free mineral water and the water in the transition solution can be evaporated without heating to the point of the Buddha'. This can reduce the steam usage of the concentration tank and greatly reduce the energy consumption; In addition, the control temperature is 50 ec~7 〇 ° c to avoid excessive temperature, which will cause the removal of sulfate mineral water and the transition solution to produce thermosetting mineral salts (such as calcium carbonate and magnesium carbonate) which are poorly soluble in water. The content of calcium ions and magnesium ions in the solution is reduced. Preferably, the operating pressure of the concentration treatment of the steps (b) and (c) ranges from _6〇〇nimHg to -700mmHg. Preferably, the step The operating temperature range of the concentration treatment of (b) and (c) is 5 〇. ^ 〜 7 (rc. In one embodiment of the present invention, the concentration processing temperature range is 6 〇 β (: ～ 65 C and operation The pressure range is _63 〇 mmHg to -690 mmHg. The separation treatment of the steps (b) and (c) is not particularly limited, and the liquid and the solid can be separated. Preferably, the step 卬And (c) the separation treatment method is selected from the high-speed centrifugal method, minus A suction filtration method or a gravity filtration method. In one embodiment of the present invention, the separation treatment method is a 13⁄4 speed centrifugal method. 10 201228944 Preferably, the transition solution of the step (b) has a hardness range of 57 573. ~ 101,219, and the sodium ion concentration range is 118, 3〇〇ppm~ 135,000 ppm, the potassium ion concentration range is 3,233 ppm~7, 〇7〇ppm, side #5 ion concentration range is 534 ppm~1,05 5 ppm, the town ion concentration range is 13,080 ppm~23,782 ppm. In one embodiment of the present invention, in the transition solution of the step (4), the sodium ion concentration is 134, 〇〇〇ppm, the potassium ion concentration It is 3,739 ppm, the feed ion concentration is 929 ppm, the magnesium ion concentration is 15,480 ppm, and the hardness range is 67,338 5. • The separation of step (b) is to separate the calcium salt from the sulfate-removing mineral water. The purpose is to prevent it from adhering to the concentration tank and to form scale after a long period of concentration. Preferably, the seawater concentrate of the step (c) has a hardness ranging from 355, 372.3 to 416, 467.3, and the sodium ion concentration range therein. For 7,368 Ppm~17,667 ppm, the potassium ion concentration range is 8,961 4 ppm~25, 32 〇ppm, the calcium ion concentration ranges from 41 8 ppm to 57 9 ppm, and the magnesium ion concentration ranges from 84,678 ppm to 99,134 ppm. In one embodiment, the sodium ion concentration in the seawater concentrate of the step (4) is 7,368 ppm, the potassium ion concentration is 8,961 4 ppm, the calcium ion concentration is 41.8 ppm, and the magnesium ion concentration is 99. 134 and hardness range 416, 467.3. The separation treatment of the step (c) is to separate the mixture of the sodium salt and the potassium salt from the excessive liquid. The removal of the sodium salt in this step is intended to bring extra kidneys when the body takes too much sodium ions. Metabolic burden, more strict (4) 疋 而 而 血 血 血 血 血 进而 进而 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 2012 People, therefore, based on the health of the human health, the first to remove the sodium salt. The purpose of the removal of the potassium salt is that the potassium salt can be used as a substitute salt for gasification, and can be provided to diabetic patients. Preferably, when the transition solution is applied to a concentration treatment in the step (4), since the solubility of the (4) and the potassium salt in the transition solution is different, the sodium salt is precipitated first and the wall is stupid. Potassium salt will be precipitated. Therefore, after the sodium salt is precipitated, the sodium salt can be firstly subjected to separation treatment, and further concentrated and separated to obtain the salt removal. The potassium salt needs to be removed according to the subsequent required seawater concentrate. In the specific example of the present month, in the step (4), a mixture of the salt and the sodium salt is simultaneously obtained. In the step (c), the salt of the step (9) is further added to the seawater concentrate, so that the seawater concentrate can retain the salt of the seawater and increase the seawater concentrate. Feed ion content. When the salt is added, the salt may be dissolved and diluted with water, and then added to the seawater concentrate to form a homogeneous solution for subsequent use. In a specific example of the present invention, after the diluted cerium salt is added to the seawater concentrate of the step (4), the nano ion concentration is 135.7 ppm, and the clock ion density is 4 ppm'. The calcium ion concentration is 542 1 Ppm, the town ion concentration is 1800.1 ppm and the hardness is 8915.2. In order to facilitate comparison with the currently marketed mineral water packaging water and sports functional beverages (currently most of the commercial products are adjusted to a hardness of 1 〇〇 to 3 〇〇), the hardness adjustment of the above-mentioned calcium salt-containing seawater concentrate is adjusted. To 1〇〇 to define the concentration range of each component' is calculated in the form of (the hardness of the condensed liquid of 201228944 added to the salt). x The ion concentration (ppm). Preferably, the hardness of the seawater concentrate based on the calcium salt added is 10 Torr, and the sodium ion concentration ranges from below, the shai magnesium ion concentration range is 丨 5 ppm or more, and the calcium ion concentration range is 5 ppm or more. In one embodiment of the present invention, the hardness of the calcium-containing seawater concentrate is 1 〇〇, the sodium ion concentration is i.52 ppm, the calcium ion concentration is 6.08 ppm, and the magnesium ion concentration is 2 〇 2 ppm.
更清楚地，本案之具體實施例之海水濃縮液製備步驟 如圖1之流程圖所示。首先將海水經由前處理獲得一礦物質 鹽水，再將該礦物質鹽水經過一前置濃縮處理取得一^縮滷 水，接著將該濃縮滷水施予一電透析處理以取得一脫除硫酸 根礦物質水，透過將該脫除硫酸根礦物f水進行_ 二 及-分離處理可獲得-過渡溶液及㈣，進_步將該過渡濃 溶液施予-濃縮處理及-分離處理，可獲得—海水濃縮液及 -鈉鹽及鉀鹽之混合物’將該鈣鹽以水稀釋55倍回 水濃縮液中即可。 ' 為避免該海水濃縮液輸送儲存過程中產生的再汙染， 或滲漏導致料生物急遽繁殖和高度料，而造纽水優養 化對海域生態有㈣響，及該海料騎輸料費高且不易 保存’發明人更進-步將該海水濃縮液製作成海水礦物質粉 末’除了節省運費外’更能方便運輸到各地區且保存上較容 易’同時可依個人的需求不同來調整所需含量而使用上較為 方便。故本發明海水礦物質粉末的製備方㈣對—如上所述 的海水濃縮液的製備方法製得的海水濃縮液料—後置濃縮 處理而製得。 13 201228944 該後置濃縮處理方式计士 μ 、Λ'又有特别的限制，是與步驟（b) 或（c)的漠縮處理方式相同。妨杜以 J較佳地，該後置濃縮處理方式More clearly, the seawater concentrate preparation step of the specific embodiment of the present invention is as shown in the flow chart of Fig. 1. First, the seawater is pretreated to obtain a mineral brine, and then the mineral brine is subjected to a preconcentration treatment to obtain a brine, and then the concentrated brine is subjected to an electrodialysis treatment to obtain a sulfate removal mineral. Water, by removing the sulfate mineral f water for _2 and - separation treatment to obtain - transition solution and (4), stepping into the concentrated concentrated solution - concentration treatment and - separation treatment, obtain - seawater concentration The mixture of the liquid and the sodium salt and the potassium salt is prepared by diluting the calcium salt with water 55 times into the water concentrate. In order to avoid the re-contamination caused by the transportation and storage of the seawater concentrate, or the leakage causes the biomass to be vigorously propagated and highly materialized, and the water-promoting of the New Zealand water has a (four) sound, and the sea-fishing and feeding costs High and difficult to save 'The inventor is more advanced - making the seawater concentrate into a seawater mineral powder'. In addition to saving freight, it is more convenient to transport to various regions and easier to store. It can also be adjusted according to individual needs. It is convenient to use the required content. Therefore, the preparation of the seawater mineral powder of the present invention (4) is obtained by treating the seawater concentrate material obtained by the method for preparing the seawater concentrate as described above, followed by concentration treatment. 13 201228944 The post-concentration method Ji, Λ' has a special limitation, which is the same as the method of pre-treatment of step (b) or (c). Preferably, the post-concentration treatment method
是選自於低溫真空濃縮方式哎A 八4令凍法。本發明之一具體例 中’該後置濃縮處理方式县始田你、w * 乃式疋知用低溫真空濃縮方式，且該 後置濃縮處理的操作溫度範圍A 6 a ^ 又现国馮60 C〜65 c及操作壓力範 圍為-690mmHg〜-630ηπηϋ§。 較佳地，該海水礦物質粉末的蘭含量比例為％至 謂之間。本發明之一具體例中，該海水礦物質粉末中的It is selected from the low temperature vacuum concentration method 哎A 八四令冻法. In a specific example of the present invention, the post-concentration treatment method of the county, Shida, w*, is known as a low-temperature vacuum concentration method, and the operating temperature range of the post-concentration treatment is A 6 a ^ C~65c and the operating pressure range is -690mmHg~-630ηπηϋ§. Preferably, the seawater mineral powder has a blue content ratio of between % and. In a specific example of the present invention, the seawater mineral powder
鎂弼含置比例為2.56 ’且該納含量為34〇〇mg/1〇〇g、該卸含 量為4300mg/l〇0g、該鈣含量為259〇〇mg/1〇〇g及該鎂含量 為 66400mg/100g。 更明楚地，本案之具體實施例之海水礦物質粉末製備 步驟如圖2之流程圖所示。首先將海水經由前處理獲得一礦 物質鹽水，再將該礦物質鹽水經過一前置濃縮處理取得一濃 縮滷水，接著將該濃縮滷水施予一電透析處理以取得—脫除 硫酸根礦物質水’透過將該脫除硫酸根礦物質水進行—濃縮 處理及一分離處理可獲得一過渡溶液及約鹽，進一步將該過 渡濃溶液施予一濃縮處理及一分離處理，可獲得一海水濃縮 液及一鈉鹽及鉀鹽之混合物，將該鈣鹽以水稀釋55倍回填 至海水濃縮液中，然後施予一後置濃縮處理，即可獲得該海 水礦物質粉末。 該海水濃縮液可直接做為保健飲料，以補充人體所需 之礦物質的來源。而海水礦物質粉末被應用於保健飲料、 含品如調味料、醫藥產品及水產養殖。 14 201228944 本發明將就以下實施例來作進一步說明，但應瞭解的 是’該實施例僅為例示說明之用，而不應被解釋為本發明 實施之限制。 <儀器設備> 1. 電透析裝置：購自於：旭硝子股份有限公司，型號為 CH-0 ’其二價陰離子膜型號為ASV(Selemi〇n ASV anion- exchange membrane， Asahi Glass Engineering Co” Ltd.) 。The content of magnesium strontium is 2.56' and the content of the nanometer is 34〇〇mg/1〇〇g, the unloading content is 4300mg/l〇0g, the calcium content is 259〇〇mg/1〇〇g and the magnesium content It is 66400 mg/100g. More specifically, the seawater mineral powder preparation steps of the specific embodiment of the present invention are shown in the flow chart of Fig. 2. First, the seawater is pretreated to obtain a mineral brine, and the mineral brine is subjected to a preconcentration treatment to obtain a concentrated brine, and then the concentrated brine is subjected to an electrodialysis treatment to obtain - remove the sulfate mineral water. 'A transition solution and a salt can be obtained by performing the concentration treatment and a separation treatment on the sulfate-removing mineral water, and further applying the concentrated concentrated solution to a concentration treatment and a separation treatment to obtain a seawater concentrate And the mixture of the monosodium salt and the potassium salt, the calcium salt is diluted 55 times with water and filled into the seawater concentrate, and then subjected to a post-concentration treatment to obtain the seawater mineral powder. The seawater concentrate can be used directly as a health drink to supplement the source of minerals needed by the body. Seawater mineral powders are used in health drinks, ingredients such as seasonings, pharmaceutical products and aquaculture. The invention is further described in the following examples, but it should be understood that the examples are merely illustrative and are not to be construed as limiting. <Instrumental Equipment> 1. Electrodialysis apparatus: purchased from: Asahi Glass Co., Ltd., model CH-0 'The type of divalent anion membrane is ASV (Selemi〇n ASV anion-exchange membrane, Asahi Glass Engineering Co) Ltd.).
2. 低溫真空濃縮裝置；石材暨資源產業研究發展中心與七 福股份有限公司共同設計組裝。 3. 高速離心裝置：石材暨資源產業研究發展中心與七福股 份有限公司共同設計組裝。 4. 感應偶合電漿原子發射光譜儀（ICp_〇ES );購自於：博 精儀器’型號為〇ptima 2丨00DV。 <實施例> (1) 濃縮滷水的製備： 先將海水（台灣花蓮外海海平面下600公尺〜70〇公尺） 經過前處理取得-硬度為9,⑽的鑛物質鹽水12公升，接 著進行前置濃縮處理’該濃縮處理的操作溫度為6(TC，操 作壓力為-63〇mmHg ’製得一硬度為2〇,892的濃縮涵水，且 該濃㈣水中的主要離子含量如下：納含量為Μ—、 鉀3里為l，5〇4ppm、鈣含量為丨，455 5ppm、鎂含量為 4，108ppm、硫酸根離子含 、 ·、、、 丁 3里為l〇,951PPm ,且鈣離子與鎂離 子的含里比為2.82,數據整理如表i所示。 (2) 脫硫酸根礦物質水的製備： 15 201228944 將上述之該濃縮滴水進行電透析處理，該電透析處理 的操作溫度為25t，操作電壓為12·5ν，操作流速為 100PSI，製得該硬度為18,704的脫硫酸根礦物質水^公 升，且該脫硫酸根礦物質水中的主要離子含量如下：鈉含量 為36,068PPm、鉀含量為1440.2Ppm、鈣含量為 l，403.5ppm、鎂含量為3,618ppm、硫酸根離子含量為 532PPm，且鎂離子與鈣離子的含量比為2 57。基於該脫除 硫酸根礦物質水的硬度為100，該硫酸根離子濃度為 2,84ppm，數據整理如表1所示。 (3) 過渡溶液及鈣鹽的製備： 將上述之該脫除硫酸根礦物質水進行低溫真空濃縮處 理及高速離心處理，該濃縮處理的操作溫度為6〇t>c〜65 。(：，操作壓力為-690mmHg〜·630ηιπιΗ§，製得該硬度為 67,338.5的過渡溶液及鈣鹽，且該過渡溶液中的主要離子含 量如下：鈉含量為134,0〇〇ppm、鉀含量為3 739ppm、鈣含 量為929ppm、鎂含量為15,480ppm，且鎂離子與飼離子的 含量比為16.7，數據整理如表1所示。 (4) 海水濃缩液及鉀鹽與鈉鹽的混合物之製備： 將上述之該過渡溶液進行低溫真空濃縮處理及高速離 心處理，該濃縮處理的操作溫度為6〇t：〜65°C，操作壓力 為-690mmHg〜-630mmHg，製得該硬度為416,467.3的海水 濃縮液及鈣鹽，且該海水濃縮液中的主要離子含量如下：納 含量為7,368ppm、鉀含量為8,961_4ppm、約含量為 4l.8ppm、鎂含量為99，134ppm，且鎂離子與鈣離子的含量 16 201228944 比為4.2Xl〇-、進一步將上述之鈣鹽用水稀釋55倍後添加 至該海水濃縮液中，其硬度為8,915 2、鈉含量為 135.7PPm、鉀含量為163.4Ppm、鈣含量為542 1ppm、鎂含 量為1800.1PPm，且鎂離子與鈣離子的含量比為3 32，數據 整理如表1所示。 (5) 海水礦物質粉末的製備： 將上述之添加鈣鹽之海水濃縮液進行後置濃縮處理， 該》辰縮處理的細作溫度為60 °C〜65 °C，操作壓力為 690mmHg〜-630mmHg，製得該海水礦物質粉末19 57克， 且該海水礦物質粉末中的主要離子含量如下：鈉含量為 3400mg/100g、鉀含量為4300mg/100g、舞含量為 25,900mg/100g、鎮含量為66,400mg/100g，且鎂離子與約離 子的含量比為2.56。 表1 硬度 納離子 (ppm) 鉀離子 (ppm) 鈣離子 (ppm) 鎂離子 (ppm) 硫酸根 離子 (ΡΡίηΊ 鎂/的比 例 礦物質鹽水 9,100 14,890 549 548.5 1,843 4,563 3.36 濃縮滷水 20,892 37,028 1,504 1,455.5 4,108 10,951 2.82 脫除硫酸根 礦物質水 18,704 36,068 1,440.2 1,403.5 3,618 532 2.84 過渡溶液 67,338.5 134,000 3,739 929 15,480 μ _爾 16.7 海水濃縮液 416,467.3 7,368 8,961.4 41.8 99,134 _ » 4.2xl〇'4 海水濃縮液 添加稀釋後 之釣鹽 8915.2 135.7 163.4 542.1 1800.1 3.32 17 201228944 綜上所述，本發明藉由濃縮滷水透過二價陰離子媒進 订電透析處理先將硫酸根離子移除，以利後續處理時可 少鈣離子的損失，接著施予濃縮處理及分離處理，取得二 海水漠縮液及礦物質鹽（如鈣鹽、鈉鹽與鉀鹽混合物）。3該 海水礦物質粉末的製備為對上述之海水濃縮液施予一後置' 濃縮處理而製得。該等製備方法所製得之海水濃縮液及海 水礦物質粉末具有低含量的额根離子及_子，並同時 含有高含量⑽離子及鎂離子。且該海水礦物質粉末為— 水溶性礦物質粉末，而海水濃縮液為一水溶性礦物質水皆 可被人體有效地吸收，故確實達到本發明之目的。 惟以上所述者，僅為本#明之較佳實施{列^，當不 能以此限定本發明實施之範圍’即大凡依本發明申請: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是一流程圖，用於說明本發明之一實施方式製 海水濃縮液的方法；及 、圖2是-流程圖，用於說明本發明之一實施方式製備 海水礦物質粉末的方法。 【主要元件符號說明】 益 182. Low-temperature vacuum concentrating device; Stone and Resource Industry Research and Development Center and Qifu Co., Ltd. jointly designed and assembled. 3. High-speed centrifugal device: Stone and Resource Industry Research and Development Center and Qifu Share Co., Ltd. jointly designed and assembled. 4. Inductively coupled plasma atomic emission spectrometer (ICp_〇ES); purchased from: Bojing Instruments' model is 〇ptima 2丨00DV. <Examples> (1) Preparation of concentrated brine: First, seawater (600 meters to 70 ft. below sea level in Hualien, Taiwan) was pretreated to obtain a hardness of 9, (10) of mineral brine of 12 liters. Then, the preconcentration treatment is carried out. The operating temperature of the concentration treatment is 6 (TC, the operating pressure is -63 〇mmHg', and a concentrated culvert having a hardness of 2 〇, 892 is obtained, and the main ion content in the concentrated (iv) water is as follows The content of sodium is Μ-, potassium is 1,5〇4ppm, calcium content is 丨, 455 5ppm, magnesium content is 4,108ppm, sulfate ion is contained, ·,, and ding 3 is l〇, 951PPm, The ratio of calcium ion to magnesium ion is 2.82, and the data is as shown in Table i. (2) Preparation of desulfate mineral water: 15 201228944 The concentrated drip water described above is subjected to electrodialysis treatment, and the electrodialysis treatment The operating temperature is 25t, the operating voltage is 12·5ν, the operating flow rate is 100PSI, and the desulfurized mineral water having a hardness of 18,704 is obtained, and the main ion content of the desulfate mineral water is as follows: sodium content It is 36,068 ppm, the potassium content is 1440.2 Ppm, and the calcium content is l, 403.5 ppm, magnesium content of 3,618 ppm, sulfate ion content of 532 ppm, and magnesium ion to calcium ion content ratio of 2 57. Based on the hardness of the sulfate-removing mineral water is 100, the sulfate ion concentration It is 2,84ppm, and the data is sorted as shown in Table 1. (3) Preparation of transition solution and calcium salt: The above-mentioned removal of sulfate mineral water is subjected to low-temperature vacuum concentration treatment and high-speed centrifugation, and the operation of the concentration treatment The temperature is 6〇t>c~65. (:, the operating pressure is -690mmHg~·630ηιπιΗ§, the transition solution and the calcium salt having a hardness of 67,338.5 are obtained, and the main ion content in the transition solution is as follows: the sodium content is 134,0〇〇ppm, potassium content of 3 739ppm, calcium content of 929ppm, magnesium content of 15,480ppm, and magnesium ion to feed ion content ratio of 16.7, data as shown in Table 1. (4) seawater concentration Preparation of liquid and mixture of potassium salt and sodium salt: The above transition solution is subjected to low-temperature vacuum concentration treatment and high-speed centrifugation, and the operation temperature of the concentration treatment is 6 〇t: ~65 ° C, and the operating pressure is -690 mmHg~ -630mmHg, made The hardness is 416, 467.3 seawater concentrate and calcium salt, and the main ion content in the seawater concentrate is as follows: the nano content is 7,368 ppm, the potassium content is 8,961_4 ppm, the content is about 41.8 ppm, and the magnesium content is 99,134 ppm. And the ratio of magnesium ion to calcium ion 16 201228944 is 4.2Xl〇-, and the above calcium salt is further diluted 55 times with water and added to the seawater concentrate, the hardness is 8,915 2. The sodium content is 135.7PPm, the potassium content It is 163.4 Ppm, the calcium content is 542 1 ppm, the magnesium content is 1800.1 ppm, and the content ratio of magnesium ion to calcium ion is 3 32. The data is as shown in Table 1. (5) Preparation of seawater mineral powder: The above-mentioned calcium salt-added seawater concentrate is subjected to post-concentration treatment, and the fine-working temperature of the shrinkage treatment is 60 ° C to 65 ° C, and the operating pressure is 690 mmHg to -630 mmHg. 19 57 g of the seawater mineral powder was prepared, and the main ion content in the seawater mineral powder was as follows: sodium content was 3400 mg/100 g, potassium content was 4300 mg/100 g, dance content was 25,900 mg/100 g, and the town content was 66,400 mg/100 g, and the content ratio of magnesium ion to about ion is 2.56. Table 1 Hardness Nano-ion (ppm) Potassium ion (ppm) Calcium ion (ppm) Magnesium ion (ppm) Sulfate ion (ΡΡίηΊ Magnesium/proportional mineral brine 9,100 14,890 549 548.5 1,843 4,563 3.36 Concentrated brine 20,892 37,028 1,504 1,455.5 4,108 10,951 2.82 Removal of sulphate mineral water 18,704 36,068 1,440.2 1,403.5 3,618 532 2.84 Transition solution 67,338.5 134,000 3,739 929 15,480 μ _ er 16.7 seawater concentrate 416,467.3 7,368 8,961.4 41.8 99,134 _ » 4.2xl〇'4 seawater concentrate added diluted salt 8915.2 135.7 163.4 542.1 1800.1 3.32 17 201228944 In summary, the present invention removes the sulfate ion by preferentially distilling the brine through the dianion medium to facilitate the subsequent treatment, thereby reducing the loss of calcium ions, and then The concentrated treatment and the separation treatment are carried out to obtain a seawater desert liquid and a mineral salt (such as a mixture of a calcium salt, a sodium salt and a potassium salt). 3 The seawater mineral powder is prepared by applying the seawater concentrate to the above. Prepared by concentration treatment. Seawater concentrates and seawater minerals prepared by the preparation methods The powder has a low content of forehead ions and _ sub-particles, and contains a high content of (10) ions and magnesium ions. The seawater mineral powder is a water-soluble mineral powder, and the seawater concentrate is a water-soluble mineral water. It is effectively absorbed by the human body, and it is indeed the object of the present invention. However, the above is only a preferred embodiment of the present invention, and if it is not possible to limit the scope of the present invention, it is generally applicable to the present invention: The simple equivalent changes and modifications made by the scope of the invention and the description of the invention are still within the scope of the invention. [FIG. 1 is a flow chart for explaining an embodiment of the present invention. A method for preparing a seawater concentrate; and FIG. 2 is a flow chart for explaining a method for preparing a seawater mineral powder according to an embodiment of the present invention.