CN103237592A - Reverse osmosis membrane separator, start-p method therefor, and method for producing permeate - Google Patents
Reverse osmosis membrane separator, start-p method therefor, and method for producing permeate Download PDFInfo
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- CN103237592A CN103237592A CN2011800580232A CN201180058023A CN103237592A CN 103237592 A CN103237592 A CN 103237592A CN 2011800580232 A CN2011800580232 A CN 2011800580232A CN 201180058023 A CN201180058023 A CN 201180058023A CN 103237592 A CN103237592 A CN 103237592A
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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
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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
- B01D61/12—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
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Abstract
In order to prevent sudden changes in pressure on a reverse osmosis membrane module when starting operation and effectively prevent the deterioration of physical properties of a reverse osmosis membrane, a reverse osmosis membrane separator provided with an energy recovery unit is characterized by being provided with: a high pressure pump (1) for raising a portion of a solution to be treated to a prescribed pressure and supplying same to the reverse osmosis membrane module unit (2); the energy recovery unit (3) for raising the pressure of a remaining treated solution by using the pressure of a concentrated water discharged from the reverse osmosis membrane module (2); a pressurizing pump (4) for further raising the treated solution pressurized in the energy recovery unit (3), to a prescribed pressure and supplying same to the reverse osmosis membrane module unit (2); a flow-regulating valve (6) for adjusting the flow of the treated solution discharged from the high pressure pump (1); a bypass flow channel from the flow-regulating valve (6) for bypassing the reverse osmosis membrane module unit (2); and a flow-regulating valve (8) that is provided in the bypass flow channel and adjusts the bypass volume of the treated solution.
Description
Technical field
The present invention relates to a kind of reverse osmosis membrane separation device, be used for using reverse osmosis membrane assembly to make the component separation of mixing or being dissolved in liquid.
Prior art
As shown in fig. 1, the reverse osmosis membrane separation device that is used for seawater desalination etc. is structure in such a way basically, make after by high-pressure pump 1 processed liquid being pressurized to predetermined value, it is fed to reverse osmosis membrane assembly unit 2, and the counter-infiltration function by means of reverse osmosis membrane assembly unit 2, make the component separation that is dissolved in the processed liquid, thereby, obtain to see through liquid.
Incidentally, as shown in Figure 2, reverse osmosis membrane assembly unit 2 is the assembly units with one or more membrane modules 20 (unit structure body), in each membrane module 20, the separating film element 22 (for example, spiral separation membrane component) that respectively has reverse osmosis membrane (diffusion barrier) is set in cylindrical container 21.Processed liquid after pressurization is when for example seawater is fed to the entrance 23 that is positioned at membrane module 20 1 ends, make the solute component separation by the diffusion barrier in the separating film elements 22 at different levels, and the low pressure of after separating sees through liquid by central tube 24, and discharges from seeing through liquid floss hole 25.The high pressure concentrate is discharged from concentrate floss hole 26, and concentrate floss hole 26 is positioned at the other end, just the end different with entrance 23 place ends.
In this reverse osmosis membrane separation device, utilize from the energy of the high pressure concentrate of this device discharge, can reduce the required power of high-pressure pump.For example, use counter-rotating pump, turbocharger or impulse turbine (Pelton turbine) to reclaim the energy of concentrate.Recently, gradually adopted the higher pressure-exchange formula energy recycle device of energy recovery efficiency.
Fig. 3 shows the general structure of the reverse osmosis membrane separation device that is equipped with pressure-exchange formula energy recycle device.Processed liquid is sent to high-pressure pump 1 and pressure-exchange formula energy recycle device 3.Make the processed liquid that is fed to high-pressure pump 1 be pressurized to predetermined value, and it is fed to reverse osmosis membrane assembly unit 2.The 2 high pressure concentrates of discharging also are fed to pressure-exchange formula energy recycle device 3 from the reverse osmosis membrane assembly unit.In pressure-exchange formula energy recycle device 3, by with high pressure concentrate positive energy exchange, processed liquid supercharging is to discharge from pressure-exchange formula energy recycle device 3.On the other hand, the energy of high pressure concentrate has been given processed liquid, and its pressure reduces, and discharges as the low pressure concentrate.The processed liquid of high pressure of discharging from pressure-exchange formula energy recycle device 3 is fed to force (forcing) pump 4, make it be pressurized to the processed liquid phase value together that has been increased by high-pressure pump 1 with pressure, itself and the processed liquid of discharging from high-pressure pump 1 are converged, be fed to reverse osmosis membrane assembly unit 2 then.
Be equipped with common operation (starting) process of above-mentioned reverse osmosis membrane separation device of pressure-exchange formula energy recycle device 3 as described below.At first, processed liquid only is fed to pressure-exchange formula energy recycle device 3.Discharge flow control valve 5 on the discharge pipe of concentrates by being arranged in from pressure-exchange formula energy recycle device 3, control the flow of processed liquid, so that its concentrated solution discharge during near steady-state operation.Then, starting force (forcing) pump 4 makes processed liquid 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 in regular turn, then processed liquid is discharged.Under this state, use the motor speed of variable frequency drives (inverter) control force (forcing) pump 4 usually, the concentrated solution discharge when making under this state the flow of the processed liquid of discharging from pressure-exchange formula energy recycle device 3 also near steady-state operation.In this stage, the pressure of processed liquid is lower, and does not carry out the separation of solute composition by reverse osmosis membrane.
Then, starting high-pressure pump 1.Make from the processed liquid that is flowed out by starting high-pressure pump 1 and the processed liquid that flows through force (forcing) pump 4 and converge, and it is fed to reverse osmosis membrane assembly unit 2.The flow that flows through the processed liquid of force (forcing) pump 4 is subjected to the control of flow control valve 5 and force (forcing) pump 4 motor speeds all the time, so that its concentrated solution discharge during near steady-state operation.So, the processed liquid corresponding with the flow of the high-pressure pump 1 processed liquid of discharging, just, the processed liquid that is fed to reverse osmosis membrane assembly unit 2 has only part when surpassing steady-state operation (its flow corresponding to concentrated solution discharge) to pass through reverse osmosis membrane, and be discharged to the outside, as the liquid that sees through after the solute component separation.
Above-mentioned in service, the time impel in beginning usually that high-pressure pump 1 is a small amount of discharges processed liquid, then, augmented flow gradually.Arrange that by discharge side at high-pressure pump 1 flow control valve 6 is fed to the flow (referring to Fig. 4) of the processed liquid of reverse osmosis membrane assembly unit 2 with adjusting, perhaps, with the motor speed (referring to Fig. 5) of variable frequency drives (inverter) 7 control high-pressure pumps, carry out this control.
Incidentally, in order to obtain the liquid that sees through by reverse osmosis membrane, must make the inlet pressure of reverse osmosis membrane assembly unit 2 be greater than or equal to the osmotic pressure of processed liquid.Be under the situation of for example seawater at processed liquid, the osmotic pressure of reverse osmosis membrane assembly unit 2 need be up to about 3 MPas (MPa).
When the reverse osmosis membrane separation device that is equipped with pressure-exchange formula energy recycle device 3 brings into operation, before starting high-pressure pump 1, the inlet pressure of reverse osmosis membrane assembly unit 2 pushes pressure (push-in pressure) near processed liquid, and, for example, be low to moderate 0.3 MPa according to appointment.In case starting high-pressure pump 1, because processed liquid does not discharge the destination as mentioned above, even open flow control valve 6 slightly so that processed liquid has only a little to flow, also make the inlet pressure of reverse osmosis membrane assembly unit 2 increase to the osmotic pressure (about 3 MPas) of processed liquid.Therefore, the pressure of reverse osmosis membrane assembly unit 2 is increased fast.
If the processed liquid of high pressure (seawater etc.) is applied to reverse osmosis membrane assembly unit 2 suddenly, since the compression shock that brings, the physical property of meeting deterioration reverse osmosis membrane.The deterioration of reverse osmosis membrane physical property is the factor that reduces of reverse osmosis membrane assembly unit 2 salt rejection rates for example, and can reduce its reverse-osmosis treated ability.
At this problem, patent documentation 1 proposes a kind of method, arranges bypass runner and the bypass flow control valve of walking around the reverse osmosis membrane assembly unit by discharging side at high-pressure pump, increases inlet pressure gradually.Yet, under the situation of the reverse osmosis membrane separation device that is equipped with pressure-exchange formula energy recycle device, discharge flow control valve on the discharge pipe of concentrate, the flow of control concentrate by being arranged in from pressure-exchange formula energy recycle device.And, by using the motor speed of variable frequency drives (inverter) control force (forcing) pump, the flow of the processed liquid of discharging from pressure-exchange formula energy recycle device is controlled, so that it approaches the concentrated solution discharge when steady-state operation.So the unique channel of avoiding inlet pressure to raise fast is when the starting high-pressure pump, to make from the processed liquid of high-pressure pump discharge and discharge by the bypass flow control valve.
Under the situation by variable frequency drives control high-pressure pump, can start with the method.Yet in many cases, large-scale reverse osmosis membrane separation device is not equipped with variable frequency drives, because the capacity motor of force (forcing) pump is bigger, therefore, needs to use very expensive variable frequency drives.In this case, even attempt to start high-pressure pump by opening the bypass flow control valve fully, but occur open circuit (trip) in the high-pressure pump owing to crossing to be loaded in, this device self can't start.If attempt to make the aperture of bypass flow control valve fixedly to start high-pressure pump, prevent opening circuit in the high-pressure pump by the minimum discharge that guarantees high-pressure pump, can start high-pressure pump.Yet at this moment, the pressure when being higher than steady-state operation is applied to suddenly on the reverse osmosis membrane assembly unit, and its inlet pressure is increased gradually.
The background technology document
Patent documentation
Patent documentation 1:JP-A-2001-113136
Summary of the invention
Problem to be solved by this invention
The reverse osmosis membrane separation device that the purpose of this invention is to provide a kind of simplification, it is equipped with energy recycle device, and can avoid when bringing into operation, acting on the situation of the rapid change in pressure on the reverse osmosis membrane assembly, thereby, 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 kind of reverse osmosis membrane separation device comprises:
Pump A, the processed liquid of a part is pressurized to predetermined value after, be fed to reverse osmosis membrane assembly;
Energy recycle device utilizes from the pressure of the concentrate of reverse osmosis membrane assembly discharge, increases the pressure of the processed liquid of remaining part;
Pump B will carry out the processed liquid after the supercharging by energy recycle device, after further being pressurized to predetermined value, be fed to reverse osmosis membrane assembly;
Flow control valve A is used for regulating the flow from the processed liquid of pump A discharge;
The bypass runner, it walks around reverse osmosis membrane assembly from flow control valve A; And
Flow control valve B, it is arranged in the bypass runner, and regulates the by-pass ratio of processed liquid.
(2) according to the reverse osmosis membrane separation device of (1), further comprise: pump C is used for processed liquid is fed to pump A and energy recycle device; And frequency converter, for the rotating speed of control pump C.
(3) starting method of the reverse osmosis membrane separation device of a kind of basis (1), this method comprises:
Before the described pump A of starting, regulate, make processed liquid flow through energy recycle device, force (forcing) pump, reverse osmosis membrane assembly and energy recycle device in regular turn, and discharge subsequently;
Then, start described pump A, the aperture with flow control valve A and flow control valve B is set to predetermined value simultaneously; And
Then, control flow control valve A and flow control valve B step by step, make that flow control valve B operates in closing direction flow control valve A in opening direction operation, increase to predetermined value until the inlet pressure of reverse osmosis membrane assembly.
(4) a kind of generation sees through the method for liquid, comprising: the reverse osmosis membrane separation device starting method starting reverse osmosis membrane separation device by according to (3) then, is fed to reverse osmosis membrane assembly with processed liquid, to obtain seeing through liquid.
The invention effect
In being equipped with the reverse osmosis membrane separation device of energy recycle device, the present invention is arranged in the by-pass ratio that the flow control valve in the bypass runner is regulated the bypass runner by use, thereby, when beginning to start high-pressure pump, can increase the pressure of the processed liquid that is fed to reverse osmosis membrane assembly gradually, thereby, avoid the physical property deterioration of reverse osmosis membrane assembly effectively with plain mode.
Description of drawings
[Fig. 1] Fig. 1 illustrates a kind of reverse osmosis membrane separation schematic representation of apparatus;
[Fig. 2] Fig. 2 is the figure that the general structure in reverse osmosis membrane assembly unit is shown;
[Fig. 3] Fig. 3 illustrates the reverse osmosis membrane separation schematic representation of apparatus that is equipped with pressure-exchange formula energy recycle device;
[Fig. 4] Fig. 4 is illustrated in high-pressure pump shown in Fig. 3 to discharge the schematic diagram that side is furnished with flow control valve;
[Fig. 5] Fig. 5 illustrates the schematic diagram that high-pressure pump shown in Figure 3 is equipped with variable frequency drives;
[Fig. 6] Fig. 6 is the reverse osmosis membrane separation schematic representation of apparatus that illustrates according to an embodiment of the present invention; And
[Fig. 7] Fig. 7 illustrates reverse osmosis membrane separation schematic representation of apparatus according to another embodiment of the present invention.
The specific embodiment
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 that mixes or be dissolved in the component separation of liquid.With processed liquid for example seawater send to high-pressure pump 1 and pressure-exchange formula energy recycle device 3.Make the processed liquid that is fed to high-pressure pump 1 be pressurized to predetermined value (for example, about 6.0 MPas), and it is fed to reverse osmosis membrane assembly unit 2.Present the processed liquid sent and the 2 high pressure concentrates of discharging from the reverse osmosis membrane assembly unit 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 processed liquid supercharging.The processed liquid of resulting high pressure is discharged from pressure-exchange formula energy recycle device 3.On the other hand, the energy of high pressure concentrate has been given processed liquid, and its pressure reduces, and discharges as the low pressure concentrate.To be fed to force (forcing) pump 4 from the processed liquid of high pressure that pressure-exchange formula energy recycle device 3 is discharged, make and be pressurized to the processed liquid phase value together that is increased by high-pressure pump 1 with pressure, itself and the processed liquid of discharging from high-pressure pump 1 are converged, and be fed to reverse osmosis membrane assembly unit 2.Receive pressure and increased to the processed liquid of predetermined value, reverse osmosis membrane assembly unit 2 produces the liquid that sees through of solute component separation by its counter-infiltration function, and also produces concentrate.
Discharge side at high-pressure pump 1 is arranged flow control valve 6, is used for control from the flow of the processed liquid of high-pressure pump 1 discharge.As mentioned above, the flow of the processed liquid of discharging from high-pressure pump 1 approaches and sees through flow quantity.So, under the operational circumstances, in order to control through flow quantity, by being arranged in through seeing through flow quantity meter 9 and seeing through flow quantity control module 10 on the liquid pipeline, flow control valve 6 is carried out flow-control usually.
Walk around the bypass runner of reverse osmosis membrane assembly unit 2 in the outlet side setting of flow control valve 6, and, the flow control valve 8 that is used for control by-pass ratio (bypass rate) arranged at the bypass runner.By the flowmeter 11 that is arranged in high-pressure pump 1 supply side and high-pressure pump Minimum Flow Control unit 12, flow control valve 8 is carried out flow-control, when starting the reverse osmosis membrane separation device, to guarantee the minimum discharge of high-pressure pump 1.
It is as follows that process is controlled in the operation of this reverse osmosis membrane separation device.At first, processed liquid only is fed to pressure-exchange formula energy recycle device 3.Discharge flow control valve 5 on the discharge pipe of concentrates by being arranged in from pressure-exchange formula energy recycle device 3, control the flow of processed liquid, so that its concentrated solution discharge during near steady-state operation.Then, starting force (forcing) pump 4 makes processed liquid 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 in regular turn, discharges then.Under this state, use the motor speed of variable frequency drives (inverter) control force (forcing) pump 4 usually, the concentrated solution discharge when making under this state the flow of the processed liquid of discharging from pressure-exchange formula energy recycle device 3 also near steady-state operation.In this stage, the pressure of processed liquid is lower, and reverse osmosis membrane does not carry out the separation of solute composition.
Then, starting high-pressure pump 1.Owing to undue oscillation or be heated and damage, must after starting, make the flow of high-pressure pump 1 increase to its minimum discharge at once for fear of high-pressure pump 1.For this purpose, starting high-pressure pump 1 under the situation that flow control valve 6,8 aperture is preset in predetermined value, thereby, guarantee minimum discharge.Particularly, under the situation that flow control valve 8 is opened fully, consider the pressure loss of flow control valve 6 primary side pipelines and the pressure loss of flow control valve 8, determine the initial opening of flow control valve 6.If starting high-pressure pump 1 under this state, although the input side pressure of flow control valve 6 depends on the discharge characteristic of high-pressure pump 1, it becomes and is higher than rated pressure, and, have for example value of about 7.0 MPas.On the other hand, because flow control valve 8 is opened fully, the inlet pressure of reverse osmosis membrane assembly unit 2 shows as almost and does not increase, and has the value of about 0.5 MPa, therefore, will be expelled to the bypass side by flow control valve 8 from the processed liquid that high-pressure pump 1 is discharged.
Then, in order to obtain seeing through liquid, according to from the instruction that sees through flow quantity control module 10, open flow control valve 6 gradually.As a result, increased the discharge rate of high-pressure pump 1 at once.Yet, because the function of high-pressure pump Minimum Flow Control unit 12, so that its maintenance equals its minimum discharge, flow control valve 8 is in the closing direction operation by the discharge rate of flow control valve 8 control high-pressure pumps 1, and the discharge rate of high-pressure pump 1 is remained in its minimum discharge.Flow control valve 6,8 by this, increases the inlet pressure of reverse osmosis membrane assembly unit 2 respectively at opening the operation of direction and closing direction.Along with carrying out this two kinds of 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 for example reaches 3.0 MPas, see through liquid and begin to discharge.
Even beginning to discharge through after the liquid, high-pressure pump Minimum Flow Control unit 12 also continues the flow-control of high-pressure pump 1 is its minimum discharge.So the flow that is expelled to the processed liquid of bypass side from flow control valve 8 reduces gradually, and, from the reverse osmosis membrane assembly unit 2 discharge with above-mentioned reduce flow corresponding through liquid.At last, flow control valve 8 cuts out fully.
After this moment, the discharge rate of high-pressure pump 1 equals the liquid measure that sees through of reverse osmosis membrane assembly unit 2.Afterwards, see through flow quantity control module 10 continuation control flow control valves 6 it is opened gradually, show metered flows until seeing through flow quantity meter 9.When reaching metered flow through flow quantity, the start-up function of this device is finished.
Particularly, begin to reach the metered flow moment the most handy about 300 seconds or the more time to seeing through liquid measure from starting high-pressure pump 1.For this purpose, suitable is performing a programme control, in 300 seconds, will increase to metered flow gradually through the flow setting value of flow quantity control module 10, with the pace of change of limited flow control valve 6 (manipulation end), thereby avoid the pressure or the changes in flow rate that are exceedingly fast.
In the 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 processed liquid of bypass can be discharged or be back to be used to the storage tank of depositing processed liquid etc. from system, with again as processed liquid.
In said method, by means of seeing through flow quantity control module 10 and high-pressure pump Minimum Flow Control unit 12, the inlet pressure of reverse osmosis membrane assembly unit 2 is increased.Alternately, as shown in Figure 7, input side in reverse osmosis membrane assembly unit 2 is arranged pressure transmitter 13, force value based on the processed liquid that is obtained by pressure transmitter 13, see through the 10 execution tandem controls (cascade control) of flow quantity control module by inlet pressure control module 14, also can control the aperture of flow control valve 6.
The quality and the temperature that depend on processed liquid, the required input pressure in reverse osmosis membrane assembly unit 2 is different.In conventional operation, in the following manner, make the cooperation that reverse osmosis membrane assembly unit 2 required input pressure is changed (increase or reduce).When the required input pressures in reverse osmosis membrane assembly unit 2 increase, according to from the instruction that sees through flow quantity control module 10, the aperture of augmented flow control valve 6.On the contrary, when reverse osmosis membrane assembly unit 2 required input pressures reduce, reduce the aperture of flow control valve 6.
According to the viewpoint of dynamic power consumption, if useless dynamic power consumption, does not appear close to opening fully in the aperture of flow control valve 6.On the other hand, the aperture of flow control valve 6 is lower than to open then fully and means: flow control valve 6 consumed energies just, useless dynamic power consumption occurred in high-pressure pump 1.This dynamic power is corresponding to moving for example used electric power ((dynamic power)=(electric energy)) of device of high-pressure pump 1.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 processed fluid supply pump 15 (referring to Fig. 7) that has variable frequency drives (inverter) 7.
If do not consider less loine pressure loss, can add the discharge pressure of supply pump 15 by the discharge pressure with high-pressure pump 1, 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 specified discharge pressure of for example supply pump 15 is 1.0 MPas, and the specified discharge pressure of high-pressure pump 1 is when being 7.0 MPas, and the necessary inlet pressure of supposing reverse osmosis membrane assembly unit 2 is 7.5 MPas.In this case, in flow control valve 6, should lose dynamic power corresponding to 0.5 MPa.If supply pump 15 is equipped with variable frequency drives (inverter) 7, be fed to the frequency of supply of supply pump 15 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 MPas, can avoid useless power consumption.This method makes needn't invalidly consume dynamic electric energy in flow control valve 6.As above illustrative, such a case may appear, and processed fluid 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 that is arranged on the bypass conduit) all are effective.
Description of reference numerals
1: high-pressure pump (pump A)
2: the 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: see through the flow quantity meter
10: see through the flow quantity control module
11: flowmeter
12: high-pressure pump Minimum Flow Control unit
13: pressure transmitter
14: the inlet pressure control module
15: supply pump (pump C)
20: membrane module
21: cylindrical container
22: separating film element
23: entrance
24: central tube
25: see through the liquid discharging
26: the concentrate discharging
Claims (4)
1. reverse osmosis membrane separation device comprises:
Pump A is pressurized to the processed liquid of a part after the predetermined value, is fed to reverse osmosis membrane assembly;
Energy recycle device utilizes from the pressure of the concentrate of described reverse osmosis membrane assembly discharge, increases the pressure of the processed liquid of remaining part;
Pump B will carry out the processed liquid after the supercharging by described energy recycle device, after further being pressurized to predetermined value, be fed to described reverse osmosis membrane assembly;
Flow control valve A is used for regulating the flow from the processed liquid of described pump A discharge;
The 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 the described bypass runner, and the by-pass ratio of regulating processed liquid.
2. reverse osmosis membrane separation device according to claim 1 further comprises: pump C is used for processed liquid is fed to described pump A and described energy recycle device; And frequency converter, for the rotating speed of the described pump C of control.
3. the starting method of a reverse osmosis membrane separation device according to claim 1, described method comprises:
Before described pump A starting, regulate, make processed liquid flow through described energy recycle device, force (forcing) pump, described reverse osmosis membrane assembly and described energy recycle device in regular turn, and discharge subsequently;
Then, start described pump A, the aperture with described flow control valve A and described flow control valve B is set to predetermined value simultaneously; And
Then, control described flow control valve A and described flow control valve B step by step, make that flow control valve B operates in closing direction described flow control valve A in opening direction operation, increase to predetermined value until the inlet pressure of described reverse osmosis membrane assembly.
4. a generation sees through the method for liquid, comprising: start described reverse osmosis membrane separation device by reverse osmosis membrane separation device according to claim 3 starting method, then, processed liquid is fed to described reverse osmosis membrane assembly, to obtain seeing through liquid.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2010269054 | 2010-12-02 | ||
| JP2010-269054 | 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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| Publication Number | Publication Date |
|---|---|
| CN103237592A true CN103237592A (en) | 2013-08-07 |
| CN103237592B CN103237592B (en) | 2015-10-14 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201180058023.2A Expired - Fee Related CN103237592B (en) | 2010-12-02 | 2011-11-16 | The production method of reverse osmosis membrane separator, its starting method and permeate |
Country Status (5)
| Country | Link |
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| JP (1) | JP5974484B2 (en) |
| CN (1) | CN103237592B (en) |
| AU (1) | AU2011338029A1 (en) |
| TW (1) | TW201231152A (en) |
| WO (1) | WO2012073693A1 (en) |
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| CN105517961A (en) * | 2013-09-11 | 2016-04-20 | 株式会社荏原制作所 | Seawater desalination system |
| 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 |
| CN110382088A (en) * | 2017-01-09 | 2019-10-25 | 威立雅水务技术支持公司 | The system and method for handling water by reverse osmosis or nanofiltration |
| CN114790050A (en) * | 2022-03-21 | 2022-07-26 | 洛阳理工学院 | System and method for advanced wastewater treatment and bypass RO (reverse osmosis) membrane cooperative regeneration |
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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 |
| CN106132514B (en) * | 2014-03-27 | 2019-04-05 | 株式会社荏原制作所 | Energy recycling system |
| GB2540603A (en) | 2015-07-23 | 2017-01-25 | Ide Technologies Ltd | Imroved reverse osmotic process for cleaning water |
| 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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- 2011-11-16 WO PCT/JP2011/076357 patent/WO2012073693A1/en active Application Filing
- 2011-11-16 CN CN201180058023.2A patent/CN103237592B/en not_active Expired - Fee Related
- 2011-11-16 JP JP2011550764A patent/JP5974484B2/en not_active Expired - Fee Related
- 2011-11-16 AU AU2011338029A patent/AU2011338029A1/en not_active Abandoned
- 2011-12-01 TW TW100144093A patent/TW201231152A/en unknown
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105517961A (en) * | 2013-09-11 | 2016-04-20 | 株式会社荏原制作所 | Seawater desalination system |
| 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 |
| CN110382088A (en) * | 2017-01-09 | 2019-10-25 | 威立雅水务技术支持公司 | The system and method for handling water by reverse osmosis or nanofiltration |
| US11230479B2 (en) | 2017-01-09 | 2022-01-25 | Veolia Water Solutions & Technologies Support | System and method for the treating of water by reverse osmosis or nanofiltration |
| CN110382088B (en) * | 2017-01-09 | 2022-04-19 | 威立雅水务技术支持公司 | System and method for treating water by reverse osmosis or nanofiltration |
| US11673815B2 (en) | 2017-01-09 | 2023-06-13 | Veolia Water Solutions & Technologies Support | System and method for the treatment of water by reverse osmosis or nanofiltration |
| CN114790050A (en) * | 2022-03-21 | 2022-07-26 | 洛阳理工学院 | System and method for advanced wastewater treatment and bypass RO (reverse osmosis) membrane cooperative regeneration |
| CN114790050B (en) * | 2022-03-21 | 2024-04-26 | 上海源依青科技有限责任公司 | System and method for advanced wastewater treatment and bypass RO (reverse osmosis) membrane collaborative regeneration |
Also Published As
| Publication number | Publication date |
|---|---|
| TW201231152A (en) | 2012-08-01 |
| AU2011338029A1 (en) | 2013-06-20 |
| CN103237592B (en) | 2015-10-14 |
| WO2012073693A1 (en) | 2012-06-07 |
| JPWO2012073693A1 (en) | 2014-05-19 |
| JP5974484B2 (en) | 2016-08-23 |
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