TW201834737A - Reverse osmosis treatment method and device - Google Patents
Reverse osmosis treatment method and device Download PDFInfo
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- TW201834737A TW201834737A TW106132174A TW106132174A TW201834737A TW 201834737 A TW201834737 A TW 201834737A TW 106132174 A TW106132174 A TW 106132174A TW 106132174 A TW106132174 A TW 106132174A TW 201834737 A TW201834737 A TW 201834737A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/04—Feed pretreatment
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
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Abstract
Description
[0001] 本發明有關一種使用逆滲透膜裝置將水處理的逆滲透處理方法，尤其是一種將對於逆滲透膜裝置之給水以熱泵予以加熱的逆滲透處理方法以及裝置。[0001] The present invention relates to a reverse osmosis treatment method for treating water using a reverse osmosis membrane device, and more particularly to a reverse osmosis treatment method and apparatus for heating a feed water for a reverse osmosis membrane device with a heat pump.
[0002] 有關逆滲透膜裝置(以下，有稱之為RO裝置之情形)，由於必須維持處理水量(導因於水之黏度降低之通量上升、導因於二氧化矽飽和溶解度上升之回收率提高)之故，乃將給水溫度加溫於25℃左右。此一給水之加熱，乃使用蒸氣、溫水、電熱器等，將會消耗能源。 [0003] 日本特開2012-91118號公報之申請專利範圍第7項，曾記載將RO裝置之給水利用熱泵加熱至23～25℃，然同案號公報中並未具體記載熱泵之熱源。 [先前技術文獻] [專利文獻] [0004] [專利文獻1] 日本特開2012-91118號公報 [0005] 將RO裝置之給水利用蒸氣、溫水、電熱器等加熱之情況下，加熱成本高。又，投入於給水加熱之能源係與濃縮水一起廢棄，成為能源損失。 [0006] 雖可將原水與濃縮水熱交換，而將濃縮水排熱回收，然因溫度差小之故，有必要增大熱交換器之傳熱面積，以致熱交換器費用增高。又，由於溫度差有其必要，因此將加熱部份全量回收不可能。 [0007] 將不同設備(冷凍機、壓縮機等)之排熱設為熱源之情況下，與RO裝置之配管將會變長，以致工事費用提高。又，還有運轉之時序不能配合的情形。 [0008] RO裝置之給水以熱泵加熱的情形下，熱泵之熱源可考慮採用RO裝置之濃縮水(以下，或稱為RO濃縮水)或處理水。然而，RO濃縮水因積垢成分(例如二氧化矽、鈣等之硬度成分)濃度與其他鹽類濃度、有機物濃度偏高之故，在熱泵之蒸發器等易於產生積垢、黏泥等之汙垢。[0002] Regarding the reverse osmosis membrane device (hereinafter referred to as the RO device), it is necessary to maintain the amount of treated water (the flux due to the decrease in viscosity of water is increased, and the recovery due to the increase in saturated solubility of cerium oxide) The rate is increased, and the feed water temperature is raised to about 25 °C. The heating of this water supply uses steam, warm water, electric heaters, etc., and will consume energy. [0003] In the seventh application of the Japanese Patent Application Laid-Open No. 2012-91118, it is described that the water supply of the RO device is heated to 23 to 25 ° C by a heat pump, and the heat source of the heat pump is not specifically described in the publication. [PRIOR ART DOCUMENT] [Patent Document 1] [Patent Document 1] Japanese Laid-Open Patent Publication No. 2012-91118 [0005] When the water supply of the RO device is heated by steam, warm water, an electric heater or the like, the heating cost is high. . Further, the energy source that is heated by the feed water is discarded together with the concentrated water, and it is an energy loss. [0006] Although the raw water can be exchanged with the concentrated water and the concentrated water is heat-recovered, since the temperature difference is small, it is necessary to increase the heat transfer area of the heat exchanger, so that the heat exchanger costs are increased. Moreover, since the temperature difference is necessary, it is impossible to recover the entire amount of the heating portion. [0007] In the case where the heat of the different devices (refrigerator, compressor, etc.) is set as the heat source, the piping with the RO device will become longer, so that the work cost is increased. Also, there is a case where the timing of the operation cannot be matched. [0008] In the case where the feed water of the RO device is heated by a heat pump, the heat source of the heat pump may consider concentrated water (hereinafter, referred to as RO concentrated water) or treated water of the RO device. However, since the concentration of the scale component (for example, hardness components such as cerium oxide and calcium) of the RO concentrated water is higher than the concentration of other salts and the concentration of the organic matter, the evaporator of the heat pump is likely to cause scale, slime, and the like. dirt.
[發明解決之課題] [0009] 本發明之目的為藉由將利用以RO濃縮水作為熱源之熱泵來加熱針對RO裝置之給水，而降低加熱成本。又，本發明於其一個方式中，其目的為防止或抑制此熱泵之蒸發器及RO裝置等之積垢、黏泥等。 [用以解決課題之手段] [0010] 本發明之逆滲透處理方法，係將原水以熱泵加熱後，利用逆滲透膜裝置進行膜分離處理，其中作為該熱泵之熱源流體的至少一部分，使用該逆滲透膜裝置之濃縮水。 [0011] 本發明之一個方式中，係以上述熱泵之蒸發器之熱源流體出口的濃縮水之二氧化矽濃度未達二氧化矽積垢析出濃度及/或朗傑利亞指數(Langelier's index)成為0以下的方式，調整上述逆滲透膜裝置之回收率及上述原水之溫度的至少一者。 [0012] 本發明之一個方式中，上述原水係設為特定pH以上之鹼性，或設為特定pH以下之酸性。 [0013] 本發明之一個方式中，係於上述原水中添加積垢防止劑及/或黏泥防止劑。 [0014] 本發明之逆滲透處理裝置，係將原水以熱泵加熱後，利用逆滲透膜裝置進行膜分離處理，其中作為該熱泵之熱源流體的至少一部分，具備將該逆滲透膜裝置之濃縮水流通之通水路。 [發明之效果] [0015] 根據本發明，藉由利用以RO濃縮水為熱源之熱泵加熱對於RO裝置之給水，可降低加熱成本。又，藉由以RO濃縮水為熱源，可以僅在RO裝置附近之配管工事等來構成本發明裝置。 [0016] 藉由使用熱泵，可增大與原水之溫度差，以小的傳熱面積即可作熱回收。 [0017] 根據本發明之一個方式，基於二氧化矽濃度與鹽類濃度高等之理由而難以作為熱泵之熱源利用的水質之RO濃縮水，可直接作為熱泵熱源利用。[Problem to be Solved by the Invention] [0009] An object of the present invention is to reduce heating costs by heating a feed water for an RO device using a heat pump using RO concentrated water as a heat source. Further, in one aspect of the present invention, the object of the present invention is to prevent or suppress the scale, slime, and the like of the evaporator, the RO device, and the like of the heat pump. [Means for Solving the Problem] [0010] The reverse osmosis treatment method of the present invention is a method in which a raw water is heated by a heat pump, and a membrane separation treatment is performed by a reverse osmosis membrane device, wherein at least a part of the heat source fluid of the heat pump is used. Concentrated water from a reverse osmosis membrane unit. [0011] In one aspect of the present invention, the concentration of cerium oxide in the concentrated water of the heat source fluid outlet of the evaporator of the heat pump is less than the cerium oxide scale deposition concentration and/or the Langelier's index. In a method of 0 or less, at least one of the recovery rate of the reverse osmosis membrane device and the temperature of the raw water is adjusted. [0012] In one aspect of the invention, the raw water system is made alkaline at a specific pH or higher, or is acidic at a specific pH or lower. [0013] In one aspect of the present invention, a scale inhibitor and/or a slime inhibitor are added to the raw water. [0014] The reverse osmosis treatment apparatus of the present invention is characterized in that after the raw water is heated by a heat pump, the membrane separation treatment is performed by a reverse osmosis membrane device, wherein at least a part of the heat source fluid of the heat pump is provided with concentrated water of the reverse osmosis membrane device. Circulating waterway. [Effects of the Invention] According to the present invention, by heating a feed water for an RO device using a heat pump using RO concentrated water as a heat source, the heating cost can be reduced. Further, by using the RO concentrated water as a heat source, the apparatus of the present invention can be constructed only by piping work in the vicinity of the RO apparatus. [0016] By using a heat pump, the temperature difference from the raw water can be increased, and heat recovery can be performed with a small heat transfer area. According to one aspect of the present invention, RO concentrated water which is difficult to use as a heat source of a heat pump based on a high concentration of cerium oxide and a salt concentration can be directly used as a heat pump heat source.
[0019] 以下，參照第1圖針對本發明之實施方式進行說明。 [0020] 經RO處理之原水係自配管1供給至熱交換器2，經加熱後，自配管3供給至熱交換器4，進一步經加熱後，再供給至RO裝置6。RO裝置6之透過水係自配管7作為處理水取出，濃縮水係往向配管8流出，並作為熱泵10之熱源流體流通至該熱泵10之蒸發器11。 [0021] 熱交換器2之熱源流體流路中，循環流通有由熱泵10之冷凝器13加熱之媒體水(作為傳熱媒體之水)。 [0022] 熱泵10在構成上係將來自蒸發器11之氟氯碳化合物替代品等之熱媒體以壓縮機12壓縮並導入冷凝器13，來自冷凝器13之熱媒體係經由膨脹閥14導入至蒸發器11。 [0023] 冷凝器13中經由配管15及泵17被導入來自熱交換器2之媒體水，由冷凝器13加熱之媒體水係經由配管16送至熱交換器2。 [0024] 蒸發器11之熱源流體流路中，自配管8被導入RO裝置6之濃縮水。由熱交換降溫之濃縮水，係經由配管9排出。 [0025] 熱交換器4之熱源流體流路中，係被供給蒸氣。 [0026] RO裝置6之濃縮水之積垢成分濃度與有機物濃度較原水為高，因此熱泵10之蒸發器11與配管8、9處積垢與黏泥發生之懸念偏高，因此有予以防止或抑制(以下稱為防止)之必要。又，RO裝置6中亦然，有防止積垢與黏泥發生之必要。 [0027] 是以，於此實施方式中，為了防止蒸發器11、RO裝置6、配管8、9之積垢、黏泥，乃進行以下之i)、ii)或iii)之對策。 [0028] i) 以流過蒸發器11之熱源流體出口11a的濃縮水之二氧化矽濃度不超過二氧化矽積垢析出濃度的方式，及/或朗傑利亞指數成為0以下的方式，調整RO回收率及原水溫度之一者或兩者。 [0029] 亦即，以[熱泵蒸發器出口11a之二氧化矽濃度]較[二氧化矽飽和溶解度]為低的方式，及/或[熱泵蒸發器出口11a之朗傑利亞指數]成為[0以下]的方式，進行將RO回收率降低、及提高原水溫度之一者或二者。 [0030] RO濃縮水及蒸發器出口之朗傑利亞指數(LSI)，一般係以下式(1)求得。式(1)中，pH係濃縮水或蒸發器出口之pH值。pHs係濃縮水或蒸發器中碳酸鈣處於既不溶解也不析出之平衡狀態時的理論上之pH值，可由下式(2)求得。(2) 式(2)中，A值係根據蒸發殘留物濃度所決定之補正值。蒸發殘留物濃度由於與導電率有所相關，因此可使用特定之換算式自導電率求取蒸發殘留物濃度。B值係根據水溫所決定之補正值。C值係根據鈣硬度所決定之補正值。D值係根據總鹼度所決定之補正值。 [0031] 可將RO透過水之一部分添加於RO濃縮水，而形成為適於流通至熱泵蒸發器之水質。亦即，將RO透過水之一部分添加至RO濃縮水亦包含於「降低回收率」。 [0032] 如是，藉由降低回收率或提高原水溫度，可將RO濃縮水中之二氧化矽濃度與朗傑利亞指數設為積垢非發生條件。例如，藉由將23～25℃之濃縮水中之二氧化矽濃度設為100～120 ppm以下，可防止二氧化矽積垢。 [0033] ii) 以RO裝置6及熱泵蒸發器11處不析出二氧化矽積垢的方式調整原水之pH。具體而言，於原水之Ca硬度為5 mg/L以下之條件下，將pH設為9以上(例如，9～11)。或是，將原水之pH設為6以下(例如，4～6)。藉由以高pH將二氧化矽離子化，可抑制凝膠化，而抑制積垢析出。又，藉由將原水設為低pH，可降低二氧化矽之析出速度而抑制二氧化矽積垢。 [0034] iii) 為使RO裝置6及熱泵蒸發器11處不析出積垢、黏泥，乃於原水中添加藥品(積垢防止劑與黏泥防止劑等)。作為積垢防止劑與黏泥防止劑，並無特別限制，可使用各種產品。 [0035] 為了將朗傑利亞指數設為0以下，可將原水之pH設為6以下(例如，4～6)，或是，於RO膜之前段設置軟水器而除去硬度成分。又，也可將鈣積垢用之積垢防止劑添加於原水中，此一情況下，朗傑利亞指數超過0也可。例如，雖與積垢防止劑之性能有關，藉由利用有機高分子積垢防止劑，將可控制朗傑利亞指數使其為0.5以下。 [0036] 作為原水，可例示的是工業用水(河川水、湖沼水等)、地下水、自來水、各種排水之處理水等，然不受此限定。 [0037] 根據第1圖之系統，將井水(18℃)加熱於25℃並以20 m3 /h作RO處理，再將透過水以25℃、14 m3 /h、將濃縮水以25℃、6 m3 /h作膜分離，而將熱泵以COP(成績係數)5運轉之情況下，如第1圖所示以設置熱泵10及熱交換器2、4、將蒸發器出口11a之濃縮水溫度設為20℃為條件而使系統運轉時之熱交換器4的蒸氣使用量，將相當於101.8 kW。 [0038] 於本發明之具備熱泵之逆滲透膜裝置中，係可於RO膜之入口與出口、蒸發器之熱源流體入口與出口之一部分或全部，設置二氧化矽與硬度成分(或朗傑利亞指數)、水溫等之測定機器(感測器或算出單元等)，基於該機器之測定值，設置將RO膜之回收率、pH調整(酸或鹼之添加機構之控制)、藥品添加(積垢防止劑與黏泥防止劑之添加機構)的一部分或全部自動控制之控制單元，而將裝置整體設計為可自動運轉。藉由在熱源流體出口設置上述測定機器而控制RO膜之運轉條件，將可使具備熱泵之逆滲透膜裝置整體安定地運轉。 [0039] 另一方面，第1圖之系統中，未設置熱交換器2及熱泵10之情況下，同條件下RO處理時之熱交換器4的蒸氣使用量相當於162.8 kW。 [0040] 上述實施方式為本發明之一例，本發明也可形成為圖示以外之方式。 [0041] 本發明雖以特定之方式詳細說明如上，但此業界當可自明的是，在不脫離本發明之意圖與範圍內尚可作各種各樣之變更。 本申請案係以2017年3月16日申請之日本特許出願2017-051091號為基礎，其全部內容可藉由引用而於此援用。[0019] Hereinafter, embodiments of the present invention will be described with reference to Fig. 1 . The RO-treated raw water is supplied from the pipe 1 to the heat exchanger 2, heated, and then supplied from the pipe 3 to the heat exchanger 4, and further heated, and then supplied to the RO device 6. The permeated water of the RO device 6 is taken out as the treated water from the pipe 7, and the concentrated water flows out to the pipe 8, and flows as a heat source fluid of the heat pump 10 to the evaporator 11 of the heat pump 10. [0021] In the heat source fluid flow path of the heat exchanger 2, medium water (water as a heat transfer medium) heated by the condenser 13 of the heat pump 10 is circulated and circulated. [0022] The heat pump 10 is configured to compress a heat medium such as a chlorofluorocarbon substitute or the like from the evaporator 11 by a compressor 12 and introduce it into a condenser 13, and the heat medium from the condenser 13 is introduced to the heat medium via the expansion valve 14. Evaporator 11. [0023] The medium water from the heat exchanger 2 is introduced into the condenser 13 via the pipe 15 and the pump 17, and the medium water heated by the condenser 13 is sent to the heat exchanger 2 via the pipe 16. [0024] In the heat source fluid flow path of the evaporator 11, the concentrated water from the RO device 6 is introduced from the pipe 8. The concentrated water cooled by the heat exchange is discharged through the piping 9. [0025] In the heat source fluid flow path of the heat exchanger 4, steam is supplied. [0026] The concentration of the scale component of the concentrated water of the RO device 6 and the concentration of the organic matter are higher than that of the raw water, so that the fouling of the evaporator 11 and the pipes 8 and 9 of the heat pump 10 and the occurrence of slime are high, so that it is prevented. Or suppression (hereinafter referred to as prevention). Further, in the RO device 6, it is also necessary to prevent the occurrence of scale and slime. [0027] In this embodiment, in order to prevent fouling and slime of the evaporator 11, the RO device 6, and the pipes 8, 9, the following measures i), ii) or iii) are carried out. [0028] i) the concentration of cerium oxide in the concentrated water flowing through the heat source fluid outlet 11a of the evaporator 11 does not exceed the concentration of the cerium oxide scale deposition, and/or the Langerial index becomes 0 or less. Adjust one or both of the RO recovery rate and the raw water temperature. [0029] That is, [the cerium oxide concentration of the heat pump evaporator outlet 11a] is lower than [the cerium oxide saturation solubility], and/or [the heat pump evaporator outlet 11a of the Langella index] becomes [ In the case of 0 or less, one or both of the RO recovery rate and the raw water temperature are increased. [0030] The Langeriya index (LSI) of the RO concentrated water and the evaporator outlet is generally obtained by the following formula (1). In the formula (1), the pH of the pH-based concentrated water or the evaporator outlet. The theoretical pH value in the case where the pHs are concentrated water or the calcium carbonate in the evaporator is in an equilibrium state of neither dissolution nor precipitation, can be obtained by the following formula (2). (2) In the formula (2), the A value is a correction value determined based on the concentration of the evaporation residue. The concentration of the evaporation residue is related to the conductivity, so the evaporation residue concentration can be obtained from the conductivity using a specific conversion formula. The B value is a correction value determined by the water temperature. The C value is a correction value determined by the hardness of the calcium. The D value is the correction value determined by the total alkalinity. [0031] One of the RO permeated water may be added to the RO concentrated water to form a water quality suitable for circulation to the heat pump evaporator. That is, the addition of RO to a portion of the water to the RO concentrated water is also included in the "reduced recovery rate". [0032] If, by reducing the recovery rate or increasing the temperature of the raw water, the concentration of cerium oxide in the RO concentrated water and the Langerial index can be set as the non-occurring conditions of the scale. For example, by setting the concentration of cerium oxide in concentrated water at 23 to 25 ° C to 100 to 120 ppm or less, it is possible to prevent cerium oxide fouling. [0033] ii) The pH of the raw water is adjusted so that the scale of the raw water is not precipitated at the RO device 6 and the heat pump evaporator 11. Specifically, the pH is set to 9 or more (for example, 9 to 11) under the condition that the Ca hardness of the raw water is 5 mg/L or less. Alternatively, the pH of the raw water is set to 6 or less (for example, 4 to 6). By ionizing cerium oxide at a high pH, gelation can be suppressed, and scale deposition can be suppressed. Further, by setting the raw water to a low pH, the precipitation rate of cerium oxide can be lowered to suppress the scale formation of cerium oxide. [0034] iii) In order to prevent fouling and slime from being deposited in the RO device 6 and the heat pump evaporator 11, a chemical (a scale inhibitor, a slime inhibitor, etc.) is added to the raw water. The antifouling agent and the slime preventing agent are not particularly limited, and various products can be used. [0035] In order to set the Languelia index to 0 or less, the pH of the raw water may be 6 or less (for example, 4 to 6), or a softener may be provided in the front stage of the RO membrane to remove the hardness component. Further, the scale inhibitor for calcium deposits may be added to the raw water. In this case, the Langerial index may exceed zero. For example, depending on the performance of the scale inhibitor, the Langeriya index can be controlled to be 0.5 or less by using the organic polymer scale inhibitor. [0036] The raw water may be exemplified by industrial water (river water, lake water, etc.), ground water, tap water, treated water of various kinds of drainage, and the like, but is not limited thereto. [0037] According to the system of Fig. 1, the well water (18 ° C) is heated at 25 ° C and treated with RO at 20 m 3 /h, and the permeated water is at 25 ° C, 14 m 3 / h, and the concentrated water is 25 ° C, 6 m 3 /h for membrane separation, and when the heat pump is operated with COP (performance coefficient) 5, as shown in Fig. 1 to set the heat pump 10 and the heat exchanger 2, 4, the evaporator outlet 11a When the temperature of the concentrated water is 20 ° C, the amount of steam used in the heat exchanger 4 when the system is operated is equivalent to 101.8 kW. [0038] In the reverse osmosis membrane device with heat pump of the present invention, the cerium oxide and the hardness component (or Langjie) may be disposed at part or all of the inlet and outlet of the RO membrane and the heat source fluid inlet and outlet of the evaporator. a measurement device (sensor, calculation unit, etc.) such as water temperature, etc., based on the measured value of the machine, setting the RO membrane recovery rate, pH adjustment (control of the acid or alkali addition mechanism), and the drug A part or all of the control unit that is automatically controlled (addition mechanism of the scale inhibitor and the slime preventive agent) is added, and the entire apparatus is designed to be automatically operated. By providing the above-described measuring device at the heat source fluid outlet to control the operating conditions of the RO membrane, the reverse osmosis membrane device equipped with the heat pump can be stably operated as a whole. On the other hand, in the system of Fig. 1, when the heat exchanger 2 and the heat pump 10 are not provided, the amount of steam used in the heat exchanger 4 during the RO treatment under the same conditions is equivalent to 162.8 kW. [0040] The above embodiment is an example of the present invention, and the present invention may be formed in a form other than the drawings. The present invention has been described in detail with reference to the preferred embodiments of the present invention. It is to be understood that various modifications may be made without departing from the spirit and scope of the invention. The present application is based on Japanese Patent Application No. 2017-051091, filed on March 16, 2017, the entire content of which is hereby incorporated by reference.
[0042][0042]
2、4‧‧‧熱交換器2, 4‧‧ ‧ heat exchanger
6‧‧‧RO裝置6‧‧‧RO device
10‧‧‧熱泵10‧‧‧ heat pump
11‧‧‧蒸發器11‧‧‧Evaporator
12‧‧‧壓縮機12‧‧‧Compressor
13‧‧‧冷凝器13‧‧‧Condenser
14‧‧‧膨脹閥14‧‧‧Expansion valve
[0018] 第1圖為本發明實施方式之逆滲透處理裝置的方塊圖。1 is a block diagram of a reverse osmosis processing apparatus according to an embodiment of the present invention.
Claims (5)
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2017051091A JP6532494B2 (en) | 2017-03-16 | 2017-03-16 | Reverse osmosis processing method and apparatus |
| JP2017-051091 | 2017-03-16 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| TW201834737A true TW201834737A (en) | 2018-10-01 |
Family
ID=63521986
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| Application Number | Title | Priority Date | Filing Date |
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| TW106132174A TW201834737A (en) | 2017-03-16 | 2017-09-20 | Reverse osmosis treatment method and device |
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| Country | Link |
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| JP (1) | JP6532494B2 (en) |
| TW (1) | TW201834737A (en) |
| WO (1) | WO2018168012A1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| TWI781329B (en) * | 2018-07-06 | 2022-10-21 | 日商栗田工業股份有限公司 | Reverse osmosis treatment method and system |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN115676975B (en) * | 2022-11-29 | 2024-03-22 | 厚德食品股份有限公司 | Water storage system for pure water machine |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS634808A (en) * | 1986-06-24 | 1988-01-09 | Takuma Co Ltd | Reverse-osmosis membrane device system |
| JPS6443304A (en) * | 1987-08-06 | 1989-02-15 | Maruyama Mfg Co | Method for heating feed water in reverse osmosis process |
| JP4193234B2 (en) * | 1998-08-17 | 2008-12-10 | 栗田工業株式会社 | Pure water production method |
| JP2007307561A (en) * | 2007-07-27 | 2007-11-29 | Kurita Water Ind Ltd | High-purity water producing apparatus and method |
| JP2011033250A (en) * | 2009-07-31 | 2011-02-17 | Sanyo Electric Co Ltd | Water heater |
| JP5308977B2 (en) * | 2009-09-28 | 2013-10-09 | サンデン株式会社 | Hot water system |
| JP2011133121A (en) * | 2009-12-22 | 2011-07-07 | Sanyo Electric Co Ltd | Heat pump water heater |
| JP5743490B2 (en) * | 2010-10-27 | 2015-07-01 | オルガノ株式会社 | Water treatment system and water treatment method |
| JP5757110B2 (en) * | 2011-03-09 | 2015-07-29 | 三浦工業株式会社 | Water treatment method and water treatment system |
| CN103370279B (en) * | 2012-02-15 | 2015-11-25 | 三菱重工业株式会社 | Seawater desalination system |
| JP2014200696A (en) * | 2013-04-01 | 2014-10-27 | パナソニック株式会社 | Hot water supply apparatus |
| JP6207381B2 (en) * | 2013-12-24 | 2017-10-04 | 東芝キヤリア株式会社 | Water heater |
| JP6229589B2 (en) * | 2014-04-25 | 2017-11-15 | 三菱電機株式会社 | Heat pump water heater |
-
2017
- 2017-03-16 JP JP2017051091A patent/JP6532494B2/en active Active
- 2017-09-08 WO PCT/JP2017/032491 patent/WO2018168012A1/en active Application Filing
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| TWI781329B (en) * | 2018-07-06 | 2022-10-21 | 日商栗田工業股份有限公司 | Reverse osmosis treatment method and system |
Also Published As
| Publication number | Publication date |
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| JP2018153732A (en) | 2018-10-04 |
| JP6532494B2 (en) | 2019-06-19 |
| WO2018168012A1 (en) | 2018-09-20 |
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