JP2013146684A - Reverse osmosis membrane separator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a reverse osmosis membrane separator capable of improving the recovery rate while controlling deposition of scale.SOLUTION: The reverse osmosis membrane separator includes: a reverse osmosis membrane module 5; a temperature detection means 4; and a control part 10 for alternately executing a high recovery rate operation mode for calculating a reference concentration ratio of silica in concentrated water W3 according to silica solubility determined from silica concentration of supply water W1 and a detected temperature value of the temperature detection means 4, controlling the flow rate of the supply water W1 so that the actual concentration ratio of the silica in the concentrated water W3 is a first target concentration ratio of reference concentration ratio excess, and controlling the discharge flow rate so that the actual discharge flow rate of the concentrated water W3 is a target flow rate value of permeated water W2 and a target discharge flow rate calculated according to the first target concentration ratio, and a low recovery rate operation mode for controlling the flow rate of the supply water W1 so that the actual concentration ratio of the silica in the concentrated water W3 is a second target concentration ratio of the reference concentration ratio or less, and controlling the discharge flow rate so that the actual discharge flow rate of the concentrated water W3 is the target discharge flow rate.

Description

  The present invention relates to a reverse osmosis membrane separation device including a reverse osmosis membrane module.

  In the semiconductor manufacturing process, the cleaning of electronic parts and medical instruments, etc., high-purity pure water containing no impurities is used. This type of pure water is generally produced by subjecting raw water such as groundwater or tap water to a reverse osmosis membrane separation treatment with a reverse osmosis membrane module (hereinafter also referred to as “RO membrane module”). By performing reverse osmosis membrane separation treatment with the RO membrane module, the raw water is separated into permeated water from which dissolved salts and the like are removed and concentrated water from which dissolved salts and the like are concentrated.

  In the RO membrane module, 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 on the surface of the RO membrane, the water permeability is reduced. For this reason, in a reverse osmosis membrane separation apparatus provided with an RO membrane module, it is important to operate so that scale deposition and fouling do not occur on the surface of the RO membrane.

  Conventionally, a reverse osmosis membrane separation apparatus that operates by setting a recovery rate within a range where the silica concentration of concentrated water does not exceed silica solubility in order to suppress precipitation of silica-based scale is known (for example, Patent Document 1). reference).

JP 2005-81254 A

  In the reverse osmosis membrane separation apparatus described in the above patent document, the recovery rate is limited by the solubility of silica. When the silica concentration of the raw water increases, the recovery rate is inevitably lowered. Therefore, in an area where the silica concentration of the raw water is high, the amount of concentrated water to be discarded increases, resulting in an increase in water production cost. The recovery rate refers to the ratio of the flow rate of the permeated water to the flow rate of the supplied water supplied to the RO membrane module.

  Therefore, an object of the present invention is to provide a reverse osmosis membrane separation device capable of improving the recovery rate while suppressing the precipitation of silica-based scale.

  The present invention includes a reverse osmosis membrane module that separates feed water into permeate and concentrated water, temperature detection means for detecting the temperature of the feed water, (i) silica concentration of the feed water obtained in advance and the temperature detection Based on the silica solubility determined from the temperature detected by the means, the reference concentration ratio of silica in the concentrated water is calculated, and (ii) the first target concentration ratio that the actual concentration ratio of silica in the concentrated water exceeds the reference concentration ratio The flow rate of the feed water supplied to the reverse osmosis membrane module is controlled so that the target drainage flow rate is calculated based on the preset permeate target flow rate value and the first target concentration rate, A high recovery rate operation mode for controlling the drainage flow rate of the concentrated water so that the actual drainage flow rate becomes the target drainage flow rate, and the second point where the actual concentration rate of silica in the concentrated water is equal to or less than the reference concentration rate The flow rate of the feed water supplied to the reverse osmosis membrane module is controlled so as to achieve a concentration rate, and the concentrated water is adjusted so that the actual drainage flow rate of the concentrated water becomes the target drainage flow rate calculated in the high recovery rate operation mode. The present invention relates to a reverse osmosis membrane separation device including a control unit that alternately executes a low recovery rate operation mode for controlling a drainage flow rate.

  Moreover, in the said control part, it is preferable that the 1st time slot | zone which performs high recovery rate operation mode is set longer than the 2nd time slot | zone which performs low recovery rate operation mode.

  In the reverse osmosis membrane separation device, the flow rate detecting means for detecting the flow rate of the permeated water, the supply water line for supplying the supply water to the reverse osmosis membrane module, and the rotational speed according to the input drive frequency are driven. A pressure pump that pumps the feed water flowing through the feed water line toward the reverse osmosis membrane module, and an inverter that outputs a driving frequency corresponding to the input current value signal to the pressure pump. The control unit calculates a driving frequency of the pressurizing pump so that the detected flow rate value by the flow rate detecting unit becomes the target flow rate value, and a current value corresponding to the calculated value of the driving frequency It is preferable to output a signal to the inverter.

  In the reverse osmosis membrane separation apparatus, a permeated water line for sending permeate to a customer, a concentrated water line for sending concentrated water from the reverse osmosis membrane module, and a concentrated water flowing through the concentrated water line. A concentrated water discharge line for discharging the part to the outside of the apparatus, a concentrated water reflux line for refluxing the remaining portion of the concentrated water flowing through the concentrated water line upstream of the pressurizing pump in the supply water line, and the concentrated water A concentrated water recirculation valve capable of adjusting a flow rate of the concentrated water flowing through the reflux line, and when the controller executes the low recovery rate operation mode, the concentrated water reflux line is It is preferable to control the concentrated water reflux valve so as not to flow.

  The controller preferably executes the flushing operation mode for cleaning the primary side of the reverse osmosis membrane module at least once after the high recovery rate operation mode is executed a plurality of times.

  In the reverse osmosis membrane separation device, the permeated water valve provided in the permeated water line and the permeated water sent to the permeated water line are returned upstream of the pressurizing pump in the supply water line. The control unit includes a permeate return line and a pressure relief valve provided in the permeate return line, and the control unit performs (i) the concentrated water return line when executing the flushing operation mode. It is preferable to control the concentrated water reflux valve so that the concentrated water does not flow, and (ii) control the permeated water valve so that the permeated water does not flow through the permeated water line.

  ADVANTAGE OF THE INVENTION According to this invention, the reverse osmosis membrane separation apparatus which can improve a recovery rate can be provided, suppressing precipitation of a silica type scale.

1 is an overall configuration diagram of a reverse osmosis membrane separation device 1 according to an embodiment. It is a flowchart which shows the process sequence in the case of performing switching control of the high recovery rate operation mode, the low recovery rate operation mode, and flushing operation mode in the control part 10. It is a flowchart which shows the process sequence in case the control part 10 performs flow volume feedback water volume control in a high recovery rate operation mode and a low recovery rate operation mode. It is a flowchart which shows the process sequence in case the control part 10 performs temperature feedforward collection | recovery rate control in high recovery rate operation mode. It is a flowchart which shows the process sequence in case the control part 10 performs temperature feedforward collection | recovery rate control in low collection | recovery rate operation mode. 4 is a flowchart illustrating a processing procedure when a flushing operation mode is executed in the control unit 10.

  Hereinafter, embodiments of a reverse osmosis membrane separation device according to the present invention will be described with reference to the drawings. The reverse osmosis membrane separation device 1 according to the present embodiment 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 reverse osmosis membrane separation device 1 according to the present embodiment.

  As shown in FIG. 1, a reverse osmosis membrane separation device 1 according to this embodiment includes a pressurizing pump 2, an inverter 3, a temperature sensor 4 as temperature detection means, and an RO membrane module 5 as a reverse osmosis membrane module. And a flow rate sensor 6 as a flow rate detection means and a permeated water valve 7. The reverse osmosis membrane separation device 1 includes a concentrated water recirculation valve 8, a safety valve 9 as a pressure relief valve, a control unit 10, and a first drain valve 11 to a third drain valve 13. In FIG. 1, a path of electrical connection is indicated by a broken line.

  The reverse osmosis membrane separation device 1 includes a supply water line L1, a permeate water line L2, a concentrate water line L3, a concentrate water discharge line L4, a concentrate water reflux line L5, and a permeate return line L6. Prepare. 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 supply water line L1 is a line for supplying the supply water W1 to the RO membrane module 5. The upstream end of the supply water line L1 is connected to a supply source (not shown) of the supply water W1. The downstream end of the supply water line L <b> 1 is connected to the primary inlet port of the RO membrane module 5.

  The pressurizing pump 2 is a device that sucks the supply water W <b> 1 and discharges it toward the RO membrane module 5. The pressurizing pump 2 is electrically connected to an inverter 3 (described later). The driving power whose frequency is converted is input from the inverter 3 to the pressurizing pump 2. The pressurizing pump 2 is driven at a rotational speed corresponding to the frequency of the supplied driving power (hereinafter also referred to as “driving frequency”).

  The inverter 3 is an electric circuit that supplies driving power whose frequency is converted to the pressurizing pump 2. The inverter 3 is electrically connected to the control unit 10. The inverter 3 receives a current value signal from the control unit 10. The inverter 3 outputs driving power having a driving frequency corresponding to the current value signal input from the control unit 10 to the pressurizing pump 2.

  The temperature sensor 4 is a device that detects the temperature of the supply water W1. The temperature sensor 4 is connected to the supply water line L1 at the connection portion J1. The connecting portion J1 is disposed between the supply source (not shown) of the supply water W1 and the pressurizing pump 2. The temperature sensor 4 is electrically connected to the control unit 10. The temperature of the supply water W1 detected by the temperature sensor 4 (hereinafter also referred to as “detected temperature value”) is transmitted to the control unit 10 as a detection signal.

  The RO membrane module 5 is a facility that performs membrane separation processing of the feed water W1 sent from the pressurizing pump 2 into permeate water W2 from which dissolved salts have been removed and concentrated water W3 from which dissolved salts have been concentrated. The RO membrane module 5 includes a single or a plurality of RO membrane elements (not shown). The RO membrane module 5 membrane-separates the supply water W1 with these RO membrane elements to produce permeated water W2 and concentrated water W3.

  The permeated water line L2 is a line for sending the permeated water W2 manufactured by the RO membrane module 5 to a customer. The upstream end of the permeate line L2 is connected to the secondary port of the RO membrane module 5. The downstream end of the permeate line L2 is connected to a demand destination device or the like (not shown).

  The flow rate sensor 6 is a device that detects the flow rate of the permeated water W2 flowing through the permeated water line L2. The flow sensor 6 is connected to the permeated water line L2 at the connection portion J2. The flow sensor 6 is electrically connected to the control unit 10. The flow rate of the permeated water W2 detected by the flow rate sensor 6 (hereinafter also referred to as “detected flow rate value”) is transmitted to the control unit 10 as a detection signal.

  The permeated water valve 7 is a device that opens and closes the permeated water line L2. The permeated water valve 7 is electrically connected to the control unit 10. The opening and closing of the valve body in the permeated water valve 7 is controlled by a drive signal from the control unit 10. The permeated water valve 7 is controlled to be in an open state in the high recovery rate operation mode and the low recovery rate operation mode (described later). Further, the permeated water valve 7 is controlled to be closed in the flushing operation mode (described later).

  The concentrated water line L3 is a line for sending the concentrated water W3 from the RO membrane module 5. The upstream end of the concentrated water line L3 is connected to the primary outlet port of the RO membrane module 5. Further, the downstream side of the concentrated water line L3 branches into a concentrated water discharge line L4 and a concentrated water reflux line L5 at the connection portion J3.

  The concentrated water discharge line L4 is a line for discharging a part of the concentrated water W3 flowing through the concentrated water line L3 to the outside of the apparatus. The downstream side of the concentrated water discharge line L4 branches to the first drainage line L11, the second drainage line L12, and the third drainage line L13 at the connecting portions J5 and J6.

  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 1st drain valve 11-the 3rd drain valve 13 are valves which adjust the drainage flow volume of the concentrated water W3 discharged | emitted out of the apparatus from the concentrated water discharge line L4.

  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 5 is 80% in the open state. The drainage flow rate of the second drain valve 12 is set so that the recovery rate of the RO membrane module 5 is 75% in the open state. The drainage flow rate of the third drain valve 13 is set so that the recovery rate of the RO membrane module 5 is 70% in the open state.

  The drainage flow rate of the concentrated water W3 discharged from the concentrated water line L3 can be adjusted in stages 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 5 can be 75%. 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 5 can be set to 70%. Therefore, in this embodiment, the drainage flow rate of the concentrated water W3 is 5% between the recovery rate of 50% and 80% 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 concentrated water reflux line L5 is a line for refluxing the remaining portion of the concentrated water W3 flowing through the concentrated water line L3 to the upstream side of the pressurizing pump 2 in the supply water line L1. The upstream end of the concentrated water reflux line L5 is connected to the concentrated water line L3 at the connection J3. The connection portion J3 is disposed between the primary side outlet port of the RO membrane module 5 and the connection portion J5. The downstream end of the concentrated water recirculation line L5 is connected to the supply water line L1 at the connection J4. The connecting portion J4 is disposed on the upstream side of the pressurizing pump 2.

  The concentrated water reflux valve 8 is a device that adjusts the flow rate of the concentrated water reflux line L5. The concentrated water reflux valve 8 is electrically connected to the control unit 10. The opening degree of the valve body in the concentrated water recirculation valve 8 is controlled by a drive signal from the control unit 10. The concentrated water recirculation valve 8 is controlled to a predetermined opening degree in the high recovery rate operation mode. Further, the valve body of the concentrated water recirculation valve 8 is controlled to be closed (opening degree 0%) in the low recovery rate operation mode and the flushing operation mode (both described later).

  The permeated water return line L6 is a line for returning the permeated water W2 sent to the permeated water line L2 to the upstream side of the pressurized pump 2 in the supply water line L1 in the flushing operation mode. The upstream end of the permeate return line L6 is connected to the permeate line L2 at the connection J7. The connecting portion J7 is disposed between the secondary port of the RO membrane module 5 and the permeated water valve 7. Further, the downstream end of the permeate return line L6 is connected to the supply water line L1 at the connection J8. The connecting portion J8 is disposed on the upstream side of the pressurizing pump 2. A safety valve 9 is provided in the permeate return line L6.

  The safety valve 9 is a valve that opens when the in-pipe pressure of the permeated water line L2 is equal to or higher than a set pressure in the flushing operation mode, and causes the permeated water W2 to flow through the permeated water return line L6. That is, the safety valve 9 returns the permeated water W2 that is equal to or higher than the set pressure to the supply water line L1 via the permeate return line L6, thereby generating excessive back pressure on the secondary side of the RO membrane module 5. To prevent.

  Note that, in the high recovery rate operation mode and the low recovery rate operation mode, the permeate water valve 7 is controlled to be in the open state, and thus the in-pipe pressure of the permeate line L2 is less than the set pressure. Therefore, in the high recovery rate operation mode and the low recovery rate operation mode, the permeated water W2 is sent to the demand destination with the safety valve 9 closed.

  The control unit 10 includes a microprocessor (not shown) including a CPU and a memory. The microprocessor incorporates an integrated timer unit (not shown) (hereinafter also referred to as “ITU”) that manages time measurement and the like. Hereinafter, functions of the control unit 10 will be described.

(Operation mode switching control)
Based on the silica solubility determined from (i) the silica concentration of the supply water W1 acquired in advance and the temperature value detected by the temperature sensor 4, the control unit 10 determines the reference concentration rate (dissolved limit concentration rate) of silica in the concentrated water W3. ) And (ii) control the flow rate of the supply water W1 supplied to the RO membrane module 5 so that the actual concentration ratio of silica in the concentrated water W3 becomes a first target concentration ratio (described later) exceeding the reference concentration ratio. A low recovery rate control mode and a low flow rate for controlling the flow rate of the supply water W1 supplied to the RO membrane module 5 so that the actual concentration rate of silica in the concentrated water W3 is a second target concentration rate (described later) equal to or lower than the reference concentration rate. The recovery operation mode is executed alternately. In the present embodiment, the high recovery rate operation mode and the low recovery rate operation mode are alternately executed nine times, and after execution of the tenth high recovery rate operation mode, the tenth low recovery rate operation mode is executed. Then, the flushing operation mode is executed once.

(High recovery rate operation mode control)
In the high recovery rate operation mode, the control unit 10 controls the flow rate of the supply water W1 so that the actual concentration rate of silica in the concentrated water W3 becomes a first target concentration rate (described later) that exceeds the reference concentration rate. Specifically, while controlling the flow rate of the permeated water W2 to a preset target flow rate value (first target flow rate value) by flow rate feedback water amount control (described later), by temperature feedforward recovery rate control (described later), The drainage flow rate is controlled so that the actual drainage flow rate of the concentrated water W3 becomes the target drainage flow rate. The target drainage flow rate in the high recovery rate operation mode is calculated from the first target flow rate value and the first target concentration magnification (described later).

  In addition, when executing the high recovery rate operation mode, the control unit 10 controls the permeated water valve 7 to be in an open state and controls the concentrated water recirculation valve 8 to a predetermined opening degree.

In the high recovery rate operation mode, the flow rate of the feed water W1 (that is, the flow rate of the permeated water W2 and the concentrated water W3 so that the actual concentration rate of silica in the concentrated water W3 is 1.2 to 1.8 times the reference concentration rate). It is preferable to control the total drainage flow rate). Hereinafter, the concentration ratio at which the actual concentration ratio is 1.2 to 1.8 times the reference concentration ratio is also referred to as “first target concentration ratio”. For example, when the silica concentration of the feed water W1 is 20 mgSiO ₂ / L and the silica solubility at 25 ° C. is 100 mgSiO ₂ / L, the standard concentration ratio is 5, so the first target concentration ratio is 6 to 9. . The recovery rate at this time is 83 to 89%.

(Low recovery rate operation mode control)
In the low recovery rate operation mode, the control unit 10 controls the flow rate of the supply water W1 so that the actual concentration rate of silica in the concentrated water W3 becomes a second target concentration rate (described later) that is equal to or lower than the reference concentration rate. Specifically, the temperature feedforward recovery rate control (second target flow rate value) is controlled while controlling the flow rate of the permeated water W2 to a lower target flow rate value (second target flow rate value) than in the high recovery rate operation mode by flow rate feedback water amount control (described later). According to the later description, control is performed so that the drainage flow rate of the concentrated water W3 becomes the target drainage flow rate calculated in the high recovery rate operation mode. The second target flow rate value in the low recovery rate operation mode is calculated from the target drainage flow rate of the concentrated water W3 calculated in the high recovery rate operation mode and the second target concentration rate (described later).

  Further, when executing the low recovery rate operation mode, the control unit 10 controls the concentrated water recirculation valve 8 to be closed (opening degree 0%) so that the concentrated water W3 does not flow through the concentrated water recirculation line L5. . The opening and closing of the permeate valve 7 is the same as in the high recovery rate operation mode.

In the low recovery rate operation mode, the flow rate of the supply water W1 (that is, the flow rate of the permeated water W2 and the concentration water W3 is adjusted so that the actual concentration rate of silica in the concentrated water W3 is 0.8 to 1 times the reference concentration rate). It is preferable to control the total drainage flow rate). Hereinafter, the concentration ratio at which the actual concentration ratio is 0.8 to 1 times the reference concentration ratio is also referred to as “second target concentration ratio”. For example, when the silica concentration of the feed water W1 is 20 mgSiO ₂ / L and the silica solubility at 25 ° C. is 100 mgSiO ₂ / L, the standard concentration ratio is 5, and therefore the second target concentration ratio is 4 to 5. . The recovery rate at this time is 75 to 80%.

(Flushing operation mode control)
The control unit 10 alternately executes the high recovery rate operation mode and the low recovery rate operation mode nine times, and after executing the tenth high recovery rate operation mode, replaces the execution of the tenth low recovery rate operation mode. Then, the flushing operation mode is executed once. The flushing operation mode is an operation mode for cleaning the primary side of the RO membrane module 5.

  In the flushing operation mode, low-concentration supply water W1 that is not mixed with the concentrated water W3 is supplied to the primary side of the RO membrane module 5. In the flushing operation mode, the pressurizing pump 2 is fixed to a driving frequency (for example, 30 Hz) lower than the maximum driving frequency (50 Hz or 60 Hz). At this time, most of the supply water W1 flows through the surface of the RO membrane without passing through the RO membrane, and is discharged to the outside from the concentrated water discharge line L4 as flushing waste water. By executing this flushing operation mode, scale nuclei and deposited suspended substances deposited on the surface of the RO membrane can be removed. The flushing operation mode is preferably executed after the high recovery rate operation mode is executed about 10 to 20 times.

  When executing the flushing operation mode, the control unit 10 controls (i) the concentrated water recirculation valve 8 to be closed so that the concentrated water W3 does not flow through the concentrated water recirculation line L5, and (ii) the permeated water line L2 The permeated water valve 7 is controlled to be closed so that the permeated water W2 does not flow. The reason why the concentrated water recirculation valve 8 is controlled to be closed is that the removed scale nucleus and suspended substances are not reattached to the surface of the RO membrane. The permeated water valve 7 is controlled to be closed in order to efficiently use the supplied water W1 for flushing cleaning.

(Time control for each operation mode)
In the control unit 10, the first time zone for executing the high recovery rate operation mode is set to 50 minutes, and the second time zone for executing the low recovery rate operation mode is set to 10 minutes. For example, when the operation in the high recovery rate operation mode with a recovery rate of 85% is set to 50 minutes and the operation in the low recovery rate operation mode with a recovery rate of 75% is set to 10 minutes, the average recovery rate per hour is 83. %. By the way, when the silica concentration of the supply water W1 is 20 mgSiO ₂ / L and the silica solubility at 25 ° C. is 100 mgSiO ₂ / L, the normal reference concentration factor is 5. When operating at this standard concentration rate, the recovery rate is 80%. Moreover, in the control part 10, the 3rd time slot | zone which performs flushing operation mode is set to 2 minutes.

(Flow rate feedback water volume control)
The control unit 10 performs flow rate feedback water volume control during execution of the high recovery rate operation mode and the low recovery rate operation mode. In this control, the control unit 10 is configured so that the flow rate value detected by the flow rate sensor 6 becomes a preset target flow rate value (first target flow rate value) or a calculated target flow rate value (second target flow rate value). The drive frequency of the pressure pump 2 is calculated, and a current value signal corresponding to the calculated value of the drive frequency is output to the inverter 3. That is, the control part 10 adjusts the rotation speed of the pressurizing pump 2 so that the permeated water W2 having a constant flow rate is produced. The first target flow rate value in the high recovery rate operation mode is set based on the flow rate of the permeated water W2 required at the demand destination. Further, the second target flow rate value in the low recovery rate operation mode is calculated by calculation as described later.

(Temperature feedforward recovery rate control)
The control unit 10 executes the following temperature feedforward recovery rate control during execution of the high recovery rate operation mode and the low recovery rate operation mode.

  In the temperature feedforward recovery rate control in the high recovery rate operation mode, the control unit 10 is based on the first target flow rate value set in advance and the first target concentration ratio that is maintained when the high recovery rate operation mode is executed. Calculate the target drainage flow rate in the high recovery rate operation mode. And the control part 10 controls opening and closing of the 1st drain valve 11-the 3rd drain valve 13 so that the actual waste_water | drain flow volume of the concentrated water W3 may turn into a target drain flow volume, when performing a high recovery rate operation mode.

  In the temperature feedforward recovery rate control in the low recovery rate operation mode, the control unit 10 sets the first drainage valves 11 to 11 so that the actual drainage flow rate of the concentrated water W3 becomes the target drainage flow rate calculated in the high recovery rate operation mode. The opening and closing of the third drain valve 13 is controlled.

  Next, operation mode switching control by the control unit 10 will be described. FIG. 2 is a flowchart illustrating a processing procedure when the control unit 10 executes switching control between the high recovery rate operation mode, the low recovery rate operation mode, and the flushing operation mode. The process of the flowchart shown in FIG. 2 is repeatedly performed during the operation of the reverse osmosis membrane separation device 1.

  In step ST101 shown in FIG. 2, the control unit 10 executes the high recovery rate operation mode. During execution of the high recovery rate operation mode, flow rate feedback water amount control (FIG. 3) and temperature feedforward recovery rate control (FIG. 4) described later are executed in parallel.

In step ST 102, the control unit 10 determines whether the time count _{t 1} by ITU reaches 50 minutes. In this step ST 102, the control unit 10, when the timing _{t 1} by ITU is determined to have reached 50 minutes (YES), the process proceeds to step ST 103. Further, in step ST 102, the control unit 10, time count _{t 1} by ITU is when it is determined not to reach the 50 minutes (NO), the process returns to step ST 101, to continue the high recovery operation mode.

In step ST 103, the control unit 10 resets the time count _{t 1} by ITU.

  In step ST104, the control unit 10 increments the count value of a counter n (not shown) that counts the number of executions of the high recovery rate operation mode by one. The counter n operates as an internal function of the control unit 10.

  In step ST105, the control unit 10 determines whether or not the count value of the counter n has reached 10 times. In step ST105, when the control unit 10 determines that the count value of the counter n has reached 10 times (YES), the process proceeds to step ST109. In step ST105, when the control unit 10 determines that the count value of the counter n has not reached 10 times (NO), the process proceeds to step ST106.

  In step ST106, the control unit 10 executes the low recovery rate operation mode. During execution of the low recovery rate operation mode, flow rate feedback water amount control (FIG. 3) and temperature feedforward recovery rate control (FIG. 5), which will be described later, are executed in parallel.

In step ST 107, the control unit 10 determines whether the time count _{t 2} by ITU has reached 10 minutes. In this step ST 107, the control unit 10, when the timing _{t 2} by ITU is determined to have reached 10 minutes (YES), the process proceeds to step ST 108. Further, in step ST 107, the control unit 10, when the timing _{t 2} by ITU is determined not to reach the 10 minutes (NO), the process returns to step ST 106, to continue the low recovery operation mode.

In step ST 108, the control unit 10 resets the time count _{t 2} by ITU, the process returns to step ST 101.

  In step ST109 (step ST105: YES determination), the control unit 10 executes the flushing operation mode. The flushing operation mode will be described later.

In step ST110, the control unit 10 determines whether the time count _{t 3} by ITU reached 2 minutes. In this step ST110, the control unit 10, when the timing _{t 3} by ITU is determined to have reached the 2 minutes (YES), the process proceeds to step ST111. Further, in step ST110, the control unit 10, when the timing _{t 3} by ITU is determined not reached 2 minutes (NO), the process returns to the step ST110.

In step ST111, the control unit 10 resets the time count _{t 3} by ITU.
In step ST112, the control unit 10 resets the count value of the counter n, and the process returns to step ST101.

  Next, flow rate feedback water amount control by the control unit 10 will be described. FIG. 3 is a flowchart illustrating a processing procedure when the control unit 10 executes the flow rate feedback water amount control. The process of the flowchart shown in FIG. 3 is repeatedly executed during operation in the high recovery rate operation mode and the low recovery rate operation mode.

  In step ST201 shown in FIG. 3, the control unit 10 controls the permeated water valve 7 to be in an open state.

In step ST202, the control unit 10 acquires or calculates a target flow rate value Q _p ′ of the permeated water W2. The target flow rate value Q _p ′ (first target flow rate value) in the high recovery rate operation mode is a set value input to the memory by the system administrator via a user interface (not shown). On the other hand, the target flow rate value Q _p ′ (second target flow rate value) in the low recovery rate operation mode is a value calculated in step ST407 of FIG. 5 as will be described later, specifically, in step ST307 of FIG. This is a value calculated from the calculated target drainage flow rate Q _d ′ and the second target concentration rate N ₂ ′ calculated in step ST405 of FIG. The target flow rate value Q _p ′ (second target flow rate value) in the low recovery rate operation mode can be obtained by the following equation (1).
_{Q p '= Q d' ·} (N 2 '-1) (1)
Note that the target flow rate value Q _p ′ has a relationship of first target flow rate value> second target flow rate value.

In step ST 203, the control unit 10 determines whether it has reached the 100ms timing _{t 4} by ITU is the control cycle. In this step ST 203, the control unit 10, when the timing _{t 4} by ITU is to have reached 100 ms (YES) determination, the process proceeds to step ST 204. Further, in step ST 203, the control unit 10, when the timing _{t 4} by ITU is determined not to reach the 100 ms (NO), the process returns to the step ST 203.

Step ST 204: In (step ST 203 YES judgment), the control unit 10 acquires the detected flow rate value _{Q p} of the permeate W2 detected by the flow sensor 6.

In step ST205, the control unit 10, so that the deviation between the target flow rate value _{Q p} 'acquired or calculated in step detected flow value acquired in ST 204 (feedback value) _{Q p} and step ST202 is zero, velocity type digital The manipulated variable U is calculated by the PID algorithm. In the velocity type digital PID algorithm, a change amount of the operation amount is calculated every control cycle (100 ms), and this amount of operation is added to the operation amount at the time of the previous control cycle to determine the current operation amount.

  In step ST206, the control unit 10 calculates the driving frequency F of the pressurizing pump 2 based on the current operation amount U and the maximum driving frequency of the pressurizing pump 2 (a set value of 50 Hz or 60 Hz).

  In step ST207, 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 ST208, the control part 10 outputs the converted electric current value signal to the inverter 3, and a process returns to step ST201. The inverter 3 supplies driving power converted to a frequency corresponding to the input current value signal to the pressurizing pump 2. As a result, the pressurizing pump 2 is driven at a rotational speed corresponding to the driving frequency input from the inverter 3.

  Next, temperature feedforward recovery rate control in the high recovery rate operation mode will be described. FIG. 4 is a flowchart showing a processing procedure when the control unit 10 performs the temperature feedforward recovery rate control in the high recovery rate operation mode. The process of the flowchart shown in FIG. 4 is repeatedly executed during operation in the high recovery rate operation mode.

In step ST301 shown in FIG. 4, the control unit 10 acquires the silica (SiO ₂ ) concentration C of the supply water W1. This silica concentration C is, for example, a set value input to the memory by the system administrator via a user interface (not shown). The silica concentration of the supply water W1 can be obtained by analyzing the water quality of the supply water W1 in advance. Further, in the supply water line L1, the silica concentration of the supply water W1 may be measured by a concentration sensor (not shown).

  In step ST302, the control unit 10 acquires the detected temperature value T of the supply water W1 from the temperature sensor 4.

  In step ST303, the control part 10 determines the silica solubility S with respect to water based on the acquired detected temperature value T. The relationship between temperature and silica solubility is stored in advance in a memory as a numerical table or a mathematical expression.

In step ST304, the control unit 10 calculates a reference concentration ratio (dissolution limit concentration ratio) N of silica in the concentrated water W3 based on the silica concentration C and the silica solubility S acquired or determined in step ST303. The standard concentration ratio N of silica can be obtained by the following formula (2).
N = S / C (2)

For example, if the silica concentration C is 20 mgSiO ₂ / L and the silica solubility S at 25 ° C. is 100 mgSiO ₂ / L, the reference concentration ratio N is “5”.

In step ST305, the control unit 10 calculates the first target concentration rate N ₁ ′ of silica in the concentrated water 3 based on the reference concentration rate N calculated in step ST304. First target concentration factor N ₁ silica _'can be determined by the following equation (3).
N ₁ ′ = α ₁ × N (3)

In the formula (3), α ₁ is a coefficient when operating at a concentration ratio exceeding the standard concentration ratio N, and its range is 2 to 3. The values of alpha ₁ is stored in the memory in advance.

In step ST306, the control unit 10 acquires the target flow rate value Q _p ′ of the permeated water W2. The target flow rate value Q _p ′ is the first target flow rate value acquired in step ST202 of FIG.

In step ST307, the control unit 10 performs the high recovery rate operation mode based on the first target concentration rate N ₁ ′ calculated in step ST304 and the target flow rate value Q _p ′ (first target flow rate value) acquired in step ST306. Drainage flow rate (hereinafter also referred to as “target drainage flow rate Q _d ′”). The target drainage flow rate Q _d ′ can be obtained by the following formula (4) in which the right side and the left side of formula (1) are shifted.
Q _d ′ = Q _p ′ / (N ₁ ′ −1) (4)

In step ST 308, the control unit 10, such that the actual waste water flow rate _{Q d} of concentrated water W3 is the target wastewater flow Qd' calculated in step ST 307, controls the opening and closing of the first drain valve 11 to the third drain valve 13 .

  In step ST309, the control part 10 controls the concentrated water recirculation | reflux valve 8 to a predetermined opening degree, and a process returns to step ST301. The opening degree of the concentrated water recirculation valve 8 is adjusted, for example, so that the flow rate of the concentrated water flowing through the concentrated water line L3 is about 3 to 5 times the flow rate of the permeated water per RO element. Is done.

  Next, temperature feedforward recovery rate control in the low recovery rate operation mode will be described. FIG. 5 is a flowchart showing a processing procedure when the control unit 10 executes the temperature feedforward recovery rate control in the low recovery rate operation mode. The process of the flowchart shown in FIG. 5 is repeatedly executed during operation in the low recovery rate operation mode. In FIG. 4, the processes in steps ST401 to ST404 are the same as the processes in steps ST301 to ST304 in FIG. 3, and thus the above description is used and the description is omitted here.

In step ST405, the control unit 10 calculates the second target concentration rate N ₂ ′ of silica in the concentrated water 3 based on the reference concentration rate N calculated in the previous step. The second target concentration magnification N ₂ ′ of silica can be obtained by the following formula (5).
N ₂ ′ = α ₂ × N (5)

In the formula (4), α ₂ is the coefficient used in the operation in the following concentration rate reference concentration factor N, the range is 0.5 to 1. The values of alpha ₂ is stored in the memory in advance.

In step ST406, the control unit 10 acquires the target drainage flow rate Q _d ′. The target drainage flow rate Q _d ′ is a value calculated in step ST307 in FIG.

In step ST407, the control unit 10 calculates a target flow rate value Q _p ′ (second target flow rate value) of the permeated water W2 in the low recovery rate operation mode. The second target flow rate value is calculated using the above-described equation (1) from the second target concentration rate N ₂ ′ calculated in step ST405 and the target drainage flow rate Q _d ′ acquired in step ST406.

In step ST 408, the control unit 10, the actual drainage flow _{Q d} are formed so that the target drainage flow _{Q d} 'acquired in step ST 406, controls the opening and closing of the first drain valve 11 to the third drain valve 13 of the concentrated water W3 To do.

  In step ST409, the control part 10 controls the concentrated water recirculation valve 8 to a closed state, and returns to step ST401.

  Next, the flushing operation mode 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 flushing operation mode. The process of the flowchart shown in FIG. 6 is executed in step ST109 shown in FIG.

In step ST501, the control part 10 controls the permeated water valve 7 to a closed state.
In step ST502, the control unit 10 controls the concentrated water recirculation valve 8 to be closed.

  In step ST503, the control unit 10 controls a predetermined valve among the first drain valve 11 to the third drain valve 13 to be in an open state. The number of drain valves to be controlled to the open state is determined in advance based on the flow rate of the supply water W1 necessary for effective flushing.

In step ST504, the control unit 10 acquires the drive frequency F _f in the flushing operation mode. This drive frequency F _f is, for example, a set value stored in advance in a memory.

In step ST505, the control unit 10 converts the value of the driving frequency F _f into a corresponding current value signal (4 to 20 mA).

  In step ST506, the control part 10 outputs the converted electric current value signal to the inverter 3, and the process of this flowchart is complete | finished. The inverter 3 supplies driving power converted to a frequency corresponding to the input current value signal to the pressurizing pump 2. As a result, the pressurizing pump 2 is driven at a rotational speed corresponding to the driving frequency input from the inverter 3.

  The supply water W1 supplied to the primary side of the RO membrane module 5 by the control of the permeated water valve 7, the concentrated water reflux valve 8, the first drain valve 11 to the third drain valve 13 and the pressurizing pump 2 is RO It flows on the surface of the membrane and is discharged from the concentrated water discharge line L4 as flushing washing waste water. Further, the permeated water W2 sent out from the secondary port of the RO membrane module 5 flows through the permeated water return line L6 by the valve opening operation of the safety valve 9, and is returned to the supply water line L1.

  According to the reverse osmosis membrane separation device 1 according to the above-described embodiment, for example, the following effects can be obtained.

  In the reverse osmosis membrane separation device 1 according to the present embodiment, the control unit 10 controls the flow rate of the supply water W1 so that the actual concentration ratio of silica in the concentrated water W3 becomes the first target concentration ratio exceeding the reference concentration ratio. A high recovery rate operation mode for controlling the drainage flow rate of the concentrated water W3 so that the actual drainage flow rate of the concentrated water W3 becomes the target drainage flow rate calculated based on the target flow rate value of the permeate and the first target concentration rate, In addition, the flow rate of the supply water W1 is controlled so that the actual concentration rate of silica in the concentrated water W3 is equal to or lower than the reference concentration rate, and the actual drainage flow rate of the concentrated water W3 is calculated in the high recovery rate operation mode. The low recovery rate operation mode for controlling the drainage flow rate of the concentrated water W3 so as to be the target drainage flow rate is alternately executed.

  According to this, the average recovery rate when the high recovery rate operation mode and the low recovery rate operation mode are executed alternately is the flow rate of the supply water W1 so that the actual concentration rate of silica in the concentrated water W3 becomes the reference concentration rate. It becomes higher than the recovery rate when controlling. Further, by executing the low recovery rate operation mode, even if scale nuclei are generated on the surface of the RO membrane during execution of the high recovery rate operation mode, they can be washed away before the scale nuclei grow.

  Therefore, even when the silica concentration of the supply water W1 is high, the recovery rate is improved while suppressing the precipitation of the silica-based scale by alternately executing the high recovery rate operation mode and the low recovery rate operation mode. Can do. As a result, since the amount of the concentrated water W3 to be discarded is minimized, it is possible to suppress an increase in fresh water generation cost.

  Moreover, in the reverse osmosis membrane separation apparatus 1 according to the present embodiment, the first time zone in which the high recovery rate operation mode is executed is set longer than the second time zone in which the low recovery rate operation mode is executed. Therefore, the average recovery rate improved by alternately executing the high recovery rate operation mode and the low recovery rate operation mode can be stably maintained.

  Moreover, in the reverse osmosis membrane separation apparatus 1 according to the present embodiment, the control unit 10 performs flow rate feedback water amount control when executing the high recovery rate operation mode and the low recovery rate operation mode. For this reason, the permeated water W2 having a stable flow rate can be supplied to the demand destination during both the high recovery rate operation mode and the low recovery rate operation mode.

  In the reverse osmosis membrane separation device 1 according to the present embodiment, the control unit 10 performs the concentrated water reflux valve 8 so that the concentrated water W3 does not flow through the concentrated water reflux line L5 when executing the low recovery rate operation mode. Is controlled to be closed. According to this, since the concentrated water W3 discharged from the RO membrane module 5 does not return to the primary side of the RO membrane module 5 in the low recovery rate operation mode, the scale nuclei generated on the surface of the RO membrane are efficiently washed away. be able to.

  Moreover, in the reverse osmosis membrane separation apparatus 1 according to the present embodiment, the control unit 10 executes the flushing operation mode once after executing the high recovery rate operation mode 10 times. In the flushing operation mode, the membrane surface is washed while the concentrated water W3 in the RO membrane module 5 is replaced with the supply water W1. For this reason, the film surface can be returned to a clean state in a short time.

  In the reverse osmosis membrane separation device 1 according to the present embodiment, a safety valve 9 is provided in the permeate return line L6. For this reason, in the flushing operation mode, when the in-pipe pressure of the permeate return line L6 becomes equal to or higher than the set pressure, the high-pressure permeate W2 is supplied to the low-pressure side (primary side of the pressurization pump 2) via the safety valve 9. Can be missed. Therefore, damage to the RO membrane due to excessive back pressure can be prevented.

  In the reverse osmosis membrane separation device 1 according to the present embodiment, the control unit 10 closes the concentrated water reflux valve 8 so that the concentrated water W3 does not flow through the concentrated water reflux line L5 when executing the flushing operation mode. The permeated water valve 7 is controlled to be closed so that the permeated water W2 does not flow through the permeated water line L2. For this reason, the supply water W1 can be effectively used as the wash water while suppressing the concentration of the supply water W1.

  Moreover, in the reverse osmosis membrane separation apparatus 1 according to the present embodiment, the control unit 10 executes the temperature feedforward recovery rate control in parallel with the flow rate feedback water amount control. For this reason, it is possible to more reliably suppress the precipitation of silica-based scale in the RO membrane module 5 while maintaining the average recovery rate improved by alternately executing the high recovery rate operation mode and the low recovery rate operation mode. it can.

  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 present embodiment, an example in which the first time period for executing the high recovery rate operation mode is set to 50 minutes and the second time period for executing the low recovery rate operation mode is set to 10 minutes has been described. Not only this example but each time slot | zone can be set arbitrarily. In that case, it is preferable to set so that the first time zone> the second time zone.

  In the present embodiment, the high recovery rate operation mode and the low recovery rate operation mode are alternately executed nine times, and after execution of the tenth high recovery rate operation mode, the tenth low recovery rate operation mode is executed. The example in which the flushing operation mode is executed once has been described. Not only this but the frequency | count of execution of each operation mode can be set arbitrarily.

  In the present embodiment, the example in which the third time zone in which the flushing operation mode is executed is set to 2 minutes has been described. However, the flushing operation mode may be continued until the electrical conductivity or the silica concentration of the cleaning wastewater discharged from the concentrated water line L3 is 1.1 times or less that of the supply water W1. Therefore, the third time zone in which the flushing operation mode is executed can be arbitrarily set within the range of this condition.

  Further, when the permeated water W2 obtained by the reverse osmosis membrane separation device 1 according to the present embodiment is supplied to a demand destination, the permeated water W2 may be supplied after being received by the treated water tank. Good. In the above configuration, the control unit 10 executes the flushing operation mode after detecting the fullness of the treated water tank after executing the high recovery rate operation mode 10 times. Thereby, the permeated water W2 can be supplied to the customer while the flushing operation mode is being executed.

  In this embodiment, the example which detects the temperature of the supply water W1 supplied to RO membrane module 5 with the temperature sensor 4 was demonstrated. Not only this but a temperature sensor may be provided in permeate line L2, and the temperature of permeate W2 obtained with RO membrane module 5 may be detected with a temperature sensor.

  In the present embodiment, the example in which the drainage flow rate of the concentrated water W3 is adjusted stepwise by selectively opening and closing the first drainage valve 11 to the third drainage valve 13 in the temperature feedforward recovery rate control has been described. Not limited to this, the concentrated water discharge line L4 may be branched and the proportional control valve may be provided in the concentrated water discharge line L4. In this case, the flow rate of the concentrated water W3 can be adjusted by transmitting a current value signal (for example, 4 to 20 mA) from the control unit 10 to the proportional control valve to control the valve opening.

  Moreover, in the structure provided with the proportional control valve, it is good also as a structure which provided the flow sensor in the concentrated water discharge line L4. In this case, the flow value detected by the flow sensor is input to the control unit 10 as a feedback value. Thereby, the actual waste water flow rate of the concentrated water W3 can be controlled more accurately.

DESCRIPTION OF SYMBOLS 1 Reverse osmosis membrane separator 2 Pressure pump 3 Inverter 4 Temperature sensor (temperature detection means)
5 RO membrane module (reverse osmosis membrane module)
6 Flow rate sensor (flow rate detection means)
7 Permeated water valve 8 Concentrated water return valve 9 Safety valve (pressure relief valve)
DESCRIPTION OF SYMBOLS 10 Control part 11 1st drain valve 12 2nd drain valve 13 3rd drain valve L1 Supply water line L2 Permeate water line L3 Concentrated water line L4 Concentrated water discharge line L5 Concentrated water recirculation line L6 Permeate return line W1 Supply water W2 Permeation Water W3 Concentrated water

Claims (6)

A reverse osmosis membrane module that separates supply water into permeate and concentrated water;
Temperature detection means for detecting the temperature of the feed water;
(I) Based on the silica concentration determined in advance from the silica concentration of the feed water obtained in advance and the temperature detected by the temperature detection means, the standard concentration ratio of silica in the concentrated water is calculated, and (ii) the silica concentration in the concentrated water The flow rate of the feed water supplied to the reverse osmosis membrane module is controlled so that the actual concentration rate becomes the first target concentration rate exceeding the reference concentration rate, and the preset target flow rate value of the permeated water and the first A high recovery rate operation mode that calculates the target drainage flow rate based on the target concentration rate and controls the drainage flow rate of the concentrated water so that the actual drainage flow rate of the concentrated water becomes the target drainage flow rate, and the actual concentration of silica in the concentrated water The flow rate of the feed water supplied to the reverse osmosis membrane module is controlled so that the magnification becomes a second target concentration rate equal to or less than the reference concentration rate, and the actual drainage flow rate of the concentrated water A control unit for performing a low recovery operation mode for controlling the drainage rate of the concentrated water so that the target water discharge flow rate calculated in the high recovery rate operation mode alternately,
A reverse osmosis membrane separation apparatus. In the control unit, the first time zone for executing the high recovery rate operation mode is set longer than the second time zone for executing the low recovery rate operation mode,
The reverse osmosis membrane separation apparatus according to claim 1. Flow rate detection means for detecting the flow rate of the permeated water,
A supply water line for supplying supply water to the reverse osmosis membrane module;
A pressurizing pump that is driven at a rotational speed according to the input driving frequency and pumps the feed water flowing through the feed water line 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 control unit calculates a driving frequency of the pressurizing pump so that a detected flow rate value detected by the flow rate detection unit becomes the target flow rate value, and outputs a current value signal corresponding to the calculated value of the driving frequency to the inverter. Output,
The reverse osmosis membrane separation apparatus according to claim 1 or 2. A permeate line for sending permeate to a customer,
A concentrated water line for delivering concentrated water from the reverse osmosis membrane module;
A concentrated water discharge line for discharging a part of the concentrated water flowing through the concentrated water line to the outside of the device;
A concentrated water reflux line for refluxing the remainder of the concentrated water flowing through the concentrated water line upstream of the pressurizing pump in the supply water line;
A concentrated water reflux valve capable of adjusting the flow rate of the concentrated water flowing through the concentrated water reflux line;
With
The control unit controls the concentrated water reflux valve so that the concentrated water does not flow through the concentrated water reflux line when the low recovery rate operation mode is executed.
The reverse osmosis membrane separation apparatus according to claim 3. The control unit executes the flushing operation mode for cleaning the primary side of the reverse osmosis membrane module at least once after the high recovery rate operation mode is executed a plurality of times.
The reverse osmosis membrane separator according to claim 4. A permeate valve provided in the permeate line;
A permeate return line for returning permeate sent to the permeate line to the upstream side of the pressurizing pump in the supply water line;
A pressure relief valve provided in the permeate return line;
With
The controller, when executing the flushing operation mode, (i) controls the concentrated water reflux valve so that the concentrated water does not flow through the concentrated water reflux line, and (ii) allows the permeate line to pass through the permeated water. Controlling the permeate valve so that the
The reverse osmosis membrane separator according to claim 5.

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