WO2010103640A1 - 軟水化装置の運転方法および軟水化装置 - Google Patents

軟水化装置の運転方法および軟水化装置 Download PDF

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WO2010103640A1
WO2010103640A1 PCT/JP2009/054741 JP2009054741W WO2010103640A1 WO 2010103640 A1 WO2010103640 A1 WO 2010103640A1 JP 2009054741 W JP2009054741 W JP 2009054741W WO 2010103640 A1 WO2010103640 A1 WO 2010103640A1
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predetermined
water
hardness
resin bed
regeneration
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PCT/JP2009/054741
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English (en)
French (fr)
Japanese (ja)
Inventor
剛 米田
三郎 中村
元 安部
伸司 松友
隼人 渡邉
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三浦工業株式会社
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Application filed by 三浦工業株式会社 filed Critical 三浦工業株式会社
Priority to PCT/JP2009/054741 priority Critical patent/WO2010103640A1/ja
Priority to CN2009801005118A priority patent/CN101970110B/zh
Priority to JP2009525824A priority patent/JP4432122B1/ja
Priority to KR1020107000712A priority patent/KR101170066B1/ko
Publication of WO2010103640A1 publication Critical patent/WO2010103640A1/ja

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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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J49/00—Regeneration or reactivation of ion-exchangers; Apparatus therefor
    • B01J49/75—Regeneration or reactivation of ion-exchangers; Apparatus therefor of water softeners
    • 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
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C02F2001/425—Treatment of water, waste water, or sewage by ion-exchange using cation exchangers

Definitions

  • the present invention relates to a method for operating a water softening device that performs split flow regeneration and a water softening device.
  • the regeneration mode and the extrusion mode in the regeneration process are generally performed using treated water (softened water) as in Patent Document 1.
  • treated water softened water
  • a treated water storage tank and a water pump are required, and the structure of a process control valve for switching the flow path of the water softening device becomes complicated.
  • the problem is that when the extrusion mode is performed with raw water, the hardness leak level in the water softening process is high and the purity of the treated water is lowered. This decrease in the purity of the treated water becomes remarkable when poor raw water (total hardness of 200 to 300 mg CaCO 3 / L or more) is used. For this reason, if the adjustment of the hardness leak level is mistaken, a serious scale failure may be caused in the boiler device or the reverse osmosis membrane device.
  • the present inventors conducted tests and studies as to what factor the hardness leak level is related to and governed.
  • the average leak hardness in the water softening process is as follows: bottom resin bed depth, regeneration level, extrusion linear velocity, extrusion amount (a number indicating how many times the amount of water is used for extruding the regenerant), total It has been found to be related to hardness and electrical conductivity.
  • the purity (average leak hardness is 3 mgCaCO 3 / L or less, preferably not causing scale obstacles to the boiler device or reverse osmosis membrane device) Is 1 mg CaCO 3 / L or less, more preferably 0.1 mg CaCO 3 / L or less), and by securing the same amount of water sampled as that of other water softening devices, it is highly economical. Has led to the completion of a split flow regeneration process.
  • the present invention ensures treated water having a purity equal to or lower than the allowable leak hardness even when inferior raw water is used as extrusion water, and ensures a water sampling amount equivalent to that of other water softening devices of the regeneration method.
  • the purpose is to achieve high economic efficiency.
  • the raw water having a predetermined electric conductivity K and a predetermined total hardness H is passed through a cation exchange resin bed having a predetermined total resin bed depth D1 in a descending flow, and treated water is passed through.
  • a split flow regeneration process in which a regenerant or raw water is collected from both sides of the upper and lower ends of the resin bed and collected at a substantially central portion of the resin bed, the regeneration process comprising: (a) A regenerant passing mode in which a sodium chloride aqueous solution or a potassium chloride aqueous solution having a predetermined regeneration level R is passed through the resin bed at a predetermined regenerant concentration C and a predetermined regeneration linear velocity V1, and (b) the lower resin following the regenerant pass mode.
  • At least a raw water extrusion mode in which raw water of a predetermined extrusion amount N passes through the floor at a predetermined extrusion linear velocity V2, and (c) in a water softening process after a regeneration process at a predetermined water temperature.
  • this is a method of operating a water softening device in which a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N when raw water having a predetermined total hardness H is used are set by the following steps (1) to (3).
  • Predetermined lower resin bed depth D2 predetermined electrical conductivity K, predetermined total hardness H, predetermined regeneration level R, predetermined regenerant concentration C, desired hardness removal capacity X in the water softening process after the regeneration process, and treated water
  • Various conditions including the allowable leak hardness Y are given.
  • the hardness removal capacity x is related to the reproduction level r and the reproduction linear velocity v1, a predetermined reproduction linear velocity V1 that is equal to or higher than the desired hardness removal capacitance X is set.
  • a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N at which the leakage hardness y of the treated water is equal to or less than the allowable leakage hardness Y are set.
  • treated water having a purity equal to or lower than the allowable leak hardness Y can be secured, and a water sampling amount equivalent to that of other water softening devices of the regeneration system can be secured.
  • high economic efficiency can be realized.
  • the second invention is an operation method of the water softening device in which the predetermined extrusion linear velocity V2 in step (3) is obtained according to a correlation with a predetermined regeneration linear velocity V1.
  • the predetermined extrusion linear velocity V2 can be automatically set by setting the predetermined regeneration linear velocity V1.
  • the third invention relates to the predetermined lower resin bed depth D2, the predetermined electrical conductivity K, the predetermined total hardness H, the predetermined regeneration level R, the predetermined regenerant concentration C, the desired hardness removal capacity X and the allowable leak hardness Y in step (1).
  • D2 150 to 750 mm
  • K 150 to 750 mm
  • K ⁇ 1500 ⁇ S / cm
  • H 500 mg
  • R 60 to 240 g / LR
  • C 5 to 15 wt%
  • X 30 to 60 g CaCO 3 / L -R
  • Y ⁇ 3 mg CaCO 3 / L is the water softener operation method set.
  • a desired hardness removal capacity X 30 can be set ⁇ 60gCaCO 3 / L-R and allowable leak hardness Y ⁇ 3mgCaCO 3 / L purity of the treated water given extrusion line speed it is possible to generate the V2 and the predetermined extrusion rate N.
  • the fourth invention is an operation method of a water softening device in which the predetermined regeneration linear velocity V1 and the predetermined extrusion linear velocity V2 in steps (2) and (3) are set in a range of 0.7 to 2 m / s.
  • a stable regeneration operation can be realized by setting the predetermined regeneration linear velocity V1 and the predetermined extrusion linear velocity V2 to 0.7 m / s or more.
  • raw water having a predetermined electric conductivity K ⁇ 1500 ⁇ S / cm and a predetermined total hardness H ⁇ 500 mgCaCO 3 / L is applied to a cation exchange resin bed having a predetermined total resin bed depth D1.
  • the fifth aspect of the present invention when raw water having a predetermined electrical conductivity K ⁇ 1500 ⁇ S / cm and a predetermined total hardness H ⁇ 500 mgCaCO 3 / L is used, the same amount of water sample as that of other regeneration-type water softening devices is secured. As a result, it is possible to realize high economic efficiency and to generate treated water having a purity of allowable leak hardness Y ⁇ 3 mg CaCO 3 / L. Further, by setting the predetermined regeneration linear velocity V1 and the predetermined extrusion linear velocity to 0.7 m / s or more, a stable regeneration operation can be realized.
  • the sixth invention for achieving the above object obtains treated water by passing raw water having a predetermined electric conductivity K and a predetermined total hardness H in a downward flow through a cation exchange resin bed having a predetermined total resin bed height D1.
  • a controller that performs a water softening process and a split flow regeneration process that collects the regenerant or raw water from the both sides of the upper and lower ends of the resin bed and collects at a substantially central portion of the resin bed,
  • a regeneration agent in which a sodium chloride aqueous solution or a potassium chloride aqueous solution having a predetermined regeneration level R is passed through the resin bed at a predetermined regeneration agent concentration C and a predetermined regeneration linear velocity V1, and (b) a regeneration agent
  • At least a raw water extruding mode in which a predetermined amount of raw water N is passed through the lower resin bed at a predetermined extrusion linear velocity V2 is executed, and (c) regeneration at a predetermined water temperature.
  • the leakage hardness y of the treated water in the water softening process after the process is related to the lower resin bed depth d2, the electrical conductivity k, the total hardness h, the regeneration level r, the extrusion linear velocity v2, and the extrusion amount n.
  • a water softening device in which a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N when raw water having a predetermined electrical conductivity K and a predetermined total hardness H is set in advance by the following steps (1) to (3).
  • Predetermined lower resin bed depth D2 predetermined electrical conductivity K, predetermined total hardness H, predetermined regeneration level R, predetermined regenerant concentration C, desired hardness removal capacity X in the water softening process after the regeneration process, and treated water
  • Various conditions including the allowable leak hardness Y are given.
  • a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N at which the leakage hardness y of the treated water is equal to or less than the allowable leakage hardness Y are set.
  • treated water having a purity equal to or lower than the allowable leak hardness Y can be ensured, and the amount of water sampled equivalent to that of other water softening devices of the regeneration system can be ensured.
  • high economic efficiency can be realized.
  • a seventh invention is the water softening device according to the sixth invention, wherein the predetermined extrusion linear velocity V2 in step (3) is determined according to a correlation with a predetermined regeneration linear velocity V1.
  • the predetermined extrusion linear velocity V2 can be automatically set by setting the predetermined regeneration linear velocity V1.
  • a desired hardness removal capacity X 30 can be set ⁇ 60gCaCO 3 / L-R and allowable leak hardness Y ⁇ 3mgCaCO 3 / L purity of the treated water given extrusion line speed it is possible to generate the V2 and the predetermined extrusion rate N.
  • raw water having a predetermined electric conductivity K ⁇ 1500 ⁇ S / cm and a predetermined total hardness H ⁇ 500 mgCaCO 3 / L is applied to a cation exchange resin bed having a predetermined total resin bed depth D1.
  • the ninth invention when raw water having a predetermined electric conductivity K ⁇ 1500 ⁇ S / cm and a predetermined total hardness H ⁇ 500 mgCaCO 3 / L is used, a water sampling amount equivalent to that of other water softening devices of other regeneration methods is secured. As a result, it is possible to realize high economic efficiency and to generate treated water having a purity of allowable leak hardness Y ⁇ 3 mg CaCO 3 / L. Further, by setting the predetermined regeneration linear velocity V1 and the predetermined extrusion linear velocity to 0.7 m / s or more, a stable regeneration operation can be realized.
  • the process flow and conditions of the water softener are shown.
  • the relationship between the extrusion linear velocity v2 and the extrusion amount n in the allowable leak hardness Y is shown.
  • the relationship between the reproduction linear velocity v1 and the hardness removal capacity x is shown.
  • An appropriate range of the regeneration linear velocity v1 and the extrusion amount n is shown.
  • the whole structure of a water softening device is shown.
  • the flow of the water softening process is shown.
  • the flow of regenerant passage mode is shown.
  • the flow of raw water extrusion mode is shown.
  • the structure of the boiler system using a water softening device is shown.
  • the structure of the reverse osmosis membrane system using a water softening apparatus is shown.
  • the raw water having a predetermined electrical conductivity K and a predetermined total hardness H is passed through the cation exchange resin bed having the predetermined total resin bed depth D1 in a descending flow.
  • the predetermined electrical conductivity K corresponds to the amount of dissolved ions in the raw water, and can be replaced with the soluble evaporation residue TDS. In the case of tap water or industrial water, the relationship is generally TDS [mg / L] ⁇ 0.5 to 0.7 ⁇ K [ ⁇ S / cm].
  • the regeneration process includes at least the following modes (a) and (b).
  • a solid line arrow S11 indicates raw water
  • a one-dot chain line arrow S12 indicates that ion exchange is performed in the middle and finally flows out as treated water.
  • the regenerant passing mode as indicated by broken line arrows S21 and S22, the regenerant is distributed from both sides of the upper end and the lower end of the resin bed while being collected by the collector located at the approximate center of the resin bed, and then the broken line As shown by arrow S23, it shows flowing out of the resin bed.
  • raw water is distributed from both sides of the upper and lower ends of the resin bed, and collected by a collector located at substantially the center of the resin bed while extruding the regenerant. After that, as shown by a solid line arrow S33, it indicates that the resin flows out of the resin bed.
  • the reproduction process includes the following setting method (C).
  • this setting method (C) a desired hardness removal capacity X is ensured as the hardness removal capacity x, and the average leakage hardness y of treated water (hereinafter simply referred to as “leak hardness y”) is equal to or less than the allowable leakage hardness Y.
  • the extrusion linear velocity v2 and the extrusion amount n are set or adjusted to the predetermined extrusion linear velocity V2 and the predetermined extrusion amount N.
  • the leak hardness y is defined as the average value of the leak hardness of the treated water collected from immediately after the start of the water softening process to the through point (for example, 1 mg CaCO 3 / L).
  • the allowable leak hardness Y is the hardness of water that is allowed at the treated water supply destination.
  • the allowable leak hardness Y is determined based on the concentration rate in the device and the solubility of scale species such as calcium carbonate.
  • the predetermined extrusion linear velocity V2 and the predetermined extrusion amount N are set in such a manner that the leakage hardness y of the treated water in the water softening process performed after the regeneration process is lower resin bed depth d2, electrical conductivity k, total hardness h, regeneration level. It was created based on the new knowledge that it is related to and controlled by parameters including r, extrusion linear velocity v2 and extrusion amount n. And this new knowledge is represented by the following formula 1 which shows the relation between leak hardness y and each above-mentioned parameter.
  • Equation 1 The unit of each parameter in Equation 1 is as follows. d2: Lower resin floor depth [mm] k: Electric conductivity of raw water [ ⁇ S / cm] h: Total hardness of raw water [mgCaCO 3 / L] r: regeneration level [g / LR (g ⁇ NaCl / LR or g ⁇ KCl / LR)] v2: extrusion linear velocity [m / s] n: Extrusion amount [BV (Bed Volume)]
  • Formula 1 is obtained by the inventors performing various experiments and approximating experimental results under the condition that the raw water temperature is constant.
  • the approximate expression is not limited to Expression 1 as long as it includes the above-described parameters.
  • the leakage hardness y of the treated water can be made equal to or less than the allowable leakage hardness Y by adjusting the value of each parameter on the right side.
  • the allowable leak hardness Y of the boiler device is 3 mgCaCO 3 / L or less, preferably 1 mgCaCO 3 / L or less.
  • the amount is preferably 0.1 mgCaCO 3 / L or less.
  • the allowable leak hardness Y of the reverse osmosis membrane device is 3 mgCaCO 3 / L or less, preferably 1 mgCaCO 3 / L or less.
  • Equation 1 when adjusting the leakage hardness y of the treated water to the allowable leakage hardness Y or less using Equation 1, among the parameters, the lower resin bed depth d2, the electrical conductivity k, the total hardness h, and the predetermined regeneration level r are set.
  • the following condition values are given from the viewpoint of designing a practical water softening device.
  • the predetermined lower resin bed depth D2 given to the lower resin bed depth d2 is D2 ⁇ 0.2 to 0.8 ⁇ D1 in relation to the predetermined total resin bed depth D1.
  • the reason is as follows.
  • the upper resin floor depth (depth from the upper end of the resin floor to the collector) and the lower resin floor depth (depth from the collector to the lower end of the resin floor) are greatly different, various problems arise.
  • the difference between the ratio of the upper resin bed depth and the ratio of the lower resin bed depth is extremely large, if the regenerant is distributed almost evenly, the substantial regeneration level of the upper resin bed and the lower resin bed The difference of r becomes extremely large.
  • the regeneration level r on the side where the floor depth is shallow (the side where the amount of resin is small) is excessively higher than the regeneration level r on the side where the floor depth is deep (the side where the amount of resin is large). For this reason, the regeneration efficiency on the side where the floor depth is deep is lowered, and as a result, the regeneration efficiency of the entire resin bed is also lowered.
  • the ratio of the upper resin bed to the entire resin bed is small, the resin flow restraining force during regeneration is reduced, which may cause regeneration failure. Therefore, a ratio of 1: 1 between the upper resin bed depth and the lower resin bed depth is most suitable from the viewpoint of stability and economy of regeneration. However, since it is acceptable even if the balance is somewhat poor, the ratio of the predetermined lower resin bed depth D2 to the predetermined total resin bed depth D1 is set in the range of 0.2 to 0.8.
  • the predetermined total resin bed depth D1 has a lower limit and an upper limit for the following reason.
  • the lower limit will be described.
  • a regenerant drift and a short pass are likely to occur, resulting in a decrease in regeneration efficiency.
  • the formation of an ion exchange zone shortens the layer length that can be effectively used, and the ion exchange capacity (through-flow exchange capacity) decreases. Therefore, in the design of a water softening device in which the amount of cation exchange resin exceeds 20 L, a bed depth of 800 mm or more is usually recommended.
  • the lower limit is 300 mm.
  • the upper limit will be described. Essentially, no upper limit is needed. However, a water softening device having a floor depth of 1500 mm or more is unlikely to be manufactured due to transportation reasons and vessel manufacturing reasons for accommodating a cation exchange resin. Therefore, the upper limit is 1500 mm.
  • the predetermined total resin bed depth D1 is set in the range of 300 to 1500 mm.
  • the predetermined lower resin bed depth is set in the range of 150 to 750 mm by setting D2 ⁇ 0.5 ⁇ D1.
  • the predetermined electric conductivity K given to the electric conductivity k is 1500 ⁇ S / cm or less
  • the predetermined total hardness H given to the total hardness h is 500 mgCaCO 3 / L or less.
  • the water softening device according to the present embodiment is intended to be used particularly in the Chinese continent and the North American continent. In these continents, most of the natural water used for boiler feed water and the like has an electric conductivity of 1500 ⁇ S / cm or less and a total hardness of 500 mg CaCO 3 / L or less.
  • the predetermined reproduction level R given to the reproduction level r is 60 to 240 g / LR.
  • the playback level is extremely high, the playback efficiency decreases. That is, it is uneconomical.
  • the playback level is extremely low, the playback frequency increases.
  • the predetermined reproduction level R is set to the above range as a common sense range.
  • the parameters for adjusting the leakage hardness y are substantially given by giving predetermined values D2, K, H and R to the lower resin bed depth d2, the electrical conductivity k, the total hardness h and the regeneration level r. It is summarized in the extrusion amount n and the extrusion linear velocity v2. Of course, in setting parameters other than the extrusion amount n and the extrusion linear velocity v2, these parameters can be set to values that reduce the leak hardness y.
  • Equation 1 in order to reduce the leak hardness y, the extrusion linear velocity v2 in the raw water extrusion mode may be increased. This means that if the passing speed of the raw water is increased, the amount of adsorption of the hardness component in the lower resin bed is reduced. Further, Equation 1 means that the leakage hardness y is reduced by reducing the extrusion amount n.
  • the degree of decrease in the leak hardness y with respect to the increase in the extrusion linear velocity v2 or the decrease in the extrusion amount n indicates that the decrease in the extrusion amount n has a larger influence than the increase in the extrusion linear velocity v2.
  • the extrusion amount n that achieves an allowable leak hardness Y or less such as boiler feed water can be expressed as the following Equations 2 and 3 using the extrusion linear velocity v2 as a parameter.
  • the leak hardness y exceeds the allowable leak hardness Y in the region above the line Q1, and is less than the allowable leak hardness Y in the region below.
  • the extrusion linear velocity v2 can decrease the leak hardness y as the value thereof is increased, but generally has a constraint condition.
  • the restriction condition is that the extrusion linear velocity v2 and the regeneration linear velocity v1 depend on the raw water pressure and the structure of the water softening device, and have a correlation unless individually equipped with a flow rate adjusting means. is there.
  • the present invention is not limited to the case where both have a correlation, but when they have a correlation, they can be handled as follows.
  • Equation 2 if the extrusion linear velocity v2 and the regeneration linear velocity v1 have a correlation, and the extrusion linear velocity v2 can be approximated by the regeneration linear velocity v1, the extrusion amount n is an equation 4 with the regeneration linear velocity v1 as a variable. It is expressed by When the extrusion linear velocity v2 is not approximated by the reproduction linear velocity v1, the relational expression corresponding to Expression 4 can be obtained by substituting the relational expression between v2 and v1 into Expression 2.
  • Equation 5 f 1 (n) is a function of the extrusion amount n, and the value increases as n increases.
  • F 2 (v2) is a function of the extrusion linear velocity v2, and increases as v2 decreases.
  • f 2 (v2) exp ( ⁇ ⁇ v2).
  • Equation 6 f 3 (v2) is a function of the extrusion linear velocity v2, and the value increases as v2 increases.
  • f 3 (v2) 1 / exp ( ⁇ ⁇ v2).
  • a 3 is a coefficient that varies depending on the allowable leak hardness Y.
  • the reproduction linear velocity v1 is the main dominant factor that determines the hardness removal capacity x together with the reproduction level r.
  • the hardness removal capacity x of the water softening device has substantially the same meaning as the ion exchange capacity.
  • a method for calculating the hardness removal capacity of the water softening device has been proposed for a long time, and the following equation 8 is shown as an example.
  • x1 is a basic hardness removal capacity and is represented by a function depending on the reproduction level r. This x1 is slightly different depending on the type of cation exchange resin. G 1 to g 8 are factors that increase or decrease x1 according to various conditions of the water softening device.
  • the factors g 1 to g 8 are respectively the electric conductivity k of the raw water, the temperature t of the raw water, the ratio s of sodium ions to the total cations, the ratio b of the pour point hardness to the raw water hardness, the water flow velocity w, the total resin bed Normally, it is set to around 1 (substantially in the range of about 0.5 to 1.5) according to changes in the depth d1, the regeneration linear velocity v1 and the regeneration agent concentration c.
  • the regenerant concentration c is set in the range of 5 to 15 wt% in the case of a standard water softening device.
  • the method for obtaining the hardness removal capacity x is not limited to the above equation 8, but can be generalized to the following equation 9.
  • Equation 9 f 5 (v1) is a function of the reproduction linear velocity v1, and the value increases as v1 increases. Further, a 5 are coefficients that change depending on the conditions of the water softener.
  • the hardness removal capacity x expressed by the equations 8 and 9 is the amount of treated water collected. As indicated by the line Q2 in FIG. 3, the hardness removal capacity x has a characteristic that increases as the reproduction linear velocity v1 decreases.
  • the desired hardness removal capacity X is set in the range of 30 to 60 g CaCO 3 / LR from the viewpoint of securing the same economic efficiency as that of the water softening device of the cocurrent regeneration type. This desired hardness removal capacity X corresponds to the case where the desired regeneration level R is 60 to 240 g / LR.
  • the reproduction linear velocity v1 is determined by the hardness removal capacity x. That is, given the desired hardness removal capacity X, the predetermined reproduction linear velocity V1 is determined.
  • the upper and lower limits are determined for the following reasons. First, the upper limit will be described. Split flow regeneration tends to shorten the contact time between the cation exchange resin bed and the regenerant compared to cocurrent regeneration. For this reason, it is necessary to suppress the upper limit of the reproduction linear velocity and to promote the reproduction by extending the contact time. Accordingly, the predetermined regeneration linear velocity V1 is preferably set to 2 m / s or less in order to secure 43 g CaCO 3 / LR as the desired hardness removal capacity X equivalent to the cocurrent regeneration.
  • This upper limit is represented by the line Q3 in FIGS. 3 and 4, and the region on the left side of the line Q3 indicates the range of the reproduction linear velocity v1 in which the hardness removal capacity x exceeds the desired hardness removal capacity X. Conversely, the region on the right side of the line Q3 indicates the range of the reproduction linear velocity v1 in which the hardness removal capacity x is less than the desired hardness removal capacity X.
  • the lower limit will be described. According to the knowledge of the present inventors, when the regeneration linear velocity v1 is less than 0.7 m / s, the regenerant drift and short path are likely to occur in the resin bed. This lower limit is represented by a line Q4 in FIG.
  • the predetermined reproduction linear velocity V1 is not more than the upper limit (the region on the left side of the line Q3 in FIG. 4), and preferably in the range of 0.7 to 2 m / s (between the lines Q3 and Q4 in FIG. 4). Area).
  • Equation 4 an upper limit of the predetermined extrusion amount N that realizes the allowable leak hardness Y or less is obtained by Equation 4. Can do. Since this upper limit is represented by the line Q1 in FIG. 4, the maximum value of the predetermined extrusion amount N is 2.5 BV corresponding to the intersection of the line Q1 and the line Q3. On the other hand, the lower limit of the predetermined extrusion amount N is 0.4 BV corresponding to the porosity of the resin bed. This lower limit is represented by the line Q5 in FIG.
  • the predetermined extrusion amount N is not more than the upper limit, and is preferably set in a range of 0.4 to 2.5 BV (a region between the line Q1 and the line Q5 in FIG. 4).
  • the preferable appropriate range of the predetermined regeneration linear velocity V1 and the predetermined extrusion amount N is the region A surrounded by the line Q1, the line Q3, the line Q4, and the line Q5 as shown in FIG.
  • the line Q1 indicating the allowable leak hardness Y is according to Equation 3. That is, the operation method of this embodiment can be said to be a method of obtaining the line Q1 by giving various conditions and setting the predetermined regeneration linear velocity V1 and the predetermined extrusion amount N within the range of the region A.
  • the predetermined extrusion amount N that realizes the allowable leak hardness Y or less can be obtained from Equation 2 by setting the predetermined extrusion linear velocity V2 separately from the predetermined regeneration linear velocity V1. .
  • the method (C) for setting or adjusting the predetermined extrusion linear velocity V2 and the predetermined extrusion amount N based on the new knowledge includes the following steps (1) to (3).
  • Predetermined lower resin bed depth D2 predetermined electrical conductivity K, predetermined total hardness H, predetermined regeneration level R, predetermined regenerant concentration C, desired hardness removal capacity X in the water softening process after the regeneration process, and treated water Various conditions including the allowable leak hardness Y are given.
  • a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N at which the leakage hardness y of the treated water is equal to or less than the allowable leakage hardness Y are set.
  • the values of the parameters affecting the leak hardness y are preferably set as follows.
  • a predetermined lower resin bed depth D2 a predetermined electrical conductivity K, a predetermined total hardness H, a predetermined regeneration level R, a predetermined regenerant concentration C, a desired hardness removal capacity X and an allowable leak hardness Y.
  • D2 150 to 750 mm
  • K 150 to 750 mm
  • K ⁇ 1500 ⁇ S / cm
  • H 500 mg CaCO 3 / L
  • R 60 to 240 g / LR
  • C 5 to 15 wt%
  • X 30 to 60 g CaCO 3 / L -R
  • Y ⁇ 3 mg CaCO 3 / L is preferably set as follows.
  • step (2) the predetermined reproduction linear velocity V1 at which the desired hardness removal capacity X is set is set in the range of 0.7 to 2 m / s.
  • step (3) the predetermined extrusion linear velocity V2 is obtained according to a correlation with a predetermined reproduction linear velocity V1.
  • the predetermined extrusion amount N is set in the range of 0.4 to 2.5 BV according to Equation 4.
  • the present embodiment includes the following method of operating the water softening device. That is, the raw water having a predetermined electrical conductivity K ⁇ 1500 ⁇ S / cm and a predetermined total hardness H ⁇ 500 mg CaCO 3 / L is passed through the cation exchange resin bed having the predetermined total resin bed depth D1 in a descending flow, and the treated water is supplied.
  • the predetermined extrusion amount N and the like are adjusted so as to satisfy the allowable leak hardness Y. That is, the predetermined reproduction linear velocity V1 is set within the range of 0.7 to 2 m / s below the upper limit at which the desired hardness removal capacity X is secured. And predetermined extrusion linear velocity V2 is calculated
  • the regeneration process can include a well-known backwash mode, wash mode, water replenishment mode, and the like.
  • the present embodiment is a water softening device that realizes the above operation method.
  • the water softening device includes a softening process for obtaining treated water by passing raw water having a predetermined electrical conductivity K and a predetermined total hardness H in a downward flow through a cation exchange resin bed having a predetermined total resin bed depth D1.
  • a controller that performs a split flow regeneration process that collects the regenerant or raw water from both sides of the upper and lower ends of the resin bed and collects at a substantially central part of the resin bed, (A) A regeneration agent passing mode in which a sodium chloride aqueous solution or a potassium chloride aqueous solution having a predetermined regeneration level R is passed through the resin bed at a predetermined regeneration agent concentration C and a predetermined regeneration linear velocity V1, and (b) a regeneration agent passage mode.
  • At least a raw water extrusion mode in which raw water of a predetermined extrusion amount N is passed through the lower resin bed at a predetermined extrusion linear velocity V2, and (c) a regeneration process at a predetermined water temperature
  • the leakage hardness y of the treated water in the water softening process is related to the lower resin bed depth d2, the electrical conductivity k, the total hardness h, the regeneration level r, the extrusion linear velocity v2, and the extrusion amount n.
  • the predetermined extrusion linear velocity V2 and the predetermined extrusion amount N when using raw water having an electrical conductivity K and a predetermined total hardness H are set in advance by the following steps (1) to (3).
  • Predetermined lower resin bed depth D2 predetermined electrical conductivity K, predetermined total hardness H, predetermined regeneration level R, predetermined regenerant concentration C, desired hardness removal capacity X in the water softening process after the regeneration process, and treated water
  • Various conditions including the allowable leak hardness Y are given.
  • a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N at which the leakage hardness y of the treated water is equal to or less than the allowable leakage hardness Y are set.
  • the predetermined extrusion amount N is set in advance by steps (1) to (3), and the raw water extrusion step is controlled so that the extrusion amount n in the raw water extrusion mode becomes the set predetermined extrusion amount N.
  • This control can be easily performed by a timer, but it is also possible to provide a flow meter so that when the flow meter counts the predetermined extrusion amount N, the raw water extrusion mode is terminated.
  • the values of the parameters affecting the leak hardness y are preferably set as follows.
  • a predetermined lower resin bed depth D2 a predetermined electrical conductivity K, a predetermined total hardness H, a predetermined regeneration level R, a predetermined regenerant concentration C, a desired hardness removal capacity X and an allowable leak hardness Y.
  • D2 150 to 750 mm
  • K 150 to 750 mm
  • K ⁇ 1500 ⁇ S / cm
  • H 500 mg CaCO 3 / L
  • R 60 to 240 g / LR
  • C 5 to 15 wt%
  • X 30 to 60 g CaCO 3 / L -R
  • Y ⁇ 3 mg CaCO 3 / L is preferably set as follows.
  • step (2) the predetermined reproduction linear velocity V1 at which the desired hardness removal capacity X is set is set in the range of 0.7 to 2 m / s.
  • step (3) the predetermined extrusion linear velocity V2 is obtained according to a correlation with a predetermined reproduction linear velocity V1.
  • the predetermined extrusion amount N is set in the range of 0.4 to 2.5 BV according to Equation 4.
  • FIG. 5 shows the overall configuration of the water softening device according to this embodiment.
  • the water softening device 1 is connected to residential buildings such as houses and condominiums, customer-collecting facilities such as hotels and public baths, cooling and heating devices such as boilers and cooling towers, and water-using devices such as food processing devices and washing devices.
  • the water softening device 1 mainly includes a resin storage tank 2, a process control valve 3, and a salt water supply device 4.
  • the resin storage tank 2 includes a bottomed vessel 6 filled with a cation exchange resin bed 5 (predetermined bed depth: D1).
  • the opening of the vessel 6 is closed with a cap 7.
  • a process control valve 3 is integrally attached to the cap 7, and the flow path of the water softening process and the flow path of the regeneration process of the water softening device 1 can be switched by a command signal from the controller 1C. It is configured as follows.
  • the cap 7 is formed with a first flow path 8, a second flow path 9 and a third flow path 10 for supplying and discharging fluid. Each of these flow paths 8, 9, and 10 is connected to various lines constituting the process control valve 3, as will be described later.
  • the first collecting pipe 11 extending near the bottom of the vessel 6 is connected to the first flow path 8.
  • a first screen 12 that prevents the resin beads from flowing out is attached to the tip of the first collection tube 11. That is, the inside of the first collection pipe 11 is communicated with the first flow path 8, and the collection position by the first screen 12 is set near the bottom of the vessel 6.
  • the second flow path 9 is connected to a second collection pipe 13 that extends to a substantially central portion (predetermined bed depth: D2) of the cation exchange resin bed 5.
  • a second screen 14 for preventing the resin beads from flowing out is attached to the tip of the second collection tube 13. That is, the inside of the second collection tube 13 is communicated with the second flow path 9, and the collection position by the second screen 14 is set at a substantially central portion of the cation exchange resin bed 5.
  • the inner diameter of the second collection tube 13 is set to be larger than the outer diameter of the first collection tube 11. Further, the axial cores of both the collecting pipes 11 and 13 are set coaxially with the axial core of the resin storage tank 2. That is, both the collecting pipes 11 and 13 are attached to the resin storage tank 2 as a collector of a double pipe structure in which the first collecting pipe 11 is set as an inner pipe and the second collecting pipe 13 is set as an outer pipe. .
  • a third screen 15 for preventing the resin beads from flowing out is mounted on the lower surface side of the cap 7. That is, the third flow path 10 communicates with the inside of the resin storage tank 2 through the third screen 15.
  • the raw water line 16 is connected to the third flow path 10 via the process control valve 3.
  • a treated water line 17 is connected to the first flow path 8 via the process control valve 3. That is, a part of the raw water line 16 and the treated water line 17 are formed in the process control valve 3, respectively.
  • the raw water line 16 is provided with a pressure switch 18 and a first valve 19 in order from the upstream side.
  • the pressure switch 18 is provided in order to detect the presence or absence of raw water pressure in the regeneration process, and is, for example, a type that turns on and off at a pressure of about 0.1 MPa necessary for normally performing the regeneration process.
  • a second valve 20 is provided in the treated water line 17.
  • the pressure switch 18, the first valve 19 and the second valve 20 are all incorporated in the process control valve 3.
  • the raw water line 16 on the upstream side of the first valve 19 is connected to the treated water line 17 on the downstream side of the second valve 20 by a bypass line 21.
  • the bypass line 21 is provided with a third valve 22.
  • the raw water line 16 on the upstream side of the first valve 19 is connected to the treated water line 17 on the upstream side of the second valve 20 by the first regenerant line 23.
  • a strainer 24 In the first regenerant line 23, a strainer 24, a first constant flow valve 25, an ejector 26, a fourth valve 27, and a first orifice 28 are provided in this order from the raw water line 16 side.
  • the strainer 24 is for removing suspended substances contained in the raw water and preventing the first constant flow valve 25 and the ejector 26 from being clogged.
  • the first constant flow valve 25 is for adjusting the raw water supplied to the ejector 26 to a flow rate within a predetermined range.
  • the first regenerant line 23 between the ejector 26 and the fourth valve 27 is connected to the raw water line 16 and the second regenerant line 29 on the downstream side of the first valve 19.
  • the second regenerant line 29 is provided with a second orifice 30.
  • the first orifice 28 and the second orifice 30 are for evenly distributing the regenerant or the raw water to the first flow path 8 and the third flow path 10 in the regenerant passage mode and the raw water extrusion mode described later. is there.
  • a salt water line 31 extending from the salt water supply device 4 is connected to the discharge side of the nozzle portion of the ejector 26.
  • the salt water line 31 is provided with a fifth valve 32.
  • the ejector 26 is configured to be able to suck salt water (for example, a saturated aqueous solution of sodium chloride) from the salt water supply device 4 using negative pressure generated when raw water is discharged from the nozzle portion.
  • salt water from the salt water supply device 4 is diluted with raw water to a predetermined regenerant concentration C (5 to 15 wt%).
  • a first drain line 33 extending to the outside of the process control valve 3 is connected to the treated water line 17 upstream of the second valve 20.
  • the first drainage line 33 is provided with a sixth valve 34 and a second constant flow valve 35 in order from the treated water line 17 side.
  • the second regenerant line 29 on the downstream side of the second orifice 30 is connected to the first drain line 33 and the second drain line 36 on the downstream side of the sixth valve 34.
  • the second drain line 36 is provided with a seventh valve 37.
  • the second flow path 9 is connected to the first drain line 33 and the third drain line 38 on the downstream side of the sixth valve 34.
  • the third drain line 38 is provided with an eighth valve 39.
  • the second constant flow valve 35 is for adjusting the amount of drainage from the resin storage tank 2 to a predetermined range of flow rate.
  • the third drain line 38 is connected to the downstream side of the second constant flow valve 35, but can be connected to the downstream side of the second constant flow valve 35 in order to reduce pressure loss.
  • the salt water supply device 4 includes a salt water tank 40.
  • a cylindrical salt water well 41 In the salt water tank 40, a cylindrical salt water well 41, and a water permeable plate 43 that partitions a salt water storage part and a storage part of regenerated salt 42 (for example, granular or pellet sodium chloride) are arranged. Yes.
  • a communication hole 44 is provided in the lower side wall of the salt water well 41 so that salt water or makeup water can freely flow therethrough.
  • a strainer 45 is accommodated in the salt water well 41.
  • the strainer 45 incorporates an air check ball 46 and a valve seat 47 with which the air check ball 46 abuts or separates.
  • the valve seat 47 is connected to the salt water line 31. That is, the process control valve 3 is connected to the salt water tank 40 by the salt water line 31.
  • the salt water line 31 is provided with a flow meter 48 that detects the flow rate in the salt water supply direction and the flow rate in the makeup water supply direction. The detection signal from the flow meter 48 is input to the controller 1C.
  • the first valve 19 and the second valve 20 are each set to the open state by a command signal from the controller 1C.
  • the third valve 22, the fourth valve 27, the fifth valve 32, the sixth valve 34, the seventh valve 37, and the eighth valve 39 are each set in a closed state.
  • the raw water flowing through the raw water line 16 is distributed through the third screen 15 after being supplied through the third flow path 10 as indicated by a solid arrow S11.
  • the raw water distributed from the third screen 15 is softened by replacing the hardness component with Na ions or K ions in the process of passing through the cation exchange resin bed 5 in a downward flow.
  • the treated water that has passed through the cation exchange resin bed 5 is collected by the first screen 12, and then flows through the first collection pipe 11, the first flow path 8, and the treated water line 17 as indicated by a one-dot chain line arrow S12. , Supplied to youth points. Then, when the cation exchange resin bed 5 cannot replace the hardness component by collecting a predetermined amount of treated water, a regeneration process is performed.
  • a backwash mode In order to recover the hardness removal capacity of the cation exchange resin bed 5, a backwash mode, a regeneration agent passing mode, a raw water extrusion mode, a rinsing mode, and a water replenishment mode are performed in this order.
  • the backwash mode, the rinse mode, and the water replenishment mode are not directly related to the present invention and are well known as shown in Patent Document 2, and thus the description thereof is omitted.
  • the third valve 22, the fourth valve 27, the fifth valve 32, and the eighth valve 39 are each set to an open state by a command signal from the controller 1C.
  • the first valve 19, the second valve 20, the sixth valve 34, and the seventh valve 37 are each set to a closed state.
  • the raw water flowing through the raw water line 16 is supplied as dilution water to the primary side of the ejector 26 via the first regenerant line 23. At this time, suspended substances in the raw water are removed by the strainer 24.
  • the flow rate of the raw water is adjusted to a predetermined range by the first constant flow valve 25.
  • the salt water line 31 also has negative pressure. As a result, the salt water in the salt water tank 40 is sucked into the ejector 26 through the salt water line 31.
  • salt water is diluted with raw water to a predetermined regenerant concentration C to prepare a regenerant.
  • a part of the regenerant is supplied via the first regenerant line 23, the treated water line 17, the first flow path 8 and the first collection pipe 11, as indicated by the broken line arrow S ⁇ b> 21, and then the first screen 12. Distributed from.
  • the remainder of the regenerant is supplied from the third screen 15 after being supplied via the second regenerant line 29, the raw water line 16 and the third flow path 10 as indicated by the broken line arrow S22. At this time, the regenerant is evenly distributed by the first orifice 28 and the second orifice 30.
  • the regenerant distributed from the first screen 12 passes through the cation exchange resin bed 5 in an upward flow and regenerates the lower resin bed 5A.
  • the regenerant distributed from the third screen 15 passes through the cation exchange resin bed 5 in a downward flow and regenerates the upper resin bed. That is, in this embodiment, split flow regeneration of the cation exchange resin bed 5 is performed. At this time, the downward flow regenerant presses the resin bed downward, and the upward flow regenerant prevents the resin bed from spreading and flowing. Then, after the regenerant that has passed through the cation exchange resin bed 5 is collected by the second screen 14, the second collection pipe 13, the second flow path 9, and the third drainage line 38, as indicated by the dashed arrow S ⁇ b> 23. And discharged from the first drainage line 33 to the outside of the system.
  • the third valve 22, the fourth valve 27, and the eighth valve 39 are each set to an open state by a command signal from the controller 1C.
  • the 1st valve 19, the 2nd valve 20, the 5th valve 32, the 6th valve 34, and the 7th valve 37 are set as a closed state, respectively.
  • the raw water flowing through the raw water line 16 is supplied to the primary side of the ejector 26 through the first regenerant line 23 as extruded water. At this time, suspended substances in the raw water are removed by the strainer 24.
  • the raw water flow rate is the first constant flow rate.
  • a part of the raw water from the ejector 26 is supplied through the first regenerant line 23, the treated water line 17, the first flow path 8 and the first collection pipe 11 as indicated by the solid arrow S31. It is distributed from one screen 12.
  • the remainder of the raw water from the ejector 26 is supplied from the third screen 15 after being supplied through the second regenerant line 29, the raw water line 16 and the third flow path 10 as indicated by the solid arrow S32. The At this time, the raw water is evenly distributed by the first orifice 28 and the second orifice 30.
  • the raw water distributed from the first screen 12 passes through the cation exchange resin bed 5 in an upward flow while pushing out the regenerant, and continuously regenerates the lower resin bed 5A.
  • the raw water distributed from the third screen 15 passes through the cation exchange resin bed 5 in a downward flow while pushing out the regenerant, and continuously regenerates the upper resin bed.
  • the raw water in the downward flow presses the resin bed downward and suppresses the development and flow of the resin bed by the raw water in the upward flow.
  • the second collection pipe 13 the second flow path 9, and the third waste water are collected. It is discharged from the first drainage line 33 through the line 38 to the outside of the system.
  • this operation method is to soften water to obtain treated water by allowing raw water having a predetermined electrical conductivity K and a predetermined total hardness H to pass through the cation exchange resin bed 5 having a predetermined total resin bed depth D1 in a downward flow.
  • a split flow regeneration process that collects at approximately the center of the resin bed while distributing regenerant or raw water from both sides of the upper and lower ends of the resin bed, the regeneration process comprising: (a) On the other hand, a regenerant passing mode in which a sodium chloride aqueous solution or a potassium chloride aqueous solution having a predetermined regeneration level R is passed at a predetermined regenerant concentration C and a predetermined regeneration linear velocity V1, and (b) following the regenerant passing mode, At least a raw water extrusion mode in which raw water of a predetermined extrusion amount N is passed at a predetermined extrusion linear velocity V2, and (c) treatment in a water softening process after a regeneration process at a predetermined water temperature.
  • the predetermined electrical conductivity K and A predetermined extrusion linear velocity V2 and a predetermined extrusion amount N when using raw water having a predetermined total hardness H are set by the following steps (1) to (3).
  • Predetermined lower resin bed depth D2 predetermined electrical conductivity K, predetermined total hardness H, predetermined regeneration level R, predetermined regenerant concentration C, desired hardness removal capacity X in the water softening process after the regeneration process, and treated water
  • Various conditions including the allowable leak hardness Y are given.
  • a predetermined reproduction linear velocity V1 that is equal to or higher than the desired hardness removal capacitance X is set.
  • a predetermined extrusion linear velocity V2 and a predetermined extrusion amount N at which the leakage hardness y of the treated water is equal to or less than the allowable leakage hardness Y are set.
  • the leak hardness y is expressed by Equation 1.
  • the allowable leak hardness Y is set to 1 mgCaCO 3 / L which is preferable in the boiler apparatus, and the extrusion linear velocity v2 is approximated by the regeneration linear velocity v1, the extrusion amount n that realizes the allowable leak hardness Y is expressed as a function of the regeneration linear velocity v1. 4 is expressed.
  • Y 1 mgCaCO 3 / L.
  • the constants of Equations 1 to 4 can be obtained when creating Equation 1 based on experimental results.
  • Predetermined lower resin bed depth D2 750 mm
  • predetermined electrical conductivity K 1500 ⁇ S / cm
  • predetermined total hardness H 500 mg CaCO 3 / L
  • predetermined regeneration level R 120 g ⁇ NaCl / LR
  • raw water temperature T 18 ° C.
  • the predetermined regeneration linear velocity V1 is changed between 0.7 to 2 m / s of the proper range
  • the predetermined extrusion amount N is changed between 0.4 to 2.5 BV of the proper range
  • the leak hardness y was obtained from Equation 1.
  • the hardness removal capacity x was obtained by Equation 8.
  • the cation exchange resin is set to “IMAC HP1220Na” manufactured by Rohm and Haas. It has been confirmed that the result of each application example almost matches the actual measurement value using the water softening device 1. That is, the data shown in FIGS. 9 to 12 can be said to be experimental results.
  • similar to the allowable leak hardness Y is SP33 and SP34 shown in FIG.
  • the object of the present invention can be achieved. That is, it is possible to achieve high economic efficiency by securing treated water having a purity equal to or lower than the allowable leak hardness Y and securing the amount of water sampled equivalent to that of other water softening devices of the regeneration method.
  • the allowable leak hardness Y may be set to about 3 mgCaCO 3 / L depending on the use of the treated water such as a reverse osmosis membrane apparatus.
  • the present invention is applied to all the application examples shown in FIGS. Can achieve the purpose.
  • the conditions of parameters other than the predetermined regeneration linear velocity V10 and the predetermined extrusion amount N are set to the side where the hardness leak level is likely to increase. For this reason, if various conditions are set to the side where the hardness leak level is further reduced, a leak hardness y of 0.1 mgCaCO 3 / L or less can be easily achieved.
  • the allowable leak hardness Y is 1 mgCaCO 3.
  • Treated water having a purity of / L or less or a purity close to this purity can be easily produced.
  • the predetermined regeneration linear velocity V1 in the range of 0.7 to 2 m / s, it is possible to prevent regeneration failure due to drift of the regenerant and short path, and it is equivalent to a cocurrent regeneration type water softening device. Hardness removal capacity can be ensured. Further, by using the equations 1 to 4, it is possible to easily design the split flow regeneration process.
  • the water softening device 1 can be used by being connected to the boiler device 50 via a treated water tank 51 as necessary.
  • the boiler device 50 has different allowable leak hardness Y depending on its can structure. Therefore, it is desirable that the water softening device 1 is configured to change the predetermined extrusion amount N according to the allowable leak hardness Y.
  • the water softening device 1 can be used by being connected to a reverse osmosis membrane device 52 via a treated water tank 51 as necessary.
  • the predetermined extrusion amount N is obtained in advance, and the raw water extrusion mode is terminated by the timer function of the controller 1C.
  • an arbitrary parameter related to the predetermined extrusion amount N is detected, and the predetermined extrusion amount is detected.
  • N can be configured to adjust.
  • the fourth valve 27 can be controlled so that only the lower resin bed 5A is terminated before the raw water extrusion mode is terminated. In this case, the amount of contamination of the lower resin bed 5A due to the hardness component can be minimized.

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JP2012157790A (ja) * 2011-01-28 2012-08-23 Miura Co Ltd イオン交換装置
JP2012166132A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012166131A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012166134A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012183485A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183486A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183487A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183483A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183482A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2013027802A (ja) * 2011-07-27 2013-02-07 Miura Co Ltd 水処理システム
JP2013123679A (ja) * 2011-12-14 2013-06-24 Miura Co Ltd 硬水軟化装置の運転方法及び硬水軟化装置
WO2014155267A1 (en) * 2013-03-25 2014-10-02 Koninklijke Philips N.V. Method of controllable water softening and water softening system

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JPS6091246U (ja) * 1983-11-25 1985-06-22 三浦工業株式会社 塩水コントロ−ル装置
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JP2012143663A (ja) * 2011-01-06 2012-08-02 Miura Co Ltd イオン交換装置
JP2012157790A (ja) * 2011-01-28 2012-08-23 Miura Co Ltd イオン交換装置
JP2012166132A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012166131A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012166134A (ja) * 2011-02-10 2012-09-06 Miura Co Ltd イオン交換装置
JP2012183486A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183485A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183487A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183483A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2012183482A (ja) * 2011-03-04 2012-09-27 Miura Co Ltd 水処理方法及び水処理システム
JP2013027802A (ja) * 2011-07-27 2013-02-07 Miura Co Ltd 水処理システム
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JP2013123679A (ja) * 2011-12-14 2013-06-24 Miura Co Ltd 硬水軟化装置の運転方法及び硬水軟化装置
WO2014155267A1 (en) * 2013-03-25 2014-10-02 Koninklijke Philips N.V. Method of controllable water softening and water softening system

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