CN103237592B - The production method of reverse osmosis membrane separator, its starting method and permeate - Google Patents
The production method of reverse osmosis membrane separator, its starting method and permeate Download PDFInfo
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- CN103237592B CN103237592B CN201180058023.2A CN201180058023A CN103237592B CN 103237592 B CN103237592 B CN 103237592B CN 201180058023 A CN201180058023 A CN 201180058023A CN 103237592 B CN103237592 B CN 103237592B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/06—Energy recovery
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/12—Controlling or regulating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/24—Specific pressurizing or depressurizing means
- B01D2313/246—Energy recovery means
Abstract
In the reverse osmosis membrane separation device being equipped with energy recycle device, in order to avoid acting on the fast-changing situation of pressure on reverse osmosis membrane assembly when bringing into operation, thus effectively prevent the deterioration of reverse osmosis membrane physical property, the invention provides a kind of reverse osmosis membrane separation device, comprise: high-pressure pump (1), after a part of liquid to be treated is pressurized to predetermined value, be fed to reverse osmosis membrane assembly unit (2); Energy recycle device (3), utilizes the pressure of the concentrate of discharging from reverse osmosis membrane assembly (2), increases the pressure of remaining part liquid to be treated; Force (forcing) pump (4), the pressure of the liquid to be treated increased by energy recycle device (3) by pressure increases further to predetermined value, is fed to reverse osmosis membrane assembly unit (2) afterwards; Flow control valve (6), for regulating the flow of the liquid to be treated of discharging from high-pressure pump (1); Bypass runner, it walks around reverse osmosis membrane assembly unit (2) from flow control valve (6); And flow control valve (8), it is arranged in bypass runner, and regulates the by-pass ratio of liquid to be treated.
Description
Technical field
The present invention relates to a kind of reverse osmosis membrane separation device, for using reverse osmosis membrane assembly to the component separation making mixing or dissolve in a liquid.
Prior art
As shown in fig. 1, reverse osmosis membrane separation device for seawater desalination etc. constructs substantially in such a way, make after by high-pressure pump 1 liquid to be treated being pressurized to predetermined value, be fed to reverse osmosis membrane assembly unit 2, and by means of the counter-infiltration function of reverse osmosis membrane assembly unit 2, make the component separation be dissolved in liquid to be treated, thus, obtain permeate.
Incidentally, as shown in Figure 2, reverse osmosis membrane assembly unit 2 is the assembly units with one or more membrane module 20 (unit structure body), in each membrane module 20, the separating film element 22 (such as, spiral separation membrane component) respectively with reverse osmosis membrane (diffusion barrier) is set in cylindrical container 21.When the liquid to be treated such as seawater after pressurizeing is fed to the entrance 23 being positioned at membrane module 20 one end, by the diffusion barrier in separating film element 22 at different levels, solute component is separated, and the low pressure permeate after separation by central tube 24, and is discharged from permeate floss hole 25.High pressure concentrate is discharged from concentrate floss hole 26, and concentrate floss hole 26 is positioned at the other end, namely different from entrance 23 place end ends.
In this reverse osmosis membrane separation device, utilize the energy of the high pressure concentrate of discharging from this device, the power needed for high-pressure pump can be reduced.Such as, reversion pump, turbocharger or impulse turbine (Pelton turbine) is used to reclaim the energy of concentrate.Recently, the pressure-exchange formula energy recycle device having gradually adopted energy recovery efficiency higher.
Fig. 3 shows the general structure of the reverse osmosis membrane separation device being equipped with pressure-exchange formula energy recycle device.By liquid to be treated dispensing to high-pressure pump 1 and pressure-exchange formula energy recycle device 3.Make the liquid to be treated being fed to high-pressure pump 1 be pressurized to predetermined value, and be fed to reverse osmosis membrane assembly unit 2.The high pressure concentrate of discharging from reverse osmosis membrane assembly unit 2 is also fed to pressure-exchange formula energy recycle device 3.In pressure-exchange formula energy recycle device 3, by with high pressure concentrate positive energy exchange, liquid to be treated supercharging, to discharge from pressure-exchange formula energy recycle device 3.On the other hand, the energy of high pressure concentrate gives liquid to be treated, and its pressure reduces, and discharges as low pressure concentrate.The high pressure liquid to be treated of discharging from pressure-exchange formula energy recycle device 3 is fed to force (forcing) pump 4, it is made to be pressurized to the value identical with the liquid to be treated that pressure has been increased by high-pressure pump 1, itself and the liquid to be treated of discharging from high-pressure pump 1 are converged, is then fed to reverse osmosis membrane assembly unit 2.
Be equipped with common operation (starting) process of the above-mentioned reverse osmosis membrane separation device of pressure-exchange formula energy recycle device 3 as described below.First, liquid to be treated is only fed to pressure-exchange formula energy recycle device 3.By being arranged in the flow control valve 5 of to discharge from pressure-exchange formula energy recycle device 3 discharge pipe of concentrate, control the flow of liquid to be treated, to make it close to concentrated solution discharge during steady-state operation.Then, start force (forcing) pump 4, make liquid to be treated sequentially flow through pressure-exchange formula energy recycle device 3, force (forcing) pump 4, reverse osmosis membrane assembly unit 2 and pressure-exchange formula energy recycle device 3, then liquid to be treated is discharged.In this case, usually use variable frequency drives (inverter) to control the motor speed of force (forcing) pump 4, make the flow of the liquid to be treated of discharging from pressure-exchange formula energy recycle device 3 in this case also close to concentrated solution discharge during steady-state operation.In this stage, the pressure of liquid to be treated is lower, and is not carried out the separation of solute component by reverse osmosis membrane.
Then, high-pressure pump 1 is started.Liquid to be treated from being flowed out by starting high-pressure pump 1 is converged with the liquid to be treated flowing through force (forcing) pump 4, and is fed to reverse osmosis membrane assembly unit 2.The flow flowing through the liquid to be treated of force (forcing) pump 4 is subject to the control of flow control valve 5 and force (forcing) pump 4 motor speed, all the time to make it close to concentrated solution discharge during steady-state operation.So, with high-pressure pump 1 discharge liquid to be treated corresponding to the flow of liquid to be treated, namely, the liquid to be treated being fed to reverse osmosis membrane assembly unit 2 only has part when steady-state operation (its flow correspond to over concentrated solution discharge) to pass through reverse osmosis membrane, and be discharged to outside, the permeate after being separated as solute component.
In above-mentioned operation, usually high-pressure pump 1 is impelled to discharge liquid to be treated on a small quantity when starting, then, augmented flow gradually.By arranging that in high-pressure pump 1 discharge side flow control valve 6 is to regulate the flow (see Fig. 4) being fed to the liquid to be treated of reverse osmosis membrane assembly unit 2, or, control the motor speed (see Fig. 5) of high-pressure pump 1 with variable frequency drives (inverter) 7, perform this and control.
Incidentally, in order to obtain the permeate by reverse osmosis membrane, the osmotic pressure of inlet pressure greater than or equal to liquid to be treated of reverse osmosis membrane assembly unit 2 must be made.When liquid to be treated is such as seawater, the osmotic pressure of reverse osmosis membrane assembly unit 2 needs up to about 3 MPas (MPa).
When being equipped with the reverse osmosis membrane separation device of pressure-exchange formula energy recycle device 3 to bring into operation, until before starting high-pressure pump 1, the inlet pressure of reverse osmosis membrane assembly unit 2 pushes pressure (push-in pressure) close to liquid to be treated, and, such as, 0.3 MPa is according to appointment low to moderate.Once start high-pressure pump 1, because liquid to be treated does not discharge destination as mentioned above, even if open slightly flow control valve 6 to only have a little flowing to make liquid to be treated, the inlet pressure of reverse osmosis membrane assembly unit 2 is also made to increase to the osmotic pressure (about 3 MPa) of liquid to be treated.Therefore, the pressure of reverse osmosis membrane assembly unit 2 is made to increase fast.
If high pressure liquid to be treated (seawater etc.) is applied to suddenly reverse osmosis membrane assembly unit 2, due to brought compression shock, the physical property of the deteriorated reverse osmosis membrane of meeting.The deterioration of reverse osmosis membrane physical property is the factor that such as reverse osmosis membrane assembly unit 2 salt rejection rate reduces, and can reduce its reverse-osmosis treated ability.
For this problem, patent document 1 proposes a kind of method, by arranging bypass runner and the bypass flow control valve of walking around reverse osmosis membrane assembly unit in high-pressure pump discharge side, increases inlet pressure gradually.But, when being equipped with the reverse osmosis membrane separation device of pressure-exchange formula energy recycle device, by being arranged in from the flow control valve the discharge pipe of pressure-exchange formula energy recycle device discharge concentrate, control the flow of concentrate.Further, by using variable frequency drives (inverter) to control the motor speed of force (forcing) pump, the flow of the liquid to be treated of discharging from pressure-exchange formula energy recycle device is controlled, to make its close concentrated solution discharge when steady-state operation.So the unique channel avoiding inlet pressure to raise fast is, when starting high-pressure pump, the liquid to be treated of discharging from high-pressure pump is discharged by bypass flow control valve.
When controlling high-pressure pump by variable frequency drives, can start by the method.But in many cases, large reverse osmosis membrane separation device is not equipped with variable frequency drives, because the capacity motor of force (forcing) pump is comparatively large, therefore, need to use very expensive variable frequency drives.In this case, even if attempt to start high-pressure pump by opening bypass flow control valve completely, but occur open circuit (trip) owing to crossing to be loaded in high-pressure pump, this device self cannot start.If attempt to make the aperture of bypass flow control valve fixedly start high-pressure pump, by ensureing that the minimum discharge of high-pressure pump prevents the open circuit in high-pressure pump, high-pressure pump can be started.But, now, be applied to suddenly on reverse osmosis membrane assembly unit higher than pressure during steady-state operation, its inlet pressure cannot be made to increase gradually.
Background technology document
Patent document
Patent document 1:JP-A-2001-113136
Summary of the invention
Problem to be solved by this invention
The object of this invention is to provide a kind of reverse osmosis membrane separation device of simplification, it is equipped with energy recycle device, and the situation acting on the rapid change in pressure on reverse osmosis membrane assembly when bringing into operation can be avoided, thus, effectively prevent the deterioration of reverse osmosis membrane physical property.
The measure of dealing with problems
In order to achieve the above object, the invention is characterized in following (1) to (4) item.
(1) a reverse osmosis membrane separation device, comprising:
Pump A, after a part of liquid to be treated is pressurized to predetermined value, is fed to reverse osmosis membrane assembly;
Energy recycle device, utilizes the pressure of the concentrate of discharging from reverse osmosis membrane assembly, increases the pressure of remaining part liquid to be treated;
Pump B, has carried out the liquid to be treated after supercharging by by energy recycle device, after being pressurized to predetermined value further, has been fed to reverse osmosis membrane assembly;
Flow control valve A, for regulating the flow of the liquid to be treated of discharging from pump A;
Bypass runner, it walks around reverse osmosis membrane assembly from flow control valve A; And
Flow control valve B, it is arranged in bypass runner, and regulates the by-pass ratio of liquid to be treated.
(2) according to the reverse osmosis membrane separation device of (1), comprise further: pump C, for liquid to be treated is fed to pump A and energy recycle device; And frequency converter, for the rotating speed of control pump C.
(3) a kind of starting method of the reverse osmosis membrane separation device according to (1), the method comprises:
Before the described pump A of starting, regulate, make liquid to be treated sequentially flow through energy recycle device, pump B, reverse osmosis membrane assembly and energy recycle device, and discharge subsequently;
Then, start described pump A, the aperture of flow control valve A and flow control valve B is set to predetermined value simultaneously; And
Then, gradual control flow control valve A and flow control valve B, flow control valve B operates in closing direction, until the inlet pressure of reverse osmosis membrane assembly increases to predetermined value in opening direction operation to make flow control valve A.
(4) produce a method for permeate, comprising: start reverse osmosis membrane separation device by the reverse osmosis membrane separation device starting method according to (3), then, liquid to be treated is fed to reverse osmosis membrane assembly, to obtain permeate.
Invention effect
In the reverse osmosis membrane separation device being equipped with energy recycle device, the by-pass ratio of the present invention by using the flow control valve be arranged in bypass runner to regulate bypass runner, thus, when starting to start high-pressure pump, the pressure of the liquid to be treated being fed to reverse osmosis membrane assembly can be increased gradually, thus, effectively avoid the physical property deterioration of reverse osmosis membrane assembly in a simple manner decoupled.
Accompanying drawing explanation
[Fig. 1] Fig. 1 is the schematic diagram that a kind of reverse osmosis membrane separation device is shown;
[Fig. 2] Fig. 2 is the figure that reverse osmosis membrane assembly unit general structure is shown;
[Fig. 3] Fig. 3 is the schematic diagram that the reverse osmosis membrane separation device being equipped with pressure-exchange formula energy recycle device is shown;
[Fig. 4] Fig. 4 illustrates that shown high-pressure pump discharge side is furnished with the schematic diagram of flow control valve in figure 3;
[Fig. 5] Fig. 5 illustrates that high-pressure pump shown in Fig. 3 is equipped with the schematic diagram of variable frequency drives;
[Fig. 6] Fig. 6 is the schematic diagram of the reverse osmosis membrane separation device illustrated according to an embodiment of the present invention; And
[Fig. 7] Fig. 7 is the schematic diagram that reverse osmosis membrane separation device is according to another embodiment of the present invention shown.
Detailed description of the invention
Below, with reference to Fig. 6, illustrate according to reverse osmosis membrane separation device of the present invention.
Fig. 6 is schematic diagram, illustrates a kind of for making the reverse osmosis membrane separation device of mixing or dissolving component separation in a liquid.Liquid to be treated such as seawater is sent to high-pressure pump 1 and pressure-exchange formula energy recycle device 3.Make the liquid to be treated being fed to high-pressure pump 1 be pressurized to predetermined value (such as, about 6.0 MPas), and be fed to reverse osmosis membrane assembly unit 2.Be fed to by the liquid to be treated of sending and the high pressure concentrate of discharging from reverse osmosis membrane assembly unit 2 to pressure-exchange formula energy recycle device 3.In pressure-exchange formula energy recycle device 3, by with high pressure concentrate positive energy exchange, make liquid to be treated supercharging.Obtained high pressure liquid to be treated is discharged from pressure-exchange formula energy recycle device 3.On the other hand, the energy of high pressure concentrate gives liquid to be treated, and its pressure reduces, and discharges as low pressure concentrate.The high pressure liquid to be treated of discharging from pressure-exchange formula energy recycle device 3 is fed to force (forcing) pump 4, make to be pressurized to the value identical with the liquid to be treated that pressure is increased by high-pressure pump 1, make it converge with the liquid to be treated of discharging from high-pressure pump 1, and be fed to reverse osmosis membrane assembly unit 2.Receive the liquid to be treated that pressure has increased to predetermined value, reverse osmosis membrane assembly unit 2 produces the permeate of solute component separation by its counter-infiltration function, and also produces concentrate.
Flow control valve 6 is arranged, for controlling the flow of the liquid to be treated of discharging from high-pressure pump 1 in the discharge side of high-pressure pump 1.As mentioned above, the flow of liquid to be treated of discharging from high-pressure pump 1 is close to permeate flow.So, under usual operational circumstances, in order to control permeate flow, by the permeate flowmeter 9 be arranged on permeate pipeline and permeate flow controlling unit 10, flow-control is carried out to flow control valve 6.
The bypass runner of reverse osmosis membrane assembly unit 2 is provided around at the outlet side of flow control valve 6, and, bypass runner is arranged the flow control valve 8 for controlling by-pass ratio (bypass rate).By the flowmeter 11 and the high-pressure pump Minimum Flow Control unit 12 that are arranged in high-pressure pump 1 supply side, flow-control is carried out to flow control valve 8, to ensure the minimum discharge of high-pressure pump 1 when starting reverse osmosis membrane separation device.
The operation manipulation process of this reverse osmosis membrane separation device is as follows.First, liquid to be treated is only fed to pressure-exchange formula energy recycle device 3.By being arranged in the flow control valve 5 of to discharge from pressure exchange type energy recovery device 3 on the discharge pipe of concentrate, control the flow of liquid to be treated, to make it close to concentrated solution discharge during steady-state operation.Then, start force (forcing) pump 4, make liquid to be treated sequentially flow through pressure-exchange formula energy recycle device 3, force (forcing) pump 4, reverse osmosis membrane assembly unit 2 and pressure-exchange formula energy recycle device 3, then discharge.In this case, usually use variable frequency drives (inverter) to control the motor speed of force (forcing) pump 4, make the flow of the liquid to be treated of discharging from pressure-exchange formula energy recycle device 3 in this case also close to concentrated solution discharge during steady-state operation.In this stage, the pressure of liquid to be treated is lower, and reverse osmosis membrane does not carry out the separation of solute component.
Then, high-pressure pump 1 is started.In order to avoid high-pressure pump 1 is due to undue oscillation or be heated and damage, must the flow of high-pressure pump 1 be made after starting at once to increase to its minimum discharge.For this purpose, start high-pressure pump 1 when the aperture of flow control valve 6,8 is preset in predetermined value, thus, ensure minimum discharge.Specifically, when flow control valve 8 is opened completely, consider the pressure loss of flow control valve 6 primary side pipeline and the pressure loss of flow control valve 8, determine the initial opening of flow control valve 6.If start high-pressure pump 1 in this case, although the input side pressure of flow control valve 6 depends on the discharge characteristic of high-pressure pump 1, it becomes higher than rated pressure, and, there is the value of such as about 7.0 MPas.On the other hand, because make flow control valve 8 open completely, the inlet pressure of reverse osmosis membrane assembly unit 2 shows as and does not almost increase, and has the value of about 0.5 MPa, therefore, the liquid to be treated of discharging from high-pressure pump 1 is expelled to bypass side by flow control valve 8.
Then, in order to obtain permeate, according to the instruction from permeate flow controlling unit 10, open flow control valve 6 gradually.As a result, the discharge rate of high-pressure pump 1 is at once increased.But, due to the function of high-pressure pump Minimum Flow Control unit 12, the discharge rate being controlled high-pressure pump 1 by flow control valve 8 equals its minimum discharge to make it keep, and the discharge rate of high-pressure pump 1 in closing direction operation, and is remained in its minimum discharge by flow control valve 8.Flow control valve 6,8, respectively at opening direction and closing direction operation, by this, makes the inlet pressure of reverse osmosis membrane assembly unit 2 increase.Along with performing these two kinds controls step by step simultaneously, reverse osmosis membrane assembly unit inlet pressure is increased gradually.When the inlet pressure of reverse osmosis membrane assembly unit 2 reaches such as 3.0 MPa, permeate starts to discharge.
Even if after starting to discharge permeate, it is its minimum discharge that high-pressure pump Minimum Flow Control unit 12 also continues the flow-control of high-pressure pump 1.So the flow being expelled to the liquid to be treated of bypass side from flow control valve 8 reduces gradually, and, discharge the permeate corresponding with above-mentioned reduction flow from reverse osmosis membrane assembly unit 2.Finally, flow control valve 8 is made to close completely.
After this moment, the discharge rate of high-pressure pump 1 equal reverse osmosis membrane assembly unit 2 through liquid measure.Afterwards, permeate flow controlling unit 10 continues control flow check control valve 6 makes it open gradually, until permeate flowmeter 9 shows metered flow.When permeate flow reaches metered flow, the start-up function of this device completes.
Specifically, from starting high-pressure pump 1 to reaching the most handy about 300 seconds of metered flow moment or more the time through liquid measure.For this purpose, suitably performing a programme controls, the flow setting value of permeate flow controlling unit 10 is increased to metered flow gradually in 300 seconds, with the pace of change of limited flow control valve 6 (manipulation end), thus avoid the pressure that is exceedingly fast or changes in flow rate.
In said apparatus structure, high-pressure pump 1 and force (forcing) pump 4 respectively comprise centrifugal pump or plunger displacement pump, and flow control valve 6,8 respectively comprises ball valve, cage valve (cage valve) or needle-valve.The storage tank etc. that the liquid to be treated of bypass can be discharged from system or be back to for depositing liquid to be treated, to be again used as liquid to be treated.
In the above-mentioned methods, by means of permeate flow controlling unit 10 and high-pressure pump Minimum Flow Control unit 12, in certain preset time, the inlet pressure of reverse osmosis membrane assembly unit 2 is made to increase.Alternately, as shown in Figure 7, pressure transmitter 13 is arranged at the input side of reverse osmosis membrane assembly unit 2, based on the force value of the liquid to be treated obtained by pressure transmitter 13, on permeate flow controlling unit 10, serials control (cascade control) is performed by inlet pressure control unit 14, also can the aperture of control flow check control valve 6.
Depend on quality and the temperature of liquid to be treated, the input pressure needed for reverse osmosis membrane assembly unit 2 is different.In conventional operation, in the following manner, the cooperation to reverse osmosis membrane assembly unit 2 required input pressure change (increase or reduce) is made.When the input pressure needed for reverse osmosis membrane assembly unit 2 increases, according to the instruction from permeate flow controlling unit 10, the aperture of augmented flow control valve 6.On the contrary, when the input pressure needed for reverse osmosis membrane assembly unit 2 reduces, the aperture of flow control valve 6 is reduced.
According to the viewpoint that dynamic power consumes, if the aperture of flow control valve 6 is close to opening completely, there is not useless dynamic power consumption.On the other hand, the aperture of flow control valve 6, lower than opening completely, means: flow control valve 6 consumed energy, namely, has occurred useless dynamic power consumption in high-pressure pump 1.This dynamic power is corresponding to the device running such as high-pressure pump 1 electric power ((dynamic power)=(electric energy)) used.In desalination unit, the reduction of power consumption is key factor.So, in order to reduce this useless power consumption, preferably, be equipped with the liquid to be treated supply pump 15 (see Fig. 7) with variable frequency drives (inverter) 7.
If do not consider less loine pressure loss, can by the discharge pressure of high-pressure pump 1 is added supply pump 15 discharge pressure, therefrom deduct the pressure corresponding with the dynamic power loss of flow control valve 6 again, calculate the necessary inlet pressure of reverse osmosis membrane assembly unit 2.Now, when the normal discharge pressure of such as supply pump 15 is 1.0 MPas, and when the normal discharge pressure of high-pressure pump 1 is 7.0 MPa, suppose that the necessary inlet pressure of reverse osmosis membrane assembly unit 2 is 7.5 MPas.In this case, the dynamic power corresponding to 0.5 MPa should be lost in flow control valve 6.If supply pump 15 is equipped with variable frequency drives (inverter) 7, the frequency of supply of supply pump 15 is fed to by conversion, regulate the output speed of supply pump 15, the discharge pressure of supply pump 15 is decreased to 0.5 MPa from rated value 1.0 MPa, useless power consumption can be avoided.This method makes in flow control valve 6, invalidly to consume dynamic electric energy.As illustrative above, may occur such a case, liquid to be treated supply pump 15 is equipped with variable frequency drives (inverter) 7 to avoid useless dynamic power consumption.Equally in this case, above-mentioned starting method and method of operating (its use traffic control valve 6 and the flow control valve 5 be arranged in bypass conduit) are all effective.
Description of reference numerals
1: high-pressure pump (pump A)
2: reverse osmosis membrane assembly unit
3: pressure-exchange formula energy recycle device
4: force (forcing) pump (pump B)
5: flow control valve
6: flow control valve (flow control valve A)
7: variable frequency drives (inverter)
8: flow control valve (flow control valve B)
9: permeate flowmeter
10: permeate flow controlling unit
11: flowmeter
12: high-pressure pump Minimum Flow Control unit
13: pressure transmitter
14: inlet pressure control unit
15: supply pump (pump C)
20: membrane module
21: cylindrical container
22: separating film element
23: entrance
24: central tube
25: permeate is discharged
26: concentrate discharges
Claims (4)
1. a reverse osmosis membrane separation device, comprising:
Pump A, after a part of liquid to be treated is pressurized to predetermined value, is fed to reverse osmosis membrane assembly;
Energy recycle device, utilizes the pressure of the concentrate of discharging from described reverse osmosis membrane assembly, increases the pressure of remaining part liquid to be treated;
Pump B, has carried out the liquid to be treated after supercharging by by described energy recycle device, after being pressurized to predetermined value further, is fed to described reverse osmosis membrane assembly;
Flow control valve A, regulates the flow of the liquid to be treated of discharging from described pump A;
Bypass runner, it walks around described reverse osmosis membrane assembly from described flow control valve A; And
Flow control valve B, it is arranged in described bypass runner, and regulates the by-pass ratio of liquid to be treated with the minimum flow of holding pump A,
Described reverse osmosis membrane separation device also comprises and is arranged in permeate flowmeter on permeate pipeline and permeate flow controlling unit, wherein, by permeate flowmeter and permeate flow controlling unit, flow-control is carried out to described flow control valve A, make it possible to the flow of the liquid to be treated of discharging from described pump A based on permeate Flow-rate adjustment.
2. reverse osmosis membrane separation device according to claim 1, comprises: pump C further, for liquid to be treated being fed to described pump A and described energy recycle device; And frequency converter, for controlling the rotating speed of described pump C.
3. a starting method for reverse osmosis membrane separation device according to claim 1, described method comprises:
Before described pump A starts, regulate, make liquid to be treated sequentially flow through described energy recycle device, described pump B, described reverse osmosis membrane assembly and described energy recycle device, and discharge subsequently;
Then, start described pump A, the aperture of described flow control valve A and described flow control valve B is set to predetermined value simultaneously; And
Then, flow control valve A described in gradual control and described flow control valve B, by permeate flow-control, make described flow control valve A in opening direction operation and, controlled by the minimum flow of described pump A, flow control valve B operates in closing direction, until the inlet pressure of described reverse osmosis membrane assembly increases to predetermined value.
4. produce a method for permeate, comprising: start described reverse osmosis membrane separation device by reverse osmosis membrane separation device according to claim 3 starting method, then, liquid to be treated is fed to described reverse osmosis membrane assembly, to obtain permeate.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2010-269054 | 2010-12-02 | ||
| JP2010269054 | 2010-12-02 | ||
| PCT/JP2011/076357 WO2012073693A1 (en) | 2010-12-02 | 2011-11-16 | Reverse osmosis membrane separator, start-up method therefor, and method for producing permeate |
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| CN103237592A CN103237592A (en) | 2013-08-07 |
| CN103237592B true CN103237592B (en) | 2015-10-14 |
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| JP (1) | JP5974484B2 (en) |
| CN (1) | CN103237592B (en) |
| AU (1) | AU2011338029A1 (en) |
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| JP2014133189A (en) * | 2013-01-08 | 2014-07-24 | Hitachi Ltd | Desalination system |
| JP6033118B2 (en) * | 2013-02-26 | 2016-11-30 | 三菱重工業株式会社 | Reverse osmosis membrane device |
| CN104341050B (en) * | 2013-07-26 | 2016-08-10 | 中国电力工程顾问集团有限公司 | A kind of seawater desalination system and method |
| CN105517961B (en) * | 2013-09-11 | 2018-10-02 | 株式会社荏原制作所 | Seawater desalination system |
| WO2015146639A1 (en) * | 2014-03-27 | 2015-10-01 | 株式会社 荏原製作所 | Energy recovery system |
| GB2540603A (en) | 2015-07-23 | 2017-01-25 | Ide Technologies Ltd | Imroved reverse osmotic process for cleaning water |
| CN107879421A (en) * | 2016-09-29 | 2018-04-06 | 东丽先端材料研究开发（中国）有限公司 | A kind of operation method of purifier and purifier |
| KR102180787B1 (en) | 2017-01-09 | 2020-11-23 | 베올리아 워터 솔루션스 앤드 테크놀로지스 서포트 | Water treatment system and method by reverse osmosis or nanofiltration |
| CN114790059B (en) * | 2022-04-11 | 2023-08-08 | 倍杰特集团股份有限公司 | Concentrating and filtering device and method for synthetic ammonia and ethylene glycol wastewater concentrated water |
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| JP2004081913A (en) * | 2002-08-23 | 2004-03-18 | Hitachi Zosen Corp | Sea water desalinating method by reverse osmosis |
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| CN1721048A (en) * | 2005-06-17 | 2006-01-18 | 中国科学院广州能源研究所 | Strong brine energy recovery device based on reverse osmosis desalination technology |
| CN101000336A (en) * | 2007-01-11 | 2007-07-18 | 上海交通大学 | Dynamic investigating method for performance of reverse osmosis antisludging agent |
| CN101782095A (en) * | 2010-03-12 | 2010-07-21 | 国家海洋局天津海水淡化与综合利用研究所 | Differential energy recovery device and method for seawater desalination system |
| JP2010253344A (en) * | 2009-04-22 | 2010-11-11 | Ebara Corp | Positive displacement energy recovery apparatus |
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2011
- 2011-11-16 JP JP2011550764A patent/JP5974484B2/en not_active Expired - Fee Related
- 2011-11-16 WO PCT/JP2011/076357 patent/WO2012073693A1/en active Application Filing
- 2011-11-16 AU AU2011338029A patent/AU2011338029A1/en not_active Abandoned
- 2011-11-16 CN CN201180058023.2A patent/CN103237592B/en not_active Expired - Fee Related
- 2011-12-01 TW TW100144093A patent/TW201231152A/en unknown
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS574286A (en) * | 1980-06-11 | 1982-01-09 | Agency Of Ind Science & Technol | Method for starting of desalting device by reverse-osmosis method provided with energy recovery device |
| JPH01123605A (en) * | 1987-11-06 | 1989-05-16 | Nkk Corp | Method for recovering energy in brine desalting plant using reverse-osmosis membrane |
| JPH07284637A (en) * | 1994-04-20 | 1995-10-31 | Toshiba Corp | Membrane module system |
| CN1132108A (en) * | 1994-10-12 | 1996-10-02 | 东丽株式会社 | Reverse osmosis separating unit and its method |
| JP2001113136A (en) * | 1999-10-20 | 2001-04-24 | Toray Ind Inc | Reverse osmosis treating device and water production method |
| CN1486214A (en) * | 2000-11-21 | 2004-03-31 | ֱ | Method and device for desalting water |
| JP2004081913A (en) * | 2002-08-23 | 2004-03-18 | Hitachi Zosen Corp | Sea water desalinating method by reverse osmosis |
| CN1721048A (en) * | 2005-06-17 | 2006-01-18 | 中国科学院广州能源研究所 | Strong brine energy recovery device based on reverse osmosis desalination technology |
| CN101000336A (en) * | 2007-01-11 | 2007-07-18 | 上海交通大学 | Dynamic investigating method for performance of reverse osmosis antisludging agent |
| JP2010253344A (en) * | 2009-04-22 | 2010-11-11 | Ebara Corp | Positive displacement energy recovery apparatus |
| CN101782095A (en) * | 2010-03-12 | 2010-07-21 | 国家海洋局天津海水淡化与综合利用研究所 | Differential energy recovery device and method for seawater desalination system |
Also Published As
| Publication number | Publication date |
|---|---|
| JPWO2012073693A1 (en) | 2014-05-19 |
| AU2011338029A1 (en) | 2013-06-20 |
| CN103237592A (en) | 2013-08-07 |
| JP5974484B2 (en) | 2016-08-23 |
| WO2012073693A1 (en) | 2012-06-07 |
| TW201231152A (en) | 2012-08-01 |
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