JP5051629B1 - Water treatment system - Google Patents

Abstract

Provided is a water treatment system capable of stably suppressing precipitation of calcium carbonate scale even when hard water having poor water quality is used while suppressing precipitation and fouling of silica scale. The water softening device (3) includes a cation exchange resin bed and a softening process for passing raw water in a downward flow through the cation exchange resin bed; A first regeneration process for regenerating the whole; and a valve means capable of switching to a second regeneration process for regenerating a part of the cation exchange resin bed by generating an upward flow for flowing the regeneration solution from the bottom to the middle. The membrane separation apparatus includes an RO membrane module (8), a pressurizing pump (6), an inverter (7) that outputs a driving frequency corresponding to the input current value signal to the pressurizing pump (6), and a transmission A control unit (10) that calculates a drive frequency using a physical quantity in the system so that the water W5 becomes a target flow rate value and outputs a current value signal corresponding to the drive frequency to the inverter (7) is provided.
[Selection] Figure 1

Description

  The present invention relates to a water treatment system including a water softening device and a reverse osmosis membrane separation device.

  In the semiconductor manufacturing process, the cleaning of electronic parts, the cleaning of medical equipment, etc., high-purity pure water containing no impurities is used. This type of pure water is generally produced by treating raw water such as ground water or tap water with a reverse osmosis membrane (hereinafter also referred to as “RO membrane”).

  When pure water is produced by the RO membrane, a phenomenon occurs in which the hardness component contained in the raw water is deposited as a scale on the surface of the RO membrane. In addition, a so-called fouling phenomenon occurs in which suspended substances (for example, insoluble colloidal iron) contained in the raw water are deposited on the surface and pores of the RO membrane. When scale deposition or fouling occurs in the RO membrane, the water permeability (water permeability coefficient) of the RO membrane decreases. As a result, the flow rate of the permeate is reduced.

  Therefore, a system for supplying soft water to the RO membrane has been proposed in order to suppress precipitation of calcium carbonate scale. This system softens raw water (hard water) by a water softening device using a cation exchange resin as a pretreatment of the RO device (see Patent Document 1).

  On the other hand, in the RO membrane in which no scale deposition or fouling occurs, the water permeation coefficient varies depending on the temperature of the supplied water (hereinafter also referred to as “supply water”). The RO membrane has a larger water permeability coefficient as the temperature of the feed water increases. For this reason, even if supply water is supplied with a fixed pressure with respect to RO membrane, the flow volume of permeate increases as temperature rises. When the flow rate of the permeated water increases, the concentration of soft water proceeds on the primary side of the RO membrane.

  In general, a hard water softening device cannot remove silica components and suspended substances contained in raw water. For this reason, when the soft water is concentrated on the primary side of the RO membrane, silica-based scale precipitation and fouling are likely to occur. That is, when soft water is supplied to the RO membrane, the precipitation of the silica-based scale and the occurrence of fouling cannot be suppressed depending on the temperature even if the precipitation of the calcium carbonate-based scale can be suppressed.

  Therefore, a system for performing flow rate feedback control has been proposed in order to keep the flow rate of the permeated water in the RO membrane constant regardless of the temperature of the supplied water. In this flow rate feedback control, the operation frequency of the pressurizing pump that sends the feed water to the RO membrane is controlled by an inverter so that the flow rate of the permeated water produced by the RO membrane becomes a target value (see Patent Document 2). .

JP 2010-82610 A JP 2005-296945 A

  However, in the conventional water softening device, it has been difficult to produce high-purity soft water in which the amount of hardness leak is sufficiently reduced by using hard water having poor water quality. Moreover, even if the conventional hard water softening device can produce high-purity soft water from hard water having poor water quality, it has been difficult to ensure a practical amount of water sampling. Accordingly, it has been difficult to stably suppress the precipitation of calcium carbonate scale in the RO membrane.

  Therefore, the present invention is a water treatment that can stably suppress precipitation of calcium carbonate scale even when hard water having poor water quality is used while suppressing the occurrence of silica scale precipitation and fouling in the RO membrane. The purpose is to provide a system.

  The present invention includes a hard water softening device for producing soft water from raw water, and a membrane separation device for producing permeated water from soft water, the hard water softening device comprising a cation exchange resin bed to which raw water or regenerated liquid is supplied, A softening process in which raw water is passed through the cation exchange resin bed in a downward flow to obtain soft water; the regenerated liquid is collected at the bottom while being distributed to the top of the cation exchange resin bed. A first regeneration process for regenerating the entire cation exchange resin bed by generating a downward flow of the cation exchange resin bed; and, after the first regeneration process, distributing the regeneration liquid to the bottom of the cation exchange resin bed, And a valve means switchable to a second regeneration process for regenerating a part of the cation exchange resin bed by generating an ascending flow of the regenerated liquid by collecting the liquid at Permeated water and concentrated water A reverse osmosis membrane module that is separated into a pressure pump that is driven at a rotational speed according to the input driving frequency, sucks soft water and discharges the soft water toward the reverse osmosis membrane module, and an input current value signal An inverter that outputs the corresponding drive frequency to the pressurization pump, and the drive frequency of the pressurization pump is calculated using a physical quantity in the system so that the flow rate of permeate becomes a preset target flow rate value, The present invention relates to a water treatment system including a control unit that outputs a current value signal corresponding to a calculated value of the drive frequency to the inverter.

  In addition, the membrane separation device includes a flow rate detection unit that detects a flow rate of permeated water, and the control unit drives the pressure pump so that a detected flow rate value of the flow rate detection unit becomes the target flow rate value. It is preferable to calculate the frequency.

  Further, the membrane separation device includes pressure detection means for detecting a discharge pressure of the pressure pump, and temperature detection means for detecting the temperature of soft water, permeated water or concentrated water, and the control unit (i ) Based on the detected temperature value of the temperature detecting means, the water permeation coefficient value at the reference temperature of the reverse osmosis membrane module, and the target flow rate value, the discharge pressure of the pressurizing pump is calculated, and (ii) the discharge pressure Is preferably set as a target pressure value, and (iii) the driving frequency of the pressurizing pump is calculated so that the detected pressure value of the pressure detecting means becomes the target pressure value.

  In addition, the membrane separation device includes temperature detection means for detecting the temperature of soft water, permeated water or concentrated water, and the control unit includes (i) a detected temperature value of the temperature detection means, and a reference for the reverse osmosis membrane module. The discharge pressure of the pressurizing pump is calculated based on the water permeability coefficient value at the temperature and the target flow rate value, and (ii) the drive frequency of the pressurizing pump is calculated based on the calculated value of the discharge pressure. It is preferable.

  In addition, the membrane separation device includes temperature detection means for detecting the temperature of soft water, permeated water or concentrated water, and a drain valve capable of adjusting a drain flow rate of the concentrated water discharged outside the device, and the control unit includes (I) calculating the allowable concentration ratio of silica in concentrated water based on the silica concentration determined from the silica concentration of raw water or soft water obtained in advance and the detected temperature value of the temperature detecting means; Calculating the drainage flow rate from the calculation value of the concentration rate and the target flow rate value of the permeated water, and (iii) controlling the drainage valve so that the actual drainage flow rate of the concentrated water becomes the calculated value of the drainage flow rate. preferable.

  The membrane separation device includes a hardness measuring means for measuring the calcium hardness of the soft water, and a drain valve capable of adjusting a drain flow rate of the concentrated water discharged to the outside of the device. Based on the obtained calcium carbonate solubility and the measured hardness value of the hardness measuring means, an allowable concentration rate of calcium carbonate in concentrated water is calculated, and (ii) the calculated value of the allowable concentration rate and the target of permeated water It is preferable to calculate the drainage flow rate from the flow rate value, and (iii) control the drainage valve so that the actual drainage flow rate of the concentrated water becomes the calculated value of the drainage flow rate.

  Further, the membrane separation device includes an electrical conductivity measuring means for measuring the electrical conductivity of the permeated water, and a drain valve capable of adjusting a drain flow rate of the concentrated water discharged outside the device, and the control unit includes: It is preferable to control the flow rate of drainage from the drainage valve so that the measured electrical conductivity value of the electrical conductivity measuring means becomes a preset target electrical conductivity value.

  ADVANTAGE OF THE INVENTION According to this invention, the water treatment which can suppress stably precipitation of a calcium carbonate type scale also in the case of using the hard water of inferior water quality, suppressing generation | occurrence | production of the silica type scale in a RO membrane, and fouling. A system can be provided.

1 is an overall configuration diagram of a water treatment system 1 according to a first embodiment. It is a schematic sectional drawing of the water softening apparatus 3. 4 is a flowchart of a process executed by the control unit 10. (A)-(c) is explanatory drawing which shows the basic process performed by the control part 10. FIG. It is a flowchart which shows the process sequence in case the control part 10 of 1st Embodiment performs flow volume feedback water volume control. It is a flowchart which shows the process sequence in case the control part 10 of 2nd Embodiment performs temperature feedforward collection | recovery rate control. It is a whole block diagram of the water treatment system 1A which concerns on 2nd Embodiment. It is a flowchart which shows the process sequence in case the control part 10A of 2nd Embodiment performs pressure feedback water volume control. It is a flowchart which shows the process sequence in case the control part 10A of 2nd Embodiment performs water quality feedforward collection | recovery rate control. It is a whole block diagram of the water treatment system 1B which concerns on 3rd Embodiment. It is a flowchart which shows the process sequence in case the control part 10B of 3rd Embodiment performs temperature feedforward water quantity control. It is a flowchart which shows the process sequence in case the control part 10B of 3rd Embodiment performs water quality feedback collection | recovery rate control.

(First embodiment)
A water treatment system 1 according to a first embodiment of the present invention will be described with reference to the drawings. The water treatment system 1 is applied to, for example, a pure water production system that produces pure water from fresh water. FIG. 1 is an overall configuration diagram of a water treatment system 1 according to the first embodiment. FIG. 2 is a schematic cross-sectional view of the water softening device 3. FIG. 3 is a flowchart of a process executed by the control unit 10. 4A to 4C are explanatory diagrams illustrating a basic process executed by the control unit 10.

  As shown in FIG. 1, the water treatment system 1 which concerns on 1st Embodiment is provided with the raw | natural water pump 2, the hard water softening apparatus 3, the salt water tank 4, and the temperature sensor 5 as a temperature detection means. The water treatment system 1 includes a pressurizing pump 6, an inverter 7, an RO membrane module 8 as a reverse osmosis membrane module, a flow rate sensor 9 as a flow rate detection means, a control unit 10, and a first drain valve 11. To a third drain valve 13. Among these, the pressurizing pump 6, the RO membrane module 8, the flow sensor 9 and the control unit 10 constitute a membrane separation device in the present embodiment. Moreover, in FIG. 1, the path | route of an electrical connection is shown with a broken line.

  Moreover, the water treatment system 1 is provided with the raw | natural water line L1, the soft water line L2, the salt water line L3, and the drainage line L4. Furthermore, the water treatment system 1 includes a permeate water line L5 and a concentrated water line L6. The “line” in the present specification is a general term for lines capable of flowing a fluid such as a flow path, a radial path, and a pipeline.

  The upstream end of the raw water line L1 is connected to a supply source (not shown) of the raw water W1. On the other hand, the downstream end of the raw water line L <b> 1 is connected to the process control valve 32 of the hard water softening device 3.

  The raw water pump 2 is provided in the raw water line L1. The raw water pump 2 pumps raw water W1 such as tap water and groundwater supplied from a supply source toward the hard water softening device 3. The operation (drive and stop) of the raw water pump 2 is electrically connected to the control unit 10. The raw water pump 2 is controlled by the control unit 10.

In the softening process ST1, the raw water line L1 and the raw water pump 2 supply the raw water W1 having an electric conductivity of 150 mS / m or less and a total hardness of 500 mgCaCO ₃ / L or less to the hard water softening device 3.

  The hard water softening device 3 is equipment for producing soft water W2 by replacing hardness components (calcium ions and magnesium ions) contained in the raw water W1 with sodium ions (or potassium ions) in the cation exchange resin bed 311. As shown in FIG. 2, the water softening device 3 mainly includes a pressure tank 31 and a process control valve 32 as a valve means.

  The pressure tank 31 is a bottomed cylindrical body having an opening at the top. The opening of the pressure tank 31 is sealed with a lid member. Inside the pressure tank 31, a cation exchange resin bed 311 made of cation exchange resin beads and a support bed 312 made of filtered gravel are accommodated.

  The cation exchange resin bed 311 functions as a treatment material that softens the raw water W1. The cation exchange resin bed 311 is stacked on the support bed 312 inside the pressure tank 31. The depth D1 of the cation exchange resin bed 311 is set in the range of 300 to 1500 mm.

The support bed 312 functions as a fluid rectifying member for the cation exchange resin bed 311. The support floor 312 is accommodated on the bottom side of the pressure tank 31.
In the pressure tank 31, a top screen 321 for preventing the cation exchange resin beads from flowing out is provided on the top of the cation exchange resin bed 311. The top screen 321 is connected to various lines constituting the process control valve 32 via a first flow path (not shown).

  The liquid distribution position and the liquid collection position by the top screen 321 are set near the top of the cation exchange resin bed 311. The top screen 321 functions as a top liquid distribution unit and a top liquid collection unit provided at the top of the cation exchange resin bed 311.

  In the pressure tank 31, a bottom screen 322 for preventing the cation exchange resin beads from flowing out is provided at the bottom of the cation exchange resin bed 311. The bottom screen 322 is connected to various lines constituting the process control valve 32 through a second flow path (not shown).

  The liquid distribution position and the liquid collection position by the bottom screen 322 are set near the bottom of the cation exchange resin bed 311. The bottom screen 322 functions as a bottom liquid distribution unit and a bottom liquid collection unit provided at the bottom of the cation exchange resin bed 311.

  In the pressure tank 31, an intermediate screen 323 that prevents the cation exchange resin beads from flowing out is located above the hardness leak prevention region 313 (described later) and in the intermediate portion in the depth direction of the cation exchange resin bed 311. Is provided. The intermediate screen 323 is connected to various lines constituting the process control valve 32 via a third flow path (not shown).

  The liquid collection position by the intermediate screen 323 is set near the intermediate part of the cation exchange resin bed 311. The intermediate part screen 323 functions as an intermediate part liquid collection part provided in the intermediate part of the cation exchange resin bed 311.

  The process control valve 32 includes various lines and valves therein. The process control valve 32 is configured to be able to switch at least the flow of the raw water W1 in the softening process ST1, the flow of the salt water W3 in the first regeneration process ST3, and the flow of the salt water W3 in the second regeneration process ST5. In the softening process ST1, the raw water W1 is passed through the cation exchange resin bed 311 in a downward flow to produce the soft water W2. On the other hand, in the first regeneration process ST3, while the salt water W3 is distributed to the top of the cation exchange resin bed 311, the downward flow of the salt water W3 is generated by collecting at the bottom, so that the cation exchange resin bed 311 Play the whole thing. In the second regeneration process ST5, while the salt water W3 is distributed to the bottom of the cation exchange resin bed 311, the upward flow of the salt water W3 is generated by collecting the salt water W3 at the middle portion, and one of the cation exchange resin beds 311 is collected. Play a part.

  The regeneration process in the present embodiment includes a first regeneration process ST3 and a second regeneration process ST5 performed after the end of the first regeneration process ST3. The first regeneration process ST3 is a cocurrent regeneration process in which the entire cation exchange resin bed 311 is regenerated. The second regeneration process ST5 is a partial countercurrent regeneration process in which a part of the cation exchange resin bed 311 is regenerated. The regeneration of the cation exchange resin bed 311 in this embodiment is operated by a two-stage regeneration process. Specifically, the operation is performed by executing the cocurrent regeneration process as the first regeneration process, and executing the partial countercurrent regeneration process as the second regeneration process after the completion of the first regeneration process.

  In the second regeneration process ST5, the salt water W3 is supplied to the hardness leak prevention region 313 in such an amount that the regeneration level is 1 to 6 eq / LR. Here, the regeneration level refers to the amount of the regenerant used for regenerating the unit volume ion exchange resin. When sodium chloride is used as the regenerant, 1 eq corresponds to 58.5 g.

The hardness leak prevention region 313 is a region that needs to be sufficiently regenerated in the cation exchange resin bed 311 in order to prevent hardness leak in the softening process ST1 as much as possible. As shown in FIG. 2, the hardness leak prevention region 313 has a depth D2 of 100 mm based on the bottom (that is, the bottom) of the cation exchange resin bed 311. In the second regeneration process ST5, the hardness leak amount can be maintained at 0.8 mgCaCO ₃ / L or less by reproducing the limited region at a regeneration level of 1 to 6 eq / LR.

  Further, the process control valve 32 has a flow of the raw water W1 in the first extrusion process ST4 executed after the first regeneration process ST3 and a flow of the raw water W1 in the second extrusion process ST6 executed after the second regeneration process ST5. And can be switched. In the first extrusion process ST4, while the raw water W1 is distributed to the top of the cation exchange resin bed 311, a downward flow of the raw water W1 is generated by collecting at the bottom, and the introduced salt water W3 is pushed out. In the second extrusion process ST6, while the raw water W1 is distributed to the bottom of the cation exchange resin bed 311, the upward flow of the raw water W1 is generated by collecting at the middle portion, and the introduced salt water W3 is pushed out.

  The process control valve 32 is connected to the upstream end of the drain line L4. From the drainage line L4, salt water W3 and raw water W1 used in the regeneration process, extrusion process, and the like are discharged as drainage W4.

  Furthermore, in the process control valve 32, the valve body drive section provided therein is electrically connected to the control section 10 via a signal line. Switching of the valve in the process control valve 32 is controlled by the control unit 10.

Here, each process implemented in the water softening apparatus 3 is demonstrated.
In the water treatment system 1 of the present embodiment, the control unit 10 to be described later performs the following processes ST1 to ST8 shown in FIG. 3 by switching the flow path of the process control valve 32.

(ST1) Softening process of passing raw water W1 from the top to the bottom with respect to the entire cation exchange resin bed 311 (ST2) Raw water W1 as washing water from the bottom to the top with respect to the entire cation exchange resin bed 311 First washing process (ST4) for passing salt water W3 as a regenerated liquid from the top to the bottom with respect to the entire cation exchange resin bed 311. Cation exchange resin for raw water W1 as extrusion water. The first extrusion process (ST5) for allowing the entire bed 311 to pass from the top to the bottom Salt water W3 as a regenerated liquid is passed from the bottom to the top of the cation exchange resin bed 311 mainly to the hardness leak prevention region 313. Second regeneration process (ST6) A second push for passing raw water W1 as extrusion water from the bottom to the top with respect to the hardness leak prevention region 313 of the cation exchange resin bed 311 mainly. Process (ST7) rinsing process (ST8) to pass from top to bottom for the entire cation exchange resin bed 311 raw water W1 as rinse water refill process for supplying raw water W1 as makeup water to the brine tank 4

  Next, an operation method of the softening process ST1, the first regeneration process ST3, and the second regeneration process ST5 which are main processes among the processes ST1 to ST8 will be described.

In the softening process ST1, as shown in FIG. 4A, the raw water W1 is distributed from the top screen 321, and the raw water W1 is allowed to pass through the entire cation exchange resin bed 311 in a downward flow. Manufacturing. The produced soft water W2 is collected from the bottom screen 322. In the softening process ST1 after the second regeneration process ST5, raw water W1 having an electric conductivity of 150 mS / m or less and a total hardness of 500 mgCaCO ₃ / L or less is supplied.

  In the first regeneration process ST3, as shown in FIG. 4 (b), salt water W3 is distributed from the top screen 321, and the salt water W3 is passed through the entire cation exchange resin bed 311 in a downward flow. The cation exchange resin bed 311 is regenerated. In the first regeneration process ST3, the salt water W3 is passed through the cation exchange resin bed 311 at a linear velocity of 0.7 to 2 m / h. The used salt water W3 obtained by regenerating the cation exchange resin bed 311 is collected from the bottom screen 322. In the first regeneration process ST3, the entire cation exchange resin bed 311 is regenerated by cocurrent regeneration.

  In 1st extrusion process ST4 implemented after completion | finish of 1st reproduction | regeneration process ST3, as shown in FIG.4 (b), raw water W1 is distributed from the top screen 321, and with respect to the whole cation exchange resin bed 311. Then, the raw water W1 is passed in a downward flow, and the salt water W3 introduced into the cation exchange resin bed 311 is pushed out. The raw water W1 that has passed through the cation exchange resin bed 311 is collected from the bottom screen 322. In the first extrusion process ST4, the raw water W1 is passed through the cation exchange resin bed 311 at a linear velocity of 0.7 to 2 m / h and an extrusion rate of 0.4 to 2.5 BV.

  In the first regeneration process ST3 and the first extrusion process ST4, cocurrent regeneration is performed on the entire cation exchange resin bed 311. Therefore, the entire amount of the cation exchange resin bed 311 is regenerated almost uniformly, so that in the softening process ST1, the sampled amount of the soft water W2 is increased to the maximum.

  In the second regeneration process ST5, as shown in FIG. 4 (c), the salt water W3 is distributed from the bottom screen 322, and the salt water W3 is passed through the cation exchange resin bed 311 in an upward flow to cause a hardness leak. The lower region of the cation exchange resin bed 311 including the prevention region 313 is regenerated. In the second regeneration process ST5, the salt water W3 is passed through the cation exchange resin bed 311 at a linear velocity of 0.7 to 2 m / h. The salt water W3 regenerated in the lower region of the cation exchange resin bed 311 is collected from the intermediate screen 323. In the second regeneration process ST5, the salt water W3 is supplied to the hardness leak prevention region 313 in such an amount that the regeneration level is 1 to 6 eq / LR. In the second regeneration process ST5, the lower region of the cation exchange resin bed 311 including the hardness leak prevention region 313 is mainly regenerated by partial countercurrent regeneration.

By performing this second regeneration process ST5, in the subsequent softening process ST1, when raw water W1 having an electric conductivity of 150 mS / m or less and a total hardness of 500 mg CaCO ₃ / L or less is supplied, the hardness leak amount is High-purity soft water W2 having a concentration of 0.8 mgCaCO ₃ / L or less can be produced.

  In the second extrusion process ST6 performed after the end of the second regeneration process ST5, as shown in FIG. 4 (c), the raw water W1 is distributed from the bottom screen 322, mainly to the hardness leak prevention region 313, The raw water W1 is passed in an upward flow to push out the salt water W3 introduced into the lower region of the cation exchange resin bed 311. The raw water W <b> 1 that has passed through the hardness leak prevention region 313 is collected from the intermediate screen 323. In the second extrusion process ST6, the raw water W1 is passed through the lower region of the cation exchange resin bed 311 at a linear velocity of 0.7 to 2 m / h and an extrusion rate of 0.4 to 2.5 BV.

In the second regeneration process ST5 and the second extrusion process ST6, partial countercurrent regeneration is performed on the lower region of the cation exchange resin bed 311. Therefore, the hardness leak prevention region 313 is regenerated intensively, so that the hardness leak amount of the soft water W2 is suppressed to the limit in the softening process ST1.
Note that the illustration of the back cleaning process ST2, the rinsing process ST7, and the water replenishment process ST8 is omitted.

Again, the structure of the water treatment system 1 is demonstrated, referring FIG.
The salt water tank 4 stores salt water W3 for regenerating the cation exchange resin bed 311. The upstream end of the salt water line L3 is connected to the salt water tank 4. The downstream end of the salt water line L3 communicates with the process control valve 32 and is connected to various lines constituting the process control valve 32, respectively.

  The salt water line L3 is provided with a salt water valve (not shown). The salt water valve opens and closes the salt water line L3. The salt water valve is incorporated in the process control valve 32. In the salt water valve, the drive unit of the valve body is electrically connected to the control unit 10 via a signal line (not shown). The opening and closing of the salt water valve is controlled by the control unit 10. The salt water tank 4 sends salt water W3 for regenerating the cation exchange resin bed 311 to the pressure tank 31 in the first regeneration process ST3.

  The temperature sensor 5 is a device that detects the temperature of the soft water W2 flowing through the soft water line L2. The temperature sensor 5 is connected to the soft water line L2 at the connection portion J1. The temperature sensor 5 is electrically connected to the control unit 10. The temperature of the soft water W2 detected by the temperature sensor 5 (hereinafter also referred to as “detected temperature value”) is transmitted to the control unit 10 as a detection signal.

  The pressurizing pump 6 is a device that sucks the soft water W <b> 2 delivered from the hard water softening device 3 and discharges it toward the RO membrane module 8. The pressure pump 6 is electrically connected to an inverter 7 (described later). Driving power whose frequency is converted is supplied from the inverter 7 to the pressurizing pump 6. The pressurizing pump 6 is driven at a rotational speed corresponding to the input driving frequency.

  The inverter 7 is an electric circuit that supplies driving power whose frequency is converted to the pressurizing pump 6. The inverter 7 is electrically connected to the control unit 10. The inverter 7 receives a current value signal from the control unit 10. The inverter 7 outputs a driving frequency corresponding to the input current value signal to the pressurizing pump 6.

  The RO membrane module 8 is a facility for subjecting the soft water W2 produced by the hard water softening device 3 to membrane separation treatment into permeated water W5 from which dissolved salts have been removed and concentrated water W6 from which dissolved salts have been concentrated. The RO membrane module 8 includes a single or a plurality of RO membrane elements (not shown). The RO membrane module 8 membrane-separates the soft water W2 with these RO membrane elements to produce permeated water W5 and concentrated water W6. The primary side inlet port of the RO membrane module 8 is connected to the downstream side of the water softening device 3 (process control valve 32) via the soft water line L2.

  An upstream end of the permeate line L5 is connected to the secondary port of the RO membrane module 8. The permeated water W5 obtained by the RO membrane module 8 is sent to a demand location or the like via the permeated water line L5. The upstream end of the concentrated water line L6 is connected to the primary outlet port of the RO membrane module 8. The concentrated water W6 obtained by the RO membrane module 8 is discharged out of the RO membrane module 8 through the concentrated water line L6. A first drain valve 11, a second drain valve 12, and a third drain valve 13 (described later) are connected to the downstream side of the concentrated water line L6.

  A part of the concentrated water W6 discharged from the concentrated water line L6 may be returned to the soft water line L2 on the upstream side of the pressurizing pump 6. By returning a part of the concentrated water W6 to the soft water line L2, the water flow rate on the surface of the RO membrane module 8 can be maintained within a predetermined range.

The RO membrane module 8 in the present embodiment has a reverse osmosis membrane (not shown) in which a negatively charged skin layer made of a crosslinked wholly aromatic polyamide is formed on the membrane surface. The reverse osmosis membrane, concentration 500 mg / L, pH 7.0, sodium chloride aqueous solution temperature 25 ° C., the operating pressure 0.7 MPa, the water permeability coefficient when supplied at a recovery rate of 15%, 1.5 × 10 ^{- 11} m ³ · m ⁻² · s ⁻¹ · Pa ⁻¹ or more and a salt removal rate of 99% or more.

In the reverse osmosis membrane set to such a performance, in the desalination treatment of fresh water, the lower the hardness of the feed water, the lower the salt removal rate (ie, (feed water EC− Permeated water EC) / feed water EC × 100) has a characteristic of increasing. Therefore, constantly supplying high-purity soft water W2 (actual value: 0.8 mgCaCO ₃ or less) produced by the water softening device 3 that performs a two-stage regeneration process consisting of cocurrent regeneration and partial countercurrent regeneration. Thus, a high salt removal rate (usually 98.5% or more) can be maintained.

The operating pressure is an average operating pressure defined by JIS K3802-1995 “Membrane Term”. The operating pressure refers to an average value of the inlet pressure on the primary side and the outlet pressure on the primary side of the RO membrane module 8. Recovery and the feed water to the RO membrane module 8 (where the aqueous sodium chloride solution), the amount of the flow rate _{Q p} permeate to the flow rate _{Q f (i.e., Q p / Q f × 100} ) refers to.

The water permeation coefficient is a value obtained by dividing the flow rate [m ³ / s] of the permeated water by the membrane area [m ² ] and the effective pressure [Pa] (see formula (3) described later). The water permeability coefficient is an index indicating the water permeation performance of the reverse osmosis membrane. That is, the water permeation coefficient means the amount of water that permeates the unit area of the membrane per unit time when a unit effective pressure is applied. The effective pressure is defined in JIS K3802-1995 “Membrane terminology”. The effective pressure is a pressure obtained by subtracting the osmotic pressure difference and the secondary pressure (back pressure) from the operating pressure (average operating pressure) (see formula (4) described later).

The salt removal rate is a value calculated from the concentration of a specific salt (here, sodium chloride concentration) before and after permeating the membrane. The salt removal rate is an index indicating the solute blocking performance of the reverse osmosis membrane. The salt removal rate is determined by (1−C _p / C _f ) × 100 from the inlet concentration C _f to the RO membrane module 8 and the permeated water concentration C _p .

  The reverse osmosis membrane that satisfies the conditions of the water permeability coefficient and the salt removal rate of this embodiment is commercially available as a reverse osmosis membrane element. As the reverse osmosis membrane element, for example, Toray Industries, Inc .: model name “TMG20-400”, Unjin Chemical, Inc .: model name “RE8040-BLF”, Nitto Denko Corporation: model name “ESPA1”, etc. may be used. it can.

  The flow rate sensor 9 is a device that detects the flow rate of the permeated water W5 flowing through the permeated water line L5. The flow sensor 9 is connected to the permeated water line L5 at the connection portion J2. The flow sensor 9 is electrically connected to the control unit 10. The flow rate of the permeated water W5 detected by the flow rate sensor 9 (hereinafter also referred to as “detected flow rate value”) is transmitted to the control unit 10 as a detection signal.

  The first drain valve 11 to the third drain valve 13 are valves that adjust the drainage flow rate of the concentrated water W6 discharged from the concentrated water line L6. The downstream side of the concentrated water line L6 described above branches into the first drainage line L11, the second drainage line L12, and the third drainage line L13 at the branch portions J3 and J4.

  A first drain valve 11 is provided in the first drain line L11. A second drain valve 12 is provided in the second drain line L12. A third drain valve 13 is provided in the third drain line L13.

  The first drain valve 11 can open and close the first drain line L11. The second drain valve 12 can open and close the second drain line L12. The third drain valve 13 can open and close the third drain line L13.

  Each of the first drain valve 11 to the third drain valve 13 includes a constant flow valve mechanism (not shown). The constant flow valve mechanisms are set to different flow values in the first drain valve 11 to the third drain valve 13. For example, the drainage flow rate of the first drain valve 11 is set so that the recovery rate of the RO membrane module 8 is 95% in the open state. The drainage flow rate of the second drainage valve 12 is set so that the recovery rate of the RO membrane module 8 is 90% in the open state. The drainage flow rate of the third drainage valve 13 is set so that the recovery rate of the RO membrane module 8 is 80% in the open state.

  The drainage flow rate of the concentrated water W6 discharged from the concentrated water line L6 can be adjusted stepwise by selectively opening and closing the first drainage valve 11 to the third drainage valve 13. For example, only the second drain valve 12 is opened, and the first drain valve 11 and the third drain valve 13 are closed. In this case, the recovery rate of the RO membrane module 8 can be 90%. Further, the first drain valve 11 and the second drain valve 12 are opened, and only the third drain valve 13 is closed. In this case, the recovery rate of the RO membrane module 8 can be 85%. Therefore, in this embodiment, the drainage flow rate of the concentrated water W6 is 5% between the recovery rate of 65% and 95% by selectively opening and closing the first drainage valve 11 to the third drainage valve 13. It can be adjusted step by step.

  The first drain valve 11 to the third drain valve 13 are each electrically connected to the control unit 10. The opening and closing of the valve body in the first drain valve 11 to the third drain valve 13 is controlled by a drive signal from the control unit 10.

  The control unit 10 includes a microprocessor (not shown) including a CPU and a memory. The control unit 10 controls the operation of the process control valve 32 based on a detection signal or the like input from a soft water flow sensor (not shown) or a salt water flow sensor. The memory of the control unit 10 stores in advance a control program for operating the water softening device 3 in the first embodiment. The CPU of the control unit 10 controls the process control valve 32 so as to sequentially switch the softening process ST1 to the water replenishment process ST6 described above according to the control program stored in the memory.

  Moreover, the control part 10 calculates the drive frequency of the pressurization pump 6 by using the detected flow rate value of the permeated water W5 as a feedback value so that the flow rate of the permeated water W5 becomes a preset target flow rate value. Then, the control unit 10 outputs a current value signal corresponding to the calculated drive frequency value to the inverter 7 (hereinafter, also referred to as “flow rate feedback water amount control”). This flow rate feedback control is a control mode executed when the flow rate of the permeated water W5 is normally detected by the flow rate sensor 9.

  Here, the flow rate feedback water amount control by the control unit 10 will be described. FIG. 5 is a flowchart showing a processing procedure when the control unit 10 executes the flow rate feedback water amount control. The process of the flowchart shown in FIG. 5 is repeatedly executed during operation of the water treatment system 1.

In step ST101 shown in FIG. 5, the control unit 10 acquires the target flow rate value Q _p ′ of the permeated water W5. This target flow rate value Q _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

  In step ST102, the control unit 10 determines whether or not the time t measured by an internal timer (not shown) has reached 100 ms which is a control cycle. In step ST102, when the control unit 10 determines that the time measured by the timer has reached 100 ms (YES), the process proceeds to step ST103. In step ST102, when the control unit 10 determines that the time measured by the timer has not reached 100 ms (NO), the process returns to step ST102.

Step ST 103: In (step ST 102 YES judgment), the control unit 10 acquires the detected flow rate value _{Q p} of the permeate water W5 detected by flow sensor 9.
In step ST 104, the control unit 10, so that the deviation between the detected flow rate value obtained in step ST 103 (feedback value) _{Q p} and the target flow rate value _{Q p} obtained in step ST 101 'is zero, velocity type digital PID algorithm To calculate the operation amount U. In the velocity type digital PID algorithm, the change amount of the operation amount is calculated every control cycle (100 ms), and this operation amount is determined by adding this to the previous operation amount.

In step ST105, the control unit 10, the operation amount U, based on the target flow rate value _{Q p} 'and the maximum driving frequency of the pressure pump 6 (the set value of 50Hz or 60 Hz), calculates a drive frequency F of the pressure pump 6 To do.
In step ST106, the control unit 10 converts the calculated value of the drive frequency F into a corresponding current value signal (4 to 20 mA).

  In step ST107, the control unit 10 outputs the converted current value signal to the inverter 7. Thereby, the process of this flowchart is complete | finished (it returns to step ST101).

  Further, the control unit 10 performs recovery rate control of the permeated water W5 based on the temperature of the soft water W2 (hereinafter also referred to as “temperature feedforward recovery rate control”). This temperature feedforward recovery rate control is executed in parallel with the above-described flow rate feedback water amount control.

  Next, temperature feedforward recovery rate control by the control unit 10 will be described. FIG. 6 is a flowchart showing a processing procedure when the control unit 10 executes the temperature feedforward recovery rate control. The process of the flowchart shown in FIG. 6 is repeatedly executed during operation of the water treatment system 1.

In step ST201 shown in FIG. 6, the control unit 10 acquires the target flow rate value Q _p ′ of the permeated water W5. This target flow rate value Q _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

In step ST 202, the control unit 10 acquires a silica (SiO ₂₎ concentration _{C s} of the soft water W2. This silica concentration C _s is a set value input to the memory by the system administrator via a user interface (not shown), for example. The silica concentration of the soft water W2 can be obtained by analyzing the water quality of the soft water W2 in advance. In the soft water line L2, the silica concentration of the soft water W2 may be measured by a sensor (not shown).

In step ST203, the control unit 10 acquires the detected temperature value T of the soft water W2 from the temperature sensor 5.
In step ST 204, the control unit 10 based on the detected temperature value T obtained, to determine the silica solubility _{S s} for water.

In step ST205, the control unit 10 calculates the allowable concentration magnification N _s of silica in the concentrated water W6 based on the silica concentration C _s acquired or determined in the previous step and the silica solubility S _s . Permissible concentration rate N _s of silica can be determined from the following equation (1).
N _s = S _s / C _s (1)
For example, if the silica concentration C _s is 20 mg SiO ₂ / L and the silica solubility S _{s at} 25 ° C. is 100 mg SiO ₂ / L, the allowable concentration ratio N _s is “5”.

In step ST 206, the control unit 10, prior to the target flow rate value Q _p acquired or calculated in step _', and based on the allowable concentration rate N _s, wastewater flow rate recovery is maximized (target drainage flow Q _d') Is calculated. The target drainage flow rate Q _d ′ can be obtained by the following equation (2).
Q _d ′ = Q _p ′ / (N _s −1) (2)

In step ST207, the control unit 10, the actual drainage flow _{Q d} is such that the target drainage flow _{Q d} 'calculated in step ST 206, controls the opening and closing of the first drain valve 11 to the third drain valve 13 of the concentrated water W6 To do. Thereby, the process of this flowchart is complete | finished (it returns to step ST201).

  According to the water treatment system 1 which concerns on 1st Embodiment mentioned above, the following effects are acquired, for example.

In the water treatment system 1 according to the first embodiment, the cation exchange resin bed 311 of the water softening device 3 is operated including the first regeneration process ST3 and the second regeneration process ST5.
In the first regeneration process ST3, as shown in FIG. 4B, the salt water W3 is distributed to the top screen 321 of the cation exchange resin bed 311 and collected at the bottom screen 322. As a result, a downward flow of the salt water W3 is generated, and the entire cation exchange resin bed 311 is regenerated.

  In the second regeneration process ST5, after the first regeneration process ST3, as shown in FIG. 4C, the salt water W3 is distributed to the bottom screen 322 of the cation exchange resin bed 311 and collected at the intermediate screen 323. Is done. As a result, an upward flow of the salt water W3 is generated, and a part of the cation exchange resin bed 311 (mainly the hardness leak prevention region 313) is regenerated. Therefore, high-purity soft water W2 having a sufficiently reduced hardness leak amount can be obtained to the maximum within a practical water sampling range.

  In the water treatment system 1 according to the first embodiment, in the second regeneration process ST5, a hardness leak prevention region in which the depth D2 (see FIG. 2) is set to 100 mm with the bottom of the cation exchange resin bed 311 as a base. An amount of salt water W3 with a regeneration level of 1 to 6 eq / LR is supplied to 313. Therefore, in the cation exchange resin bed 311, the hardness leak prevention region 313, which is an exit region important for preventing hardness leak, can be almost completely regenerated. According to this, in the softening process ST1, even when hard water of poor water quality having a high hardness level is used as the raw water W1, it is possible to obtain high-purity soft water W2 in which the amount of hardness leak is suppressed to the limit.

  Therefore, according to the water treatment system 1 according to the first embodiment, high-purity soft water W2 can be constantly supplied to the RO membrane module 8. For this reason, in the water treatment system 1, precipitation of a silica-type scale and generation | occurrence | production of fouling in the RO membrane module 8 can be suppressed. Moreover, in the water treatment system 1, precipitation of calcium carbonate scale can be stably suppressed even when poor water quality hard water is used.

  Moreover, in the water treatment system 1 which concerns on 1st Embodiment, the control part 10 performs temperature feedforward collection | recovery rate control in parallel with flow volume feedback water amount control. For this reason, in the water treatment system 1, precipitation of the silica scale in the RO membrane module 8 can be more reliably suppressed while maximizing the recovery rate of the permeated water W5.

(Second Embodiment)
Next, a water treatment system 1A according to a second embodiment of the present invention will be described with reference to FIG. FIG. 7 is an overall configuration diagram of a water treatment system 1A according to the second embodiment. In the second embodiment, differences from the first embodiment will be mainly described. In the second embodiment, the same or equivalent components as those in the first embodiment will be described with the same reference numerals. In the second embodiment, the description overlapping with the first embodiment is omitted as appropriate.

  As shown in FIG. 7, the water treatment system 1A according to the second embodiment includes a raw water pump 2, a hard water softening device 3, a salt water tank 4, a temperature sensor 5, a pressure pump 6, an inverter 7, RO membrane module 8. Further, the water treatment system 1A includes a control unit 10A, a first drain valve 11 to a third drain valve 13, a hardness sensor 14 as hardness measuring means, and a pressure sensor 15 as pressure detecting means.

  The hardness sensor 14 is a device that measures the calcium hardness (hardness leak amount: calcium carbonate equivalent value) of the soft water W2 flowing through the soft water line L2. The hardness sensor 14 is connected to the soft water line L2 at the connection portion J2. The hardness sensor 14 is electrically connected to the control unit 10A. The calcium hardness (hereinafter also referred to as “measured hardness value”) of the soft water W2 measured by the hardness sensor 14 is transmitted to the control unit 10A as a detection signal.

  The pressure sensor 15 is a device that detects the discharge pressure (operating pressure) of the pressure pump 6. The pressure sensor 15 is connected to the soft water line L2 at a connection portion J5 provided in the vicinity of the discharge side of the pressure pump 6. In the present embodiment, the pressure of the soft water W <b> 2 immediately after being discharged from the pressurizing pump 6 is set as the discharge pressure of the pressurizing pump 6. The pressure sensor 15 is electrically connected to the control unit 10A. The pressure of the soft water W2 detected by the pressure sensor 15 (hereinafter also referred to as “detected pressure value”) is transmitted as a detection signal to the control unit 10A.

  The control unit 10A is configured by a microprocessor (not shown) including a CPU and a memory. 10 A of control parts control the operation | movement of the process control valve 32 (refer FIG. 2) based on the detection signal etc. which were input from the soft water flow sensor not shown and the salt water flow sensor. In the memory of the control unit 10A, a control program for performing the operation of the water softening device 3 in the second embodiment is stored in advance. The CPU controls the process control valve 32 so as to sequentially switch the softening process ST1 to the water replenishment process ST8 according to the control program stored in the memory (see FIG. 3).

  Further, the control unit 10A calculates the driving frequency of the pressurizing pump 6 using the detected pressure value of the pressurizing pump 6 as a feedback value so that the flow rate of the permeated water W5 becomes a preset target flow rate value. Then, the control unit 10A outputs a current value signal corresponding to the calculated drive frequency value to the inverter 7 (hereinafter also referred to as “pressure feedback water amount control”).

  Here, the pressure feedback water amount control by the control unit 10A will be described. FIG. 8 is a flowchart showing a processing procedure when the control unit 10A executes the pressure feedback water amount control. The process of the flowchart shown in FIG. 8 is repeatedly executed during operation of the water treatment system 1.

In step ST301 shown in FIG. 8, the control unit 10A acquires the target flow rate value Q _p ′ of the permeated water W5. This target flow rate value Q _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

In step ST302, the control unit 10A acquires the water permeability coefficient L _p at the reference temperature (25 ° C.) of the RO membrane module 8. This water permeability coefficient L _p is, for example, a set value input to the memory by a system administrator via a user interface (not shown).

This pressure feedback water volume control can be executed as a backup of the flow rate feedback water volume control in the first embodiment. In that case, the water permeability coefficient L _p may be a calculated value immediately before the failure of the flow sensor 9 (see FIG. 1) occurs.

The calculated value of the water permeability coefficient L _{p at} the reference temperature can be obtained based on the following formulas (3) and (4).
L _p = Q _p / (K · A · P _e ) (3)
(K: temperature correction coefficient, A: membrane area of RO membrane module 8, P _e : effective pressure)
_{P e = P d - (ΔP} 1/2) -P 2 -Δπ + P s (4)
(However, P _d : discharge pressure of the pressure pump 6, ΔP ₁ : differential pressure on the primary side of the RO membrane module 8, P ₂ : back pressure on the secondary side of the RO membrane module 8, Δπ: of the RO membrane module 8 Osmotic pressure difference, P _s : pressure on the suction side of the pressure pump 6)

In equation (3), the temperature correction coefficient K is a function of the detected temperature value T of the temperature sensor 5. Since the membrane area A is determined by the number of reverse osmosis membrane elements used, a preset value can be used. In the calculation of the effective pressure P _e according to formula (4), the values of ΔP _{1, P 2, Δπ,} and P _s, is operating steadily, because that regarded as substantially constant, the use of a preset value Can do. Therefore, if at least three parameters including the detected temperature value T of the temperature sensor 5, the detected flow value Q _p of the flow sensor 9, and the detected pressure value P _d of the pressure sensor 15 are acquired during operation of the membrane separator, it can be calculated water permeability coefficient L _p at the reference temperature.

In step ST303, the control unit 10A acquires the detected temperature value T of the soft water W2 detected by the temperature sensor 5.
In step ST304, the control unit 10A calculates the temperature correction coefficient K based on the detected temperature value T acquired in step ST303.

In step ST305, the control unit 10A obtains or calculates the target flow rate value Q _p ′, water permeation coefficient L _p , temperature correction coefficient K, and required set values (A, ΔP ₁ , P ₂ , Δπ) obtained in the previous step. , P _s ), the discharge pressure P _d ′ of the pressure pump 6 is calculated based on the above formulas (3) and (4). Then, the calculated value of the discharge pressure P _d ′ is set as the target pressure value.

  In step ST306, the control unit 10A determines whether or not the time measured by an internal timer (not shown) has reached 100 ms, which is the control cycle. In step ST306, when it is determined by control unit 10A that the time measured by the timer has reached 100 ms (YES), the process proceeds to step ST307. In Step ST306, when it is determined by the control unit 10A that the time measured by the timer has not reached 100 ms (NO), the process returns to Step ST306.

Step ST 307: In (step ST 306 YES judgment), the control unit 10A acquires the detected pressure value _{P d} of the pressure pump 6 detected by the pressure sensor 15.
In step ST 308, the control unit 10A, so that the deviation between the detected pressure value obtained in step ST 307 (feedback value) _{P d} and the target pressure value _{P d} set in step ST 305 'is zero, velocity type digital PID algorithm To calculate the operation amount U. In the velocity type digital PID algorithm, the change amount of the operation amount is calculated every control cycle (100 ms), and this operation amount is determined by adding this to the previous operation amount.

In step ST309, the control unit 10A calculates the driving frequency F of the pressurizing pump 6 based on the operation amount U, the target pressure value P _d ′, and the maximum driving frequency of the pressurizing pump 6 (set value of 50 Hz or 60 Hz). To do.
In step ST310, the control unit 10A converts the calculated value of the drive frequency F into a corresponding current value signal (4 to 20 mA).

  In step ST311, control unit 10A outputs the converted current value signal to inverter 7. Thereby, the process of this flowchart is complete | finished (it returns to step ST301).

  Further, the control unit 10A performs the recovery rate control of the permeated water W5 based on the hardness of the soft water W2 (hereinafter, also referred to as “water quality feedforward recovery rate control”). This water quality feedforward recovery rate control is executed in parallel with the pressure feedback water amount control described above.

  Next, water quality feedforward recovery rate control by the control unit 10A will be described. FIG. 9 is a flowchart illustrating a processing procedure when the control unit 10A executes the water quality feedforward recovery rate control. The process of the flowchart shown in FIG. 9 is repeatedly executed during operation of the water treatment system 1.

In step ST401 shown in FIG. 9, the control unit 10A acquires the target flow rate value Q _p ′ of the permeated water W5. This target flow rate value Q _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

At step ST 402, the control unit 10A acquires the measured hardness value _{C c} of the soft water W2 measured by the hardness sensor 14.
In step ST 403, the control unit 10A acquires the calcium carbonate solubility _{S c} to water. This calcium carbonate solubility _Sc is, for example, a set value input to the memory by the system administrator via a user interface (not shown). In addition, the calcium carbonate solubility with respect to water can be regarded as a substantially constant value at a normal operation temperature (5 to 35 ° C.).

In step ST404, the control unit 10A calculates an allowable concentration factor _Nc of calcium carbonate in the concentrated water W6 based on the measured hardness value C _c and the calcium carbonate solubility S _c acquired in the previous step. The permissible concentration factor _Nc of calcium carbonate can be obtained by the following equation (5).
N _c = S _c / C _c (5)
For example, if the measured hardness value C _c is ₃ mg CaCO ₃ / L and the calcium carbonate solubility S _{c at} 25 ° C. is 15 mg CaCO ₃ / L, the allowable concentration ratio N _c is “5”.

In step ST 405, the control unit 10A, the previous target flow rate value Q _p acquired or calculated in step _', and based on the allowable concentration rate N _c, wastewater flow rate recovery is maximized (target drainage flow Q _d') Is calculated. The target drainage flow rate Q _d ′ can be obtained by the following equation (6).
Q _d ′ = Q _p ′ / (N _c −1) (6)

In step ST 406, the control unit 10A controls the opening and closing of the actual drainage flow _{Q d} is the target wastewater flow rate and _{Q d} 'so as to first drain valve 11 to the third drain valve 13 calculated in step ST405 concentrated water W6 . Thereby, the process of this flowchart is complete | finished (it returns to step ST401).

  According to 1 A of water treatment systems which concern on 2nd Embodiment mentioned above, the effect similar to 1st Embodiment is acquired. In particular, in the water treatment system 1A according to the second embodiment, the control unit 10A controls the flow rate of the permeated water W5 by pressure feedback water amount control. This pressure feedback water amount control can be executed as a backup of the flow rate feedback water amount control in the first embodiment. For this reason, even if a failure occurs in the flow rate sensor 9 (see FIG. 1) during the execution of the flow rate feedback water amount control of the first embodiment, a stable water amount can be obtained by switching to the pressure feedback water amount control of the second embodiment. The permeated water W5 can be manufactured.

  In the water treatment system 1A according to the second embodiment, the control unit 10A performs water quality feedforward recovery rate control. For this reason, in the water treatment system 1A, even when the amount of hardness leak increases due to poor regeneration of the water softening device 3, the precipitation of calcium carbonate scale in the RO membrane module 8 while maximizing the recovery rate of the permeated water W5. Can be more reliably suppressed.

(Third embodiment)
Next, a water treatment system 1B according to a third embodiment of the present invention will be described with reference to FIG. FIG. 10 is an overall configuration diagram of a water treatment system 1B according to the third embodiment. In the third embodiment, differences from the first embodiment will be mainly described. In the third embodiment, the same or equivalent components as those in the first embodiment and the second embodiment will be described with the same reference numerals. Moreover, in 3rd Embodiment, the description which overlaps with 1st Embodiment and 2nd Embodiment is abbreviate | omitted suitably.

  As shown in FIG. 10, the water treatment system 1B according to the third embodiment includes a raw water pump 2, a hard water softening device 3, a salt water tank 4, a temperature sensor 5, a pressure pump 6, an inverter 7, RO membrane module 8. Further, the water treatment system 1B includes a control unit 10B, a first drain valve 11 to a third drain valve 13, and an electric conductivity sensor 16 as electric conductivity measuring means.

  The electrical conductivity sensor 16 is a device that measures the electrical conductivity of the permeated water W5 flowing through the permeated water line L5. The electrical conductivity sensor 16 is connected to the permeated water line L5 at the connection portion J2. The electrical conductivity sensor 16 is electrically connected to the control unit 10B. The electric conductivity of the permeated water W5 measured by the electric conductivity sensor 16 (hereinafter also referred to as “measured electric conductivity value”) is transmitted as a detection signal to the control unit 10B.

  The control unit 10B is configured by a microprocessor (not shown) including a CPU and a memory. The control unit 10B controls the operation of the process control valve 32 (see FIG. 2) based on detection signals and the like input from a soft water flow sensor (not shown) and a salt water flow sensor. A control program for operating the water softening device 3 in the third embodiment is stored in advance in the memory of the control unit 10B. The CPU controls the process control valve 32 so as to sequentially switch the softening process ST1 to the water replenishment process ST8 according to the control program stored in the memory (see FIG. 3).

  Further, the control unit 10B calculates the driving frequency of the pressurizing pump 6 using the detected temperature value of the temperature sensor 5 as a feedforward value so that the flow rate of the permeated water W5 becomes a preset target flow rate value. And the control part 10B outputs the electric current value signal corresponding to the computed value of the computed drive frequency to the inverter 7 (henceforth "temperature feedforward water amount control").

  Here, the temperature feedforward water amount control by the control unit 10B will be described. FIG. 11 is a flowchart illustrating a processing procedure when the control unit 10B executes the temperature feedforward water amount control. The process of the flowchart shown in FIG. 11 is repeatedly executed during operation of the water treatment system 1.

In step ST501 shown in FIG. 11, the control unit 10B acquires the target flow rate value Q _p ′ of the permeated water W5. This target flow rate value Q _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

In Step ST502, the control unit 10B acquires the water permeability coefficient L _p at the reference temperature (25 ° C.) of the RO membrane module 8. This water permeability coefficient L _p is, for example, a set value input to the memory by a system administrator via a user interface (not shown).

In addition, this temperature feedforward water amount control can be performed as a backup of the flow rate feedback water amount control in the first embodiment. In that case, the water permeability coefficient L _p may be a calculated value immediately before the failure of the flow sensor 9 (see FIG. 1) occurs. The water permeation coefficient L _{p at the} reference temperature can be calculated by the method described in the second embodiment.

In step ST503, the control unit 10B acquires the detected temperature value T of the soft water W2 detected by the temperature sensor 5.
In step ST504, the control unit 10B calculates a temperature correction coefficient K based on the detected temperature value T acquired in step ST503.

In step ST505, the control unit 10B obtains or calculates the target flow rate value Q _p ′, water permeation coefficient L _p , temperature correction coefficient K, and required set values (A, ΔP ₁ , P ₂ , Δπ) obtained in the previous step. , P _s ), the discharge pressure P _d ′ of the pressurizing pump 6 is calculated based on the equations (3) and (4) described in the second embodiment.

In Step ST506, the control unit 10B calculates the driving frequency F of the pressurizing pump 6 based on the following equation (7) using the calculated value of the discharge pressure P _d ′.
^{_{F = a · P d '2}} + b · P d' + c (7)
(However, a, b, c are coefficients determined by the specifications of the pressure pump 6)

In step ST507, the control unit 10B converts the calculated value of the drive frequency F into a corresponding current value signal (4 to 20 mA).
In step ST508, control unit 10B outputs the converted current value signal to inverter 7. Thereby, the process of this flowchart is complete | finished (it returns to step ST501).

  Further, the control unit 10B performs recovery rate control of the permeated water W5 based on the electrical conductivity of the permeated water W5 (hereinafter also referred to as “water quality feedback recovery rate control”). This water quality feedback recovery rate control is executed in parallel with the temperature feedforward water amount control described above.

  Next, water quality feedback recovery rate control by the control unit 10B will be described. FIG. 12 is a flowchart illustrating a processing procedure when the control unit 10B executes water quality feedback recovery rate control. The process of the flowchart shown in FIG. 12 is repeatedly executed during operation of the water treatment system 1.

In step ST601 shown in FIG. 12, the control unit 10B obtains a target electrical conductivity value E _p ′ of the permeated water W5. The target electric conductivity value E _p ′ is an index of purity required for the permeated water W5. The target electrical conductivity value E _p ′ is, for example, a set value that is input to the memory by the system administrator via a user interface (not shown).

In step ST 602, the control unit 10B obtains the measured electric conductivity value _{E p} of the electric conductivity sensor 16 permeate water W5 measured by.
In step ST 603, the control unit 10B, as the deviation between the obtained measured electrical conductivity value (feedback value) _{E p} and step target electric conductivity value obtained at ST 301 _{E p} 'in step ST602 becomes zero, the The opening / closing of the first drain valve 11 to the third drain valve 13 is controlled. That is, by increasing or decreasing the drainage flow rate of the concentrated water W6, the concentration of dissolved salts on the membrane surface is changed so that the permeated water W5 having the required purity can be obtained. Thereby, the process of this flowchart is complete | finished (it returns to step ST601).

  According to the water treatment system 1B according to the third embodiment described above, the same effect as in the first embodiment can be obtained. In particular, in the water treatment system 1B according to the third embodiment, the flow rate of the permeated water W5 is controlled by temperature feedforward water amount control. This temperature feedforward water amount control can be executed as a backup of the flow rate feedback water amount control in the first embodiment. For this reason, even when a failure occurs in the flow rate sensor 9 (see FIG. 1) during the execution of the flow rate feedback water amount control of the first embodiment, it is stabilized by switching to the temperature feedforward water amount control of the third embodiment. Water permeate W5 can be produced.

  Moreover, in the water treatment system 1B which concerns on 3rd Embodiment, the control part 10B performs water quality feedforward collection | recovery rate control. For this reason, in the water treatment system 1B, the recovery rate of the permeated water W5 can be maximized while satisfying the water quality required for the permeated water W5.

The preferred embodiments of the present invention have been described above. However, the present invention is not limited to the above-described embodiments, and can be implemented in various forms.
For example, in the first embodiment, the example in which the silica concentration of the soft water W2 is acquired in the temperature feedforward recovery rate control has been described. Not only this but the silica density | concentration of raw | natural water W1 may be acquired.

In 2nd Embodiment, the water quality feedforward collection | recovery rate control demonstrated the example which calculates the waste_water | drain flow volume from which the collection | recovery rate becomes the maximum based on the permissible concentration rate of calcium carbonate and the target flow rate value of the permeate W5. The present invention is not limited to this, and the following method may be adopted. That is, compared with the allowable concentration rate N _s permissible concentration rate N _c and silica calcium carbonate, selects the smaller side allowable concentration rate. Then, based on the selected allowable concentration ratio and the target flow rate value of the permeated water W5, the drainage flow rate at which the recovery rate is maximized is calculated.

  In the first to third embodiments, the example in which the temperature of the soft water W2 supplied to the RO membrane module 8 is detected has been described. However, the temperature of the permeated water W5 obtained by the RO membrane module 8 may be detected. Further, the temperature of the concentrated water W6 obtained by the RO membrane module 8 may be detected.

  In the first to third embodiments, an example in which the drainage flow rate of the concentrated water W6 is adjusted stepwise by selectively opening and closing the first drainage valve 11 to the third drainage valve 13 in each recovery rate control will be described. did. It is good also as a structure which provided not only this but the proportional control valve in the concentrated water line L6. The drainage flow rate of the concentrated water W6 can be adjusted by transmitting a current value signal (for example, 4 to 20 mA) from the control unit to the proportional control valve to control the valve opening.

  Further, in the configuration in which the proportional control valve is provided, a flow rate sensor may be provided in the concentrated water line L6. The flow value detected by the flow sensor is input as a feedback value to the control unit. Thereby, the actual waste water flow rate of the concentrated water W6 can be controlled more accurately.

  In the first embodiment, the example in which the flow rate feedback water amount control and the temperature feedforward recovery rate control are combined has been described. Not limited to this, the pressure feedback water amount control and the temperature feedforward recovery rate control of the second embodiment may be combined. Moreover, it is good also as a structure which combined the temperature feedforward water amount control and temperature feedforward recovery rate control of 3rd Embodiment.

  In the second embodiment, the example in which the pressure feedback water amount control and the water quality feedforward recovery rate control are combined has been described. Not limited to this, the flow rate feedback water amount control and the water quality feedforward recovery rate control of the first embodiment may be combined. Further, the temperature feedforward water amount control and the water quality feedforward recovery rate control of the third embodiment may be combined.

  In the third embodiment, the example in which the temperature feedforward water amount control and the water quality feedback recovery rate control are combined has been described. Not limited to this, the flow rate feedback water amount control and the water quality feedback recovery rate control of the first embodiment may be combined. Moreover, it is good also as a structure which combined the pressure feedback water volume control and water quality feedback collection | recovery rate control of 2nd Embodiment.

  The present invention can be implemented in various other forms without departing from the spirit or main features thereof. Therefore, the above-described embodiments or examples are merely examples in all respects and should not be interpreted in a limited manner. The scope of the present invention is indicated by the scope of claims, and is not restricted by the text of the specification. Further, all modifications and changes belonging to the equivalent scope of the claims are within the scope of the present invention.

1, 1A, 1B Water treatment system 3 Water softening device 5 Temperature sensor (temperature detection means)
6 Pressurizing pump 7 Inverter 8 RO membrane module 9 Flow rate sensor (flow rate detection means)
10, 10A, 10B Control unit 11 First drain valve (drain valve)
12 Second drain valve (drain valve)
13 Third drain valve (drain valve)
14 Hardness sensor (hardness measuring means)
15 Pressure sensor (pressure detection means)
16 Electric conductivity sensor (electric conductivity measuring means)
L1 Raw water line L2 Soft water line L3 Salt water line L4 Drainage line L5 Permeate water line L6 Concentrated water line W1 Raw water W2 Soft water W3 Salt water W4 Drainage W5 Permeated water W6 Concentrated water

Claims (7)

A hard water softening device for producing soft water from raw water, and a membrane separation device for producing permeated water from soft water,
The water softening device comprises a cation exchange resin bed to which raw water or regenerated liquid is supplied,
A softening process in which raw water is passed through the cation exchange resin bed in a downward flow to obtain soft water; the regenerated liquid is collected at the bottom while being distributed to the top of the cation exchange resin bed, and A first regeneration process that generates a downward flow and regenerates the entire cation exchange resin bed; and, after the first regeneration process, distributes the regeneration liquid to the bottom of the cation exchange resin bed, And a valve means capable of generating an upward flow of regenerated liquid by collecting the liquid and switching to a second regenerating process for regenerating a part of the cation exchange resin bed,
The membrane separator comprises a reverse osmosis membrane module that separates supplied soft water into permeated water and concentrated water;
A pressure pump that is driven at a rotational speed according to the input driving frequency, sucks soft water, and discharges it toward the reverse osmosis membrane module;
An inverter that outputs a driving frequency corresponding to the input current value signal to the pressurizing pump;
The driving frequency of the pressurizing pump is calculated using a physical quantity in the system so that the flow rate of permeated water becomes a preset target flow rate value, and a current value signal corresponding to the calculated value of the driving frequency is calculated by the inverter. A control unit that outputs to
A water treatment system comprising. The membrane separation device includes a flow rate detection means for detecting a flow rate of permeated water,
The control unit calculates a driving frequency of the pressurizing pump so that a detected flow rate value of the flow rate detection unit becomes the target flow rate value;
The water treatment system according to claim 1. The membrane separation device includes pressure detection means for detecting a discharge pressure of the pressure pump;
Temperature detecting means for detecting the temperature of soft water, permeated water or concentrated water, and
The controller calculates (i) a discharge pressure of the pressurizing pump based on a detected temperature value of the temperature detecting means, a water permeation coefficient value at a reference temperature of the reverse osmosis membrane module, and the target flow rate value. (Ii) setting the calculated value of the discharge pressure as a target pressure value, and (iii) calculating the driving frequency of the pressurizing pump so that the detected pressure value of the pressure detecting means becomes the target pressure value.
The water treatment system according to claim 1. The membrane separation device comprises temperature detection means for detecting the temperature of soft water, permeated water or concentrated water,
The controller calculates (i) a discharge pressure of the pressurizing pump based on a detected temperature value of the temperature detecting means, a water permeation coefficient value at a reference temperature of the reverse osmosis membrane module, and the target flow rate value. (Ii) calculating the driving frequency of the pressurizing pump based on the calculated value of the discharge pressure;
The water treatment system according to claim 1. The membrane separation device includes temperature detecting means for detecting the temperature of soft water, permeated water or concentrated water;
A drainage valve capable of adjusting the drainage flow of the concentrated water discharged outside the device,
The controller calculates (i) an allowable concentration rate of silica in the concentrated water based on the silica concentration determined from the silica concentration of raw water or soft water acquired in advance and the detected temperature value of the temperature detecting means, ii) calculating the drainage flow rate from the calculated value of the permissible concentration rate and the target flow rate value of the permeated water, and (iii) adjusting the drainage valve so that the actual drainage flow rate of the concentrated water becomes the calculated value of the drainage flow rate. Control,
The water treatment system according to claim 1. The membrane separator includes a hardness measuring means for measuring the calcium hardness of soft water,
A drainage valve capable of adjusting the drainage flow of the concentrated water discharged outside the device,
The control unit calculates (i) an allowable concentration rate of calcium carbonate in concentrated water based on (i) the calcium carbonate solubility acquired in advance and the measured hardness value of the hardness measuring means, and (ii) the allowable concentration rate Calculate the drainage flow rate from the calculated value and the target flow rate value of the permeated water, and (iii) control the drainage valve so that the actual drainage flow rate of the concentrated water becomes the calculated value of the drainage flow rate.
The water treatment system according to claim 1. The membrane separation device comprises electrical conductivity measuring means for measuring electrical conductivity of permeated water,
A drainage valve capable of adjusting the drainage flow of the concentrated water discharged outside the device,
The control unit controls the flow rate of drainage from the drainage valve so that the measured electrical conductivity value of the electrical conductivity measuring unit becomes a preset target electrical conductivity value.
The water treatment system according to claim 1.

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