US20040134521A1 - Direct osmosis cleaning - Google Patents
Direct osmosis cleaning Download PDFInfo
- Publication number
- US20040134521A1 US20040134521A1 US10/718,539 US71853903A US2004134521A1 US 20040134521 A1 US20040134521 A1 US 20040134521A1 US 71853903 A US71853903 A US 71853903A US 2004134521 A1 US2004134521 A1 US 2004134521A1
- Authority
- US
- United States
- Prior art keywords
- permeate
- pressure
- membrane
- saline solution
- feed
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
- 238000004140 cleaning Methods 0.000 title claims abstract description 99
- 239000012466 permeate Substances 0.000 claims abstract description 180
- 239000012528 membrane Substances 0.000 claims abstract description 140
- 238000000034 method Methods 0.000 claims abstract description 108
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 89
- 238000000926 separation method Methods 0.000 claims abstract description 42
- 239000002904 solvent Substances 0.000 claims abstract description 12
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 148
- 239000012267 brine Substances 0.000 claims description 110
- 230000003204 osmotic effect Effects 0.000 claims description 40
- 239000000243 solution Substances 0.000 claims description 35
- 238000010612 desalination reaction Methods 0.000 claims description 34
- 238000004891 communication Methods 0.000 claims description 15
- 238000011084 recovery Methods 0.000 claims description 14
- 239000012530 fluid Substances 0.000 claims description 10
- 239000012459 cleaning agent Substances 0.000 claims description 9
- 150000003839 salts Chemical class 0.000 claims description 7
- 238000003860 storage Methods 0.000 claims description 7
- 239000000047 product Substances 0.000 claims description 5
- 239000011780 sodium chloride Substances 0.000 claims description 4
- 238000001223 reverse osmosis Methods 0.000 description 120
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 45
- 239000013535 sea water Substances 0.000 description 8
- 125000004122 cyclic group Chemical group 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000035515 penetration Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000000108 ultra-filtration Methods 0.000 description 2
- 235000012206 bottled water Nutrition 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000000149 penetrating effect Effects 0.000 description 1
- 230000002093 peripheral effect Effects 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- -1 seawater Chemical compound 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910021642 ultra pure water Inorganic materials 0.000 description 1
- 239000012498 ultrapure water Substances 0.000 description 1
Images
Classifications
-
- 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
- B01D61/10—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- 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
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0022—Apparatus therefor
-
- 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
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/10—Spiral-wound membrane modules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/06—Use of osmotic pressure, e.g. direct osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/20—By influencing the flow
- B01D2321/2066—Pulsated flow
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
- B01D2321/26—By suction
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Definitions
- This invention relates to method and system for cleaning membranes, in particular reverse osmosis and nanofiltration membranes in desalination and water treatment plants.
- the method of reverse osmosis is an effective and energy-saving method of desalination which is widely employed for obtaining water for industrial use, for agriculture, potable water and ultrapure water.
- the method consists in applying mechanical (gauge) pressure over a saline solution, such as seawater, which is higher than the osmotic pressure of the same solution, in a volume delimited by a semi-permeable membrane (RO membrane).
- a saline solution such as seawater
- RO membrane semi-permeable membrane
- osmotic pressures of solutions are referenced to pure solvent, i.e. if given saline water solution has osmotic pressure PO, this means, pure water from the other side of an osmotic membrane will permeate towards this solution as if under gauge pressure PO.
- foulants such as suspended particles, organic matter, colloids tend to accumulate on the “feed” surface of the membrane. Some dissolved salts also may precipitate on the surface, forming scale. A fouled membrane has reduced separability, increased pressure losses and therefore has to be cleaned.
- a more effective method is using the direct osmosis by feeding saline solution to the fouled feed side of the RO membrane while supplying solvent (water) to the permeate side of the membrane.
- solvent water
- the higher osmotic pressure at the feed side sucks the water from the permeate side to the feed side of the RO membrane, whereby the water penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface.
- EP0768112 and JP2000-079328 disclose similar implementations of the direct osmosis method. It is suggested that when the membrane is cleaned, the production RO process is stopped, the saline solution is supplied to the feed side of the membrane essentially without pressure (or at least under pressure lower than the osmotic pressure of the solution), and the water is supplied to the permeate side of the membrane also without pressure. Thus, the cleaning water is sucked back to the feed side essentially under the net differential between the two osmotic pressures.
- the typical RO membrane is a tight multi-layered structure with very narrow passages (see FIG. 5) where water flows very slowly. Some areas of the membrane are close to the channel supplying water, other areas are remote. On the other hand, the osmotic pressure of the typical saline solution—seawater or brine—is high, and the net differential is also high. The combination of these factors leads to very fast back-suction of water (“catastrophic” filtration) from the permeate side to the feed side through the close areas of the membrane. As a result, the water can not reach the remote areas of the membrane before it is entirely sucked in the close areas, while the concentration at both sides of the membrane in the close areas is soon equalized. The cleaning process, therefore, stops in a few seconds and the membrane cannot be cleaned uniformly.
- a direct-osmosis method of cleaning fouled RO membranes in modules for RO separation The membrane has a feed side and an opposite permeate side and extends between a front end and a rear end of the RO module.
- the module has a front-end feed port and a rear-end brine port in communication with the feed side of the membrane, and at least one permeate port in communication with the permeate side of the membrane.
- the normal RO separation process in the same module includes feeding raw saline solution comprising water, dissolved salts and a potential foulant with osmotic pressure PO 1 , to the front-end feed port at gauge pressure PF 1 >PO 1 , collecting permeate with osmotic pressure PO 2 from the permeate port at gauge pressure PP 2 , and removing residual brine from the rear-end feed port at gauge pressure PB 3 .
- the foulant accumulates at the feed side of the RO membrane.
- the cleaning method comprises:
- step (b) the net driving differential ⁇ PN resulting from pressures PO 4 , PD 4 , PO 5 , and PC 5 is directed to the feed side, whereby the water is sucked from the permeate side of the RO membrane to the feed side of the RO membrane, penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface.
- the gauge pressure PC 5 is between the pressures PF 1 and PO 1 in the normal RO process, while the ⁇ PN directed to the feed side is provided by raising the gauge pressure PD 4 with respect to the gauge pressure PP 2 in the normal RO process.
- the concentrated saline solution may be fed to the rear-end brine port at step (b), and withdrawn from the front-end feed port at step (c), or vice-versa.
- the concentrated saline solution of step (b) may be residual brine supplied from another RO module performing normal RO separation process, or the raw saline solution of the normal RO separation process.
- the dilute saline solution of step (a) may be the permeate obtained in the same RO module during its normal separation process and stored, may be permeate obtained from another RO module performing normal RO separation process, or may be residual brine obtained in a next-stage separator of the same desalination plant, or from any other source.
- the cleaned RO module is a first-stage module
- residual brine obtained from the first-stage permeate in a second-stage separator may be used.
- raw saline solution and permeate are fed to the respective sides of the membrane by the same pressure source (pump) that provides the gauge pressure PF 1 for the normal RO process.
- pump pressure source
- the method is advantageously applicable for RO membranes, where the permeate side of the membrane communicates with the permeate port through a permeate channel, and the membrane has parts adjacent the permeate channel and parts remote therefrom.
- the net driving differential ⁇ PN in this case is such that it allows the dilute saline solution to reach the remote parts of the membrane before the water is entirely sucked to the feed side of the membrane through the parts adjacent to the permeate channel.
- the efficiency of the method may be enhanced in the following ways: Alternating from time to time the feeding and the withdrawing of the concentrated saline solution between the front-end and the rear-end feed port; application of pulsating gauge pressure PD 4 ; changing from time to time gauge pressure PD 4 and/or PC 5 so that the net pressure differential ⁇ PN is reversed towards the permeate side, whereby the RO module performs intermittently normal RO separation process.
- the cleaning method may be further improved.
- the feeding in steps (a) and (b) is performed through the same-end port of the respective side, and a second dilute saline solution is fed to the other-end permeate port under gauge pressure PD 4 and osmotic pressure PO 4 ′ ⁇ PO 4 .
- the pressure PO 4 ′ compensates for a fall of the net driving differential ⁇ PN due to the fall of osmotic pressure at the feed side as the concentrated saline solution flows from the same-end feed port towards the other-end feed port and sucks in solvent from the permeate side.
- Cleaning agent may be added to the dilute saline solution of step (a) and/or to the concentrated saline solution of step (b).
- the cleaning method of the present invention is especially advantageous for desalination facilities with energy recovery plant using a plurality of RO modules.
- each of the RO modules performs in turn the cleaning process, while the rest of the RO modules perform normal RO separation process.
- the concentrated saline solution of step (b) is then a portion of the residual brine removed from the rest of RO modules.
- the rest of the removed residual brine is fed to the energy recovery plant at high pressure PR, and the pressure of the concentrated saline solution withdrawn at step (c) is boosted up to the pressure PR before feeding to the energy recovery plant.
- a cleaning system for performing the above cleaning method in a desalination plant comprising a plurality of modules for RO separation.
- the RO modules are connected in parallel and are adapted to perform the above-described normal separation process.
- the desalination plant further comprises a source of raw solution with high-pressure feed pump, a common high-pressure raw solution feed line connecting the front-end feed ports of the modules to the source of raw solution, a common high-pressure brine collection line connecting the rear-end brine ports of the modules to a first brine discharge outlet, and a common permeate collection line connecting the permeate ports of the modules to a product storage tank or a next-stage separator.
- the system for cleaning fouled RO membranes according to the above cleaning method comprises:
- the first line is the common high-pressure brine collection line
- the second line is a common line connecting front-end feed ports of the RO modules to a second brine discharge outlet, the system being adapted to use a portion of the collected brine as concentrated saline solution in the step (b) of the method, and to discharge the portion of brine through the second brine discharge outlet in step (c) of the method.
- the first line is the common high-pressure raw solution feed line
- the second line is the common high-pressure brine collection line
- the system is adapted to use a portion of the raw solution as concentrated saline solution in the step (b) of the method, and to discharge the portion of raw solution through the first brine discharge outlet in step (c) of the method.
- the pressurized source of dilute saline solution may be a permeate storage tank with a high-pressure permeate feed pump.
- the permeate storage tank is a pressure-exchange vessel having a permeate chamber and a feed chamber divided by a diaphragm or a piston.
- the permeate chamber is connected to the common high-pressure cleaning line, while the feed chamber is connected via a first stop valve to a high-pressure fluid source, and via a second stop valve to a discharge line.
- the vessel can be filled with high-pressure fluid to discharge the permeate under high pressure via the cleaning line, and can be filled with permeate to discharge the fluid through the discharge line.
- the high-pressure fluid source may be the common high-pressure raw solution feed line or the common high-pressure brine collecting line.
- next-stage separators have a booster pump in communication with the next-stage brine outlet and a common brine line connecting the permeate ports of the first-stage modules to the booster pump.
- next-stage brine can be used as dilute saline solution at step (a) of the cleaning method applied in turn to each RO module of the first stage.
- the next-stage separator may be connected to the common permeate collection line, and may obtain the next-stage brine from the first-stage permeate.
- the common permeate collection line is connected to the rear-end permeate port of each module.
- the system further comprises a second source of second dilute saline solution, a common line connecting the front-end permeate ports of the RO modules to the second source, and a plurality of valves and pumps adapted to close or open each of the ports and common lines and to feed each of the dilute saline solutions with osmotic pressure PO 4 or PO 4 ′ to the front-end or rear-end permeate port of each of said RO modules under pressure PD 4 .
- the cleaning system preferably comprises a tank with cleaning agent, a line connecting the tank to the source of dilute saline solution, and/or lines adapted to feed the cleaning agent to the feed ports of the modules together with the concentrated saline solution during step (b) of the cleaning method.
- the cleaning system may further comprise a booster pump with inlet port connected to the second brine discharge outlet and outlet port connected to the common brine collection line.
- step (b) feeding the raw saline solution obtained in step (b) to an energy recovery plant.
- the direct-osmosis cleaning method of the present invention provides a number of major advantages:
- Cleaning of the RO membranes in a train of RO modules may be performed continuously, in turn with each RO module, without interrupting the operation of any RO module and the desalination process as a whole;
- Spirally wound RO membranes may be thoroughly cleaned from accumulated suspended solids, scaling, and bio-fouling;
- RO membranes cleaned by this method will have lower pressure drop (hydraulic losses) than membranes cleaned by known methods and will therefore save power required for desalination;
- the gauge pressure at the feed side of the RO membrane is never lower than the gauge pressure at the permeate side, thereby preserving the integrity of the membrane;
- the method allows brine from intermediate stages of the desalination process to be utilized more effectively.
- FIG. 1 is a scheme of a prior art desalination plant with a plurality of RO modules
- FIG. 2 is a schematic longitudinal section of a RO membrane in a RO module in prior art normal desalination process
- FIG. 3 is a schematic longitudinal section of a RO membrane in a RO module in the direct osmosis cleaning process of the present invention
- FIG. 4 is a scheme of the desalination plant of FIG. 1 equipped with a cleaning system of the present invention.
- FIG. 5 is a schematic cross-section of a RO membrane in a RO module.
- FIG. 6 is a schematic longitudinal section of a RO membrane in a RO module in a variation of the direct osmosis cleaning process.
- FIG. 7 is a scheme of the desalination plant of FIG. 1 equipped with a “cyclic” cleaning system of the present invention.
- each RO module 12 has an elongated housing 18 with front end and rear end.
- a RO membrane 20 extends between the front end and the rear end dividing the internal volume of the housing into feed side and permeate side (FIG. 2 is simplified, the membrane may be pleated/folded and rolled into a rather complex shape, as shown in FIG. 5).
- the membrane 20 has, consequently, feed side surface 21 and permeate side surface 22 .
- the housing 18 has front-end feed port 24 and rear-end brine port 26 in communication with the feed side of the membrane 20 , and front-end permeate port 28 and rear-end permeate port 30 in communication with the permeate side of the membrane.
- the desalination plant 10 further comprises a common high-pressure feed collector 34 connecting HPP 14 to the front-end feed ports 24 of the modules 12 via high pressure feed lines 35 ; a common high-pressure brine collector 36 connected to the rear-end brine ports 26 of the modules 12 via high-pressure brine lines 37 ; common rear permeate collector 38 connected to the rear-end permeate ports 30 via rear permeate lines 39 ; and common front permeate collector 40 connected to the front-end permeate ports 28 via front permeate lines 42 .
- the ERG 17 comprises a group of work exchangers 50 , a circulation pump 52 connected to the feed collector 34 , high-pressure brine inlet 54 connected to the brine collector 36 , low-pressure brine discharge outlet 55 , and low-pressure feed inlet 56 .
- the desalination plant 10 is connected to a source of raw solution (seawater) such as water pretreatment stage (not shown) at the inlet of the HPP 14 and at the feed inlet 56 of the ERG group 17 .
- Outlets of permeate collectors 38 and 40 are connected to next separation stages or product tanks (not shown).
- Check valves 58 connect the rear-end brine port 26 to the rear-end permeate port 30 of each RO module 12 so as to prevent increasing of the pressure at the permeate side over the pressure at the feed side.
- a plurality of valves 60 , 61 , 62 , 63 are adapted to close or open each of the above ports and common lines as will be explained below.
- the obtained permeate product has low TDS content and low osmotic pressure PO 2 ⁇ 0.3 bar.
- the permeate is withdrawn from the permeate side under gauge pressure PP 2 ⁇ 2 bar.
- the feed water salinity and osmotic pressure increase as the feed water flows towards the rear end of the module while the gauge pressure falls due to hydraulic losses. Therefore, the net driving differential falls, and the permeate salinity varies along the membrane.
- the obtained permeate can be divided into front permeate (lower TDS) transferred via front permeate collector 40 , and rear permeate (higher TDS) transferred via rear permeate collector 38 .
- the seawater usually contains potential foulants such as suspended particles, organic molecules, live microorganisms or dissolved salts which may form scale.
- potential foulants such as suspended particles, organic molecules, live microorganisms or dissolved salts which may form scale.
- the foulants 64 accumulate at the feed side of the RO membrane contaminating it, reducing its permeability and increasing the hydraulic losses.
- FIG. 4 shows the inventive cleaning system integrated with the desalination plant 10 of FIG. 1.
- the latter has additionally a second-stage RO module 68 with middle-pressure pump 70 .
- the second-stage module 68 receives rear-end product (permeate) from the permeate collector 38 of the first stage described above, transfers the second-stage permeate 71 to the front permeate collector 40 , and discharges residual brine to drain 72 through valve 73 .
- the system for cleaning fouled RO membranes by direct osmosis comprises:
- a high-pressure cleaning collector 80 connecting the rear permeate ports 30 of the RO modules 12 to the source of dilute saline solution;
- a cleaning booster brine pump 84 with inlet connected to the brine collector 82 , and outlet connected to the high-pressure brine collector 36 ;
- valves 86 , 87 , 88 , and 89 adapted to close or open each of the above ports and collectors, so as to allow performing of the normal separation process and the cleaning method on each RO module in turn, as will be explained below.
- stop-valves 60 A, 61 A and 63 A associated with the module 12 A are closed, while the same valves on the other RO modules are opened (closed valves are drawn in solid black in FIG. 4), whereby the module 12 A quits the normal RO process;
- stop-valve 62 A remains opened, whereby the rear-end brine port of the module 12 A remains connected to the high-pressure brine collector 36 ;
- stop-valve 87 A is opened and the cleaning booster brine pump 84 is operated, whereby the brine starts to circulate through the feed side of the module 12 A in reverse direction;
- the cleaning booster pump 78 is operated to feed second-stage brine to the permeate side of the RO membrane in the module 12 A;
- valve 86 A is opened to drain the remaining second-stage brine from the permeate side.
- FIG. 3 explains in further detail the cleaning process on the RO membrane (the pressure values are only exemplary).
- the net driving differential ⁇ PN is now:
- ⁇ PN is directed to the feed side, whereby the water is sucked from the permeate side of the RO membrane to the feed side.
- the water penetrates into the interface between the membrane and the accumulated foulants 64 , and separates the foulants from the membrane surface.
- the first-stage brine, together with the foulants and the penetrated water (Brine 1 ′) is withdrawn through the front-end feed port 24 under gauge pressure which is less than PB 3 due to hydraulic losses in the flow along the membrane.
- the booster brine pump 84 restores these losses and feeds the brine to the common high-pressure brine collector 36 for passing to the EGR 17 .
- the net driving differential can be adjusted by regulating the pressure PD 4 by means of the VFD 79 .
- the direct-osmosis cleaning method of the present invention can be applied in turn to each RO module 12 by switching of valves, without interrupting the desalination process.
- the penetrating water acquires higher gauge pressure at the feed side, PC 5 , and this pressure is later returned to the system in the energy recovery group 17 . In this way, part of the energy spent for separation of the permeate from the brine, and preserved in the form of higher osmotic pressure of the latter, is restored in the cleaning process.
- the dilute solution which is used as source of water in the cleaning process may be taken also from other stages of the desalination plant, or from other sources.
- FIG. 4 shows (in phantom line) that rear permeate stored in tank 76 may be used instead of second-stage brine.
- Raw seawater may be used as concentrated solution at the feed side instead of brine.
- seawater from the ERG 17 may be taken before the booster pump 52 and used in the cleaning process.
- Cleaning agent (not shown) can be added to the dilute solution, or to the concentrated solution, or to both.
- the gauge pressure at the feed side PC 5 is between the feed water pressure PF 1 and the osmotic pressure of the feed water PO 1 in the normal RO process.
- the gauge pressure PD 4 at the permeate side is significantly higher than the gauge pressure PP 2 i in the normal RO process, so as to provide ⁇ PN directed to the feed side.
- the net driving differential ⁇ PN is lower than the osmotic pressure of the saline solution at the feed side, thereby avoiding the “catastrophic” filtration described in the Background.
- FIG. 5 shows schematically the cross- section of the RO module 12 .
- the RO membrane 20 is pleated, with highly permeable spacer material 93 and 94 inserted between the membrane folds at the feed side and the permeate side, respectively.
- the membrane is rolled into a very tight spiral around a tube 95 and is inserted in the module housing 18 .
- the tube 95 is perforated and constitutes a permeate channel 96 connecting the front-end permeate port 28 and the rear-end permeate port 30 to the permeate side of the RO membrane 20 . It can be seen that the dilute solution (permeate) can easily reach membrane parts adjacent to the permeate channel 96 , such as in zone I.
- the present method allows the net driving differential ⁇ PN to be regulated so that the dilute saline solution can reach the remote parts of the membrane before the water is entirely sucked to the feed side of the membrane through the parts adjacent to the permeate channel 96 .
- the cleaning method of the present invention is improved to overcome this disadvantage.
- a source of second dilute solution is provided, with osmotic pressure PO 4 ′ lower than PO 4 .
- This may be, for example, the rear-end permeate with PO 4 ′ ⁇ 0.3 bar from the tank 76 shown in FIG. 4.
- Another high-pressure pump, a cleaning collector and valves are added to connect the front permeate ports 28 of the RO modules 12 to the source of second dilute saline solution.
- the method of the present invention may be simplified to “rinsing” of fouled RO membranes without stopping the operation of the RO module.
- the “rinsing” method comprises:
- FIG. 7 Another simplified system performing an effective “cyclic” version of the same direct-osmosis cleaning process is illustrated in FIG. 7.
- the simplified cyclic cleaning system is integrated, as before, in the desalination plant 10 of FIG. 1, but does not involve connections to next RO stages, and comprises only:
- valves 107 adapted to close or open each of the permeate ports to the cleaning collector 105 , so as to allow performing of the normal separation process and the simplified cyclic cleaning method on each RO module in turn.
- the pressure-exchange vessel 103 has a feed-water chamber 109 and a permeate chamber 111 divided by a flexible diaphragm 113 .
- the permeate chamber 111 is in communication with the cleaning collector 105 while the feed-water chamber 109 is connected to the high-pressure feed collector 34 via a stop-valve 115 , and to a drain pipe 119 via a drain valve 117 .
- the permeate collector 38 and the valves 61 connecting it to the RO modules are adapted to work under the high pressure of the feed collector 34 .
- Stop-valves 107 A and 115 are opened, whereby the feed water under the high feed pressure enters the feed-water chamber 109 and displaces the diaphragm 113 and the permeate from the chamber 111 towards the permeate side of the RO module 12 A.
- the cleaning sequence is finished when the chamber 111 collapses to a minimum volume or the stop-valve 115 is closed;
- the gauge pressures at the feed side and at the permeate side of the membrane are equalized.
- the osmotic pressure in the permeate channel is much lower than in the feed-brine channel, whereby the net driving differential ⁇ PN is reversed towards the feed side, and the permeate passes back through the membrane separating the foulant therefrom.
- the mobilized foulant is carried away with the high-pressure flow through the brine collector 36 and is drained through the ERG 17 . Due to the high gauge pressure in the permeate channel, the sucked-back water has sufficient energy to reach the remote areas of the membrane.
- the diaphragm 113 is needed only to separate the permeate from the feed water in the pressure-exchange vessel 103 .
- cylinder with a plunger may be used, similar to work exchangers 50 .
- the valve 115 may be complemented with a pressure regulator to control the driving differential ⁇ PN if necessary.
- the drained feed water may be returned back to the suction side of the HPP 14 .
- the pressure-exchange vessel 103 may use, as a source of high-pressure fluid, not only the feed collector 34 but also the brine collector 36 .
- the high- pressure cleaning collector 105 may be connected to either permeate port (front or rear), or to both.
- the cyclic process allows cleaning the membranes without depressurization of the RO modules and without stopping the feed-brine flow and the flow towards the energy recovery plant.
- it does not use another pressure source besides the pressure of the feed flow, and does not require a variable frequency drive or other complicated control of the HPP output. Due to the same reason, the gauge pressure in the permeate channel cannot exceed the gauge pressure in the feed channel, so that the check valves 58 become unnecessary.
- the available quantity of permeate for one cleaning cycle is limited by the volume of the pressurization cylinder 103 but the cycle may be repeated as necessary.
- the cleaning method of the present invention may be used for cleaning nanofiltration and ultrafiltration membranes. It can be applied to single RO modules, and can be used with any type of energy recovery device, such as Pelton turbine, Francice turbine, or work exchanger.
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Nanotechnology (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
A method of cleaning a fouled RO membrane in a module for RO separation, the membrane having feed side and permeate side, the foulant accumulating at the feed side. The cleaning method comprises:
feeding concentrated saline solution to the feed side of the RO membrane under the high gauge pressure of the normal RO separation process;
feeding dilute saline solution to the permeate side of the RO membrane under higher pressure than the permeate pressure of the normal RO process, so that a net driving differential ΔPN is directed to the feed side, whereby the solvent is being sucked from the permeate side to the feed side, penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface; and
withdrawing the concentrated saline solution together with the separated foulant and the penetrated solvent from the feed side of the RO membrane.
Description
- This invention relates to method and system for cleaning membranes, in particular reverse osmosis and nanofiltration membranes in desalination and water treatment plants.
- The method of reverse osmosis (RO) is an effective and energy-saving method of desalination which is widely employed for obtaining water for industrial use, for agriculture, potable water and ultrapure water. The method consists in applying mechanical (gauge) pressure over a saline solution, such as seawater, which is higher than the osmotic pressure of the same solution, in a volume delimited by a semi-permeable membrane (RO membrane). Thereby, the solvent (water) is squeezed through the membrane to its “permeate” side while dissolved salts remain in the solution at the “feed” side of the membrane.
- Herein, osmotic pressures of solutions are referenced to pure solvent, i.e. if given saline water solution has osmotic pressure PO, this means, pure water from the other side of an osmotic membrane will permeate towards this solution as if under gauge pressure PO.
- When the RO membrane is used for a long time for separation of salts, other components of the raw solution termed “foulants” herein, such as suspended particles, organic matter, colloids tend to accumulate on the “feed” surface of the membrane. Some dissolved salts also may precipitate on the surface, forming scale. A fouled membrane has reduced separability, increased pressure losses and therefore has to be cleaned.
- It is known to clean the membrane by stopping the production process and pumping cleaning chemical solutions to wash the fouled surface. Such methods are costly, not very effective, and create new environmental problems.
- A more effective method is using the direct osmosis by feeding saline solution to the fouled feed side of the RO membrane while supplying solvent (water) to the permeate side of the membrane. The higher osmotic pressure at the feed side sucks the water from the permeate side to the feed side of the RO membrane, whereby the water penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface.
- Publications EP0768112 and JP2000-079328 disclose similar implementations of the direct osmosis method. It is suggested that when the membrane is cleaned, the production RO process is stopped, the saline solution is supplied to the feed side of the membrane essentially without pressure (or at least under pressure lower than the osmotic pressure of the solution), and the water is supplied to the permeate side of the membrane also without pressure. Thus, the cleaning water is sucked back to the feed side essentially under the net differential between the two osmotic pressures.
- However, the typical RO membrane is a tight multi-layered structure with very narrow passages (see FIG. 5) where water flows very slowly. Some areas of the membrane are close to the channel supplying water, other areas are remote. On the other hand, the osmotic pressure of the typical saline solution—seawater or brine—is high, and the net differential is also high. The combination of these factors leads to very fast back-suction of water (“catastrophic” filtration) from the permeate side to the feed side through the close areas of the membrane. As a result, the water can not reach the remote areas of the membrane before it is entirely sucked in the close areas, while the concentration at both sides of the membrane in the close areas is soon equalized. The cleaning process, therefore, stops in a few seconds and the membrane cannot be cleaned uniformly.
- In accordance with the present invention, there is provided a direct-osmosis method of cleaning fouled RO membranes in modules for RO separation. The membrane has a feed side and an opposite permeate side and extends between a front end and a rear end of the RO module. The module has a front-end feed port and a rear-end brine port in communication with the feed side of the membrane, and at least one permeate port in communication with the permeate side of the membrane.
- The normal RO separation process in the same module includes feeding raw saline solution comprising water, dissolved salts and a potential foulant with osmotic pressure PO1, to the front-end feed port at gauge pressure PF1>PO1, collecting permeate with osmotic pressure PO2 from the permeate port at gauge pressure PP2, and removing residual brine from the rear-end feed port at gauge pressure PB3. During this process, the foulant accumulates at the feed side of the RO membrane.
- The cleaning method comprises:
- a) feeding dilute saline solution to the permeate side of the RO membrane under gauge pressure PD4 and osmotic pressure PO4;
- b) feeding concentrated saline solution to the feed side of the RO membrane under gauge pressure PC5 and osmotic pressure PO5.
- c) withdrawing the concentrated saline solution together with the separated foulant and the penetrated water from the feed side of the RO membrane.
- At step (b), the net driving differential ΔPN resulting from pressures PO4, PD4, PO5, and PC5 is directed to the feed side, whereby the water is sucked from the permeate side of the RO membrane to the feed side of the RO membrane, penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface.
- In the inventive method, the gauge pressure PC5 is between the
pressures PF 1 and PO1 in the normal RO process, while the ΔPN directed to the feed side is provided by raising the gauge pressure PD4 with respect to the gauge pressure PP2 in the normal RO process. - The concentrated saline solution may be fed to the rear-end brine port at step (b), and withdrawn from the front-end feed port at step (c), or vice-versa.
- The concentrated saline solution of step (b) may be residual brine supplied from another RO module performing normal RO separation process, or the raw saline solution of the normal RO separation process.
- The dilute saline solution of step (a) may be the permeate obtained in the same RO module during its normal separation process and stored, may be permeate obtained from another RO module performing normal RO separation process, or may be residual brine obtained in a next-stage separator of the same desalination plant, or from any other source. Advantageously, if the cleaned RO module is a first-stage module, then residual brine obtained from the first-stage permeate in a second-stage separator may be used.
- In a preferred embodiment, raw saline solution and permeate are fed to the respective sides of the membrane by the same pressure source (pump) that provides the gauge pressure PF1 for the normal RO process.
- The method is advantageously applicable for RO membranes, where the permeate side of the membrane communicates with the permeate port through a permeate channel, and the membrane has parts adjacent the permeate channel and parts remote therefrom. The net driving differential ΔPN in this case is such that it allows the dilute saline solution to reach the remote parts of the membrane before the water is entirely sucked to the feed side of the membrane through the parts adjacent to the permeate channel.
- The efficiency of the method may be enhanced in the following ways: Alternating from time to time the feeding and the withdrawing of the concentrated saline solution between the front-end and the rear-end feed port; application of pulsating gauge pressure PD4; changing from time to time gauge pressure PD4 and/or PC5 so that the net pressure differential ΔPN is reversed towards the permeate side, whereby the RO module performs intermittently normal RO separation process.
- In view of the fact that the standard RO module has a front-end permeate port and a rear-end permeate port in communication with said permeate side of the RO membrane, the cleaning method may be further improved. The feeding in steps (a) and (b) is performed through the same-end port of the respective side, and a second dilute saline solution is fed to the other-end permeate port under gauge pressure PD4 and osmotic pressure PO4′<PO4. The pressure PO4′ compensates for a fall of the net driving differential ΔPN due to the fall of osmotic pressure at the feed side as the concentrated saline solution flows from the same-end feed port towards the other-end feed port and sucks in solvent from the permeate side.
- Cleaning agent may be added to the dilute saline solution of step (a) and/or to the concentrated saline solution of step (b).
- The cleaning method of the present invention is especially advantageous for desalination facilities with energy recovery plant using a plurality of RO modules. In this case, each of the RO modules performs in turn the cleaning process, while the rest of the RO modules perform normal RO separation process. The concentrated saline solution of step (b) is then a portion of the residual brine removed from the rest of RO modules. The rest of the removed residual brine is fed to the energy recovery plant at high pressure PR, and the pressure of the concentrated saline solution withdrawn at step (c) is boosted up to the pressure PR before feeding to the energy recovery plant.
- According to another aspect of the present invention, there is provided a cleaning system for performing the above cleaning method in a desalination plant comprising a plurality of modules for RO separation. The RO modules are connected in parallel and are adapted to perform the above-described normal separation process. The desalination plant further comprises a source of raw solution with high-pressure feed pump, a common high-pressure raw solution feed line connecting the front-end feed ports of the modules to the source of raw solution, a common high-pressure brine collection line connecting the rear-end brine ports of the modules to a first brine discharge outlet, and a common permeate collection line connecting the permeate ports of the modules to a product storage tank or a next-stage separator.
- The system for cleaning fouled RO membranes according to the above cleaning method comprises:
- a) a pressurized source of dilute saline solution providing the pressure PD4;
- b) a common high-pressure line connecting the permeate ports of the modules to the source of dilute saline solution;
- c) a pressurized source of concentrated saline solution providing the pressure PC5;
- d) a first line to connect the source of concentrated saline solution to the feed side of the membrane in each RO module;
- e) a second line to withdraw the concentrated saline solution from the feed side of the membrane in each RO module; and
- f) a plurality of valves adapted to close or open each of the above ports and common lines so as to allow performing of the normal separation process and the cleaning method on each RO module in turn.
- In one embodiment, the first line is the common high-pressure brine collection line, the second line is a common line connecting front-end feed ports of the RO modules to a second brine discharge outlet, the system being adapted to use a portion of the collected brine as concentrated saline solution in the step (b) of the method, and to discharge the portion of brine through the second brine discharge outlet in step (c) of the method.
- In another embodiment, the first line is the common high-pressure raw solution feed line, the second line is the common high-pressure brine collection line, and the system is adapted to use a portion of the raw solution as concentrated saline solution in the step (b) of the method, and to discharge the portion of raw solution through the first brine discharge outlet in step (c) of the method.
- The pressurized source of dilute saline solution may be a permeate storage tank with a high-pressure permeate feed pump. In a preferred embodiment, the permeate storage tank is a pressure-exchange vessel having a permeate chamber and a feed chamber divided by a diaphragm or a piston. The permeate chamber is connected to the common high-pressure cleaning line, while the feed chamber is connected via a first stop valve to a high-pressure fluid source, and via a second stop valve to a discharge line. The vessel can be filled with high-pressure fluid to discharge the permeate under high pressure via the cleaning line, and can be filled with permeate to discharge the fluid through the discharge line. Advantageously, the high-pressure fluid source may be the common high-pressure raw solution feed line or the common high-pressure brine collecting line.
- Preferably, in a multi-stage desalination plant where the plurality of RO modules constitute a first stage, the next-stage separators have a booster pump in communication with the next-stage brine outlet and a common brine line connecting the permeate ports of the first-stage modules to the booster pump. Thereby the next-stage brine can be used as dilute saline solution at step (a) of the cleaning method applied in turn to each RO module of the first stage. In particular, the next-stage separator may be connected to the common permeate collection line, and may obtain the next-stage brine from the first-stage permeate.
- Advantageously, if each one of the plurality of modules has a front-end permeate port and a rear-end permeate port in communication with the permeate side of the RO membrane, the common permeate collection line is connected to the rear-end permeate port of each module. The system further comprises a second source of second dilute saline solution, a common line connecting the front-end permeate ports of the RO modules to the second source, and a plurality of valves and pumps adapted to close or open each of the ports and common lines and to feed each of the dilute saline solutions with osmotic pressure PO4 or PO4′ to the front-end or rear-end permeate port of each of said RO modules under pressure PD4.
- The cleaning system preferably comprises a tank with cleaning agent, a line connecting the tank to the source of dilute saline solution, and/or lines adapted to feed the cleaning agent to the feed ports of the modules together with the concentrated saline solution during step (b) of the cleaning method.
- If the desalination plant includes an energy recovery plant connected to the first brine discharge outlet, then the cleaning system may further comprise a booster pump with inlet port connected to the second brine discharge outlet and outlet port connected to the common brine collection line.
- According to an alternative aspect of the present invention, there is provided a simplified “rinsing” method of cleaning a fouled RO membrane in a module for RO separation as described above. The “rinsing” method comprises
- a) changing the
gauge pressure PF 1 to a pulsatinggauge pressure PF 1′ with average value close to the osmotic pressure PO1 so that a net driving differential ΔPN resulting from pressures PO, PO2, PP2, and PF1′ would be directed alternatively to the feed side and the permeate side of the membrane, whereby, when the ΔPN is directed to the feed side, the above-described direct-osmosis cleaning process is performed, while when the ΔPN is directed to the permeate side, the RO membrane performs normal RO separation; - b) withdrawing the raw saline solution together with the separated foulant through said rear-end brine port; and optionally,
- c) feeding the raw saline solution obtained in step (b) to an energy recovery plant.
- The direct-osmosis cleaning method of the present invention provides a number of major advantages:
- Cleaning of the RO membranes in a train of RO modules may be performed continuously, in turn with each RO module, without interrupting the operation of any RO module and the desalination process as a whole;
- Cleaning of the membranes is so effective that the stage of ultrafiltration pretreatment may be skipped for certain types of raw water, since the inventive cleaning method can remove fouling due to suspended solids present in raw water.
- Spirally wound RO membranes may be thoroughly cleaned from accumulated suspended solids, scaling, and bio-fouling;
- RO membranes cleaned by this method will have lower pressure drop (hydraulic losses) than membranes cleaned by known methods and will therefore save power required for desalination;
- The gauge pressure at the feed side of the RO membrane is never lower than the gauge pressure at the permeate side, thereby preserving the integrity of the membrane;
- Operative pressures and workloads in various parts of the desalination plant practically do not change during cleaning, thereby prolonging the operational life of the equipment;
- The output of the High-Pressure Pumping group in the desalination plant practically does not change during a cleaning operation which allows to save energy and reduce wear of the pumps and motors.
- The utilization of pressure energy is close to ideal. Part of the energy spent for separation of the permeate from the brine is restored in the cleaning process: When permeate or second-stage brine penetrates through the membrane to the feed side with higher osmotic pressure, it acquires the higher gauge pressure of the feed side (at the cost of decreasing the osmotic pressure at the same side). Then this higher pressure of the permeate is utilized in the energy recovery plant.
- The method allows brine from intermediate stages of the desalination process to be utilized more effectively.
- In order to understand the invention and to see how it may be carried out in practice, preferred embodiments will now be described, by way of non-limiting examples only, with reference to the accompanying drawings, in which:
- FIG. 1 is a scheme of a prior art desalination plant with a plurality of RO modules;
- FIG. 2 is a schematic longitudinal section of a RO membrane in a RO module in prior art normal desalination process;
- FIG. 3 is a schematic longitudinal section of a RO membrane in a RO module in the direct osmosis cleaning process of the present invention;
- FIG. 4 is a scheme of the desalination plant of FIG. 1 equipped with a cleaning system of the present invention.
- FIG. 5 is a schematic cross-section of a RO membrane in a RO module; and
- FIG. 6 is a schematic longitudinal section of a RO membrane in a RO module in a variation of the direct osmosis cleaning process.
- FIG. 7 is a scheme of the desalination plant of FIG. 1 equipped with a “cyclic” cleaning system of the present invention.
- With reference to FIG. 1, there is shown a prior
art desalination plant 10 comprising a plurality ofmodules 12 for RO separation connected in parallel, a high-pressure pumping group (HPP) 14 with variable frequency drive (VFD) 16, energy recovery group (ERG) 17 and interconnecting piping and control means as explained below. With reference also to FIG. 2, eachRO module 12 has anelongated housing 18 with front end and rear end. ARO membrane 20 extends between the front end and the rear end dividing the internal volume of the housing into feed side and permeate side (FIG. 2 is simplified, the membrane may be pleated/folded and rolled into a rather complex shape, as shown in FIG. 5). Themembrane 20 has, consequently, feedside surface 21 and permeateside surface 22. Thehousing 18 has front-end feed port 24 and rear-end brine port 26 in communication with the feed side of themembrane 20, and front-end permeate port 28 and rear-end permeate port 30 in communication with the permeate side of the membrane. - The
desalination plant 10 further comprises a common high-pressure feed collector 34 connectingHPP 14 to the front-end feed ports 24 of themodules 12 via highpressure feed lines 35; a common high-pressure brine collector 36 connected to the rear-end brine ports 26 of themodules 12 via high-pressure brine lines 37; commonrear permeate collector 38 connected to the rear-end permeate ports 30 viarear permeate lines 39; and commonfront permeate collector 40 connected to the front-end permeate ports 28 via front permeate lines 42. - The
ERG 17 comprises a group ofwork exchangers 50, acirculation pump 52 connected to thefeed collector 34, high-pressure brine inlet 54 connected to thebrine collector 36, low-pressurebrine discharge outlet 55, and low-pressure feed inlet 56. - The
desalination plant 10 is connected to a source of raw solution (seawater) such as water pretreatment stage (not shown) at the inlet of theHPP 14 and at thefeed inlet 56 of theERG group 17. Outlets ofpermeate collectors valves 58 connect the rear-end brine port 26 to the rear-end permeate port 30 of eachRO module 12 so as to prevent increasing of the pressure at the permeate side over the pressure at the feed side. A plurality ofvalves - A normal RO separation process in the
desalination plant 10 will now be described, with specific pressure values given only as a non-limiting example. - Pretreated seawater with osmotic pressure PO=33 bar is supplied to the suction side of
HPP 14 and thefeed inlet 56 ofERG 17. High-pressure feed water supplied from HHP and ERG under gauge pressure PF1=65 bar enters the high-pressure feed collector 34 and, via high-pressure feed lines 35 and front-end feed ports 24 enters the feed side ofRO modules 12. The excess pressure AP=PF1-PO1=32 bar drives the water to the permeate side of the RO membrane. The obtained permeate product has low TDS content and low osmotic pressure PO2≈0.3 bar. The permeate is withdrawn from the permeate side under gauge pressure PP2≈2 bar. Hence, the net driving differential across the membrane is: - ΔPN=
PF 1−PO 1−PP 2+PO 2≈30.3 bar - The feed water salinity and osmotic pressure increase as the feed water flows towards the rear end of the module while the gauge pressure falls due to hydraulic losses. Therefore, the net driving differential falls, and the permeate salinity varies along the membrane. Thus, the obtained permeate can be divided into front permeate (lower TDS) transferred via
front permeate collector 40, and rear permeate (higher TDS) transferred viarear permeate collector 38. - The seawater that reaches the rear end of the feed side is high-salinity brine with osmotic pressure PO3=58 bar. It exits the
RO module 12 under gauge pressure PB3=64 bar via the rear-end brine port 26, high-pressure brine line 37, enters the high-pressure brine collector 36 and is passed to theERG 17. In the ERG, the high pressure of the brine is transferred to the feed water while the brine is discharged through theoutlet 55. - The seawater usually contains potential foulants such as suspended particles, organic molecules, live microorganisms or dissolved salts which may form scale. During the process of separation, the
foulants 64 accumulate at the feed side of the RO membrane contaminating it, reducing its permeability and increasing the hydraulic losses. - With reference to FIGS. 3 and 4, the system and the method of the present invention for cleaning fouled RO membranes by direct osmosis will be described in detail. FIG. 4 shows the inventive cleaning system integrated with the
desalination plant 10 of FIG. 1. The latter has additionally a second-stage RO module 68 with middle-pressure pump 70. The second-stage module 68 receives rear-end product (permeate) from thepermeate collector 38 of the first stage described above, transfers the second-stage permeate 71 to thefront permeate collector 40, and discharges residual brine to drain 72 throughvalve 73. - The system for cleaning fouled RO membranes by direct osmosis comprises:
- a) a pressurized source of dilute saline solution such as brine from the second-
stage RO module 68 with a cleaningbooster pump 78 having avariable frequency drive 79; - b) a high-
pressure cleaning collector 80 connecting therear permeate ports 30 of theRO modules 12 to the source of dilute saline solution; - c) a
cleaning brine collector 82 connected to front-end feed ports 24 of the RO modules; - d) a cleaning
booster brine pump 84 with inlet connected to thebrine collector 82, and outlet connected to the high-pressure brine collector 36; - e) drains85 at the front-
end permeate ports 28 of eachmodule 12; and - f) a plurality of
valves - The inventive cleaning method, applied for example to the
RO module 12A, works in the following way: - a) stop-
valves module 12A are closed, while the same valves on the other RO modules are opened (closed valves are drawn in solid black in FIG. 4), whereby themodule 12A quits the normal RO process; - b) stop-
valve 62A remains opened, whereby the rear-end brine port of themodule 12A remains connected to the high-pressure brine collector 36; - c) stop-
valve 87A is opened and the cleaningbooster brine pump 84 is operated, whereby the brine starts to circulate through the feed side of themodule 12A in reverse direction; - d) the
cleaning booster pump 78 is operated to feed second-stage brine to the permeate side of the RO membrane in themodule 12A; and - e) the
valve 86A is opened to drain the remaining second-stage brine from the permeate side. - FIG. 3 explains in further detail the cleaning process on the RO membrane (the pressure values are only exemplary). The second-stage brine (Brine2) has osmotic pressure PO4=13 bar and is fed to the permeate side under gauge pressure PD4=33 bar. The first-stage brine (Brine 1) at the feed side has osmotic pressure PO5=PO3=58 bar and gauge pressure PC5=PB3=64 bar, as in the normal RO process described with reference to FIG. 2. The net driving differential ΔPN is now:
- ΔPN=PC 5−PO 5−
PD 4+PO 4≈−14 bar - ΔPN is directed to the feed side, whereby the water is sucked from the permeate side of the RO membrane to the feed side. The water penetrates into the interface between the membrane and the accumulated
foulants 64, and separates the foulants from the membrane surface. The first-stage brine, together with the foulants and the penetrated water (Brine 1′) is withdrawn through the front-end feed port 24 under gauge pressure which is less than PB3 due to hydraulic losses in the flow along the membrane. Thebooster brine pump 84 restores these losses and feeds the brine to the common high-pressure brine collector 36 for passing to theEGR 17. The net driving differential can be adjusted by regulating the pressure PD4 by means of theVFD 79. - It will be appreciated that in the operation of the desalination plant, the direct-osmosis cleaning method of the present invention can be applied in turn to each
RO module 12 by switching of valves, without interrupting the desalination process. Advantageously, the penetrating water acquires higher gauge pressure at the feed side, PC5, and this pressure is later returned to the system in theenergy recovery group 17. In this way, part of the energy spent for separation of the permeate from the brine, and preserved in the form of higher osmotic pressure of the latter, is restored in the cleaning process. - The dilute solution which is used as source of water in the cleaning process may be taken also from other stages of the desalination plant, or from other sources. FIG. 4 shows (in phantom line) that rear permeate stored in
tank 76 may be used instead of second-stage brine. Raw seawater may be used as concentrated solution at the feed side instead of brine. For example, seawater from theERG 17 may be taken before thebooster pump 52 and used in the cleaning process. Cleaning agent (not shown) can be added to the dilute solution, or to the concentrated solution, or to both. - In the inventive method, the gauge pressure at the feed side PC5 is between the feed
water pressure PF 1 and the osmotic pressure of thefeed water PO 1 in the normal RO process. The gauge pressure PD4 at the permeate side is significantly higher than the gauge pressure PP2i in the normal RO process, so as to provide ΔPN directed to the feed side. The net driving differential ΔPN is lower than the osmotic pressure of the saline solution at the feed side, thereby avoiding the “catastrophic” filtration described in the Background. - The latter advantage is illustrated in FIG. 5, showing schematically the cross- section of the
RO module 12. TheRO membrane 20 is pleated, with highlypermeable spacer material tube 95 and is inserted in themodule housing 18. Thetube 95 is perforated and constitutes apermeate channel 96 connecting the front-end permeate port 28 and the rear-end permeate port 30 to the permeate side of theRO membrane 20. It can be seen that the dilute solution (permeate) can easily reach membrane parts adjacent to thepermeate channel 96, such as in zone I. However, it will take much time and hydraulic losses for the dilute solution to reach remote membrane parts in the peripheral zone II. The present method allows the net driving differential ΔPN to be regulated so that the dilute saline solution can reach the remote parts of the membrane before the water is entirely sucked to the feed side of the membrane through the parts adjacent to thepermeate channel 96. - The efficiency of the present method may be enhanced in the following ways:
- Alternating from time to time the feeding and the withdrawing of the concentrated saline solution between the front-
end feed port 24 and the rear-end brine port 26, for example by reversing thebooster pump 84; - Application of pulsating gauge pressure PD4, for example by means of the
VFD 79; and - Changing from time to time the gauge pressure PD4 and/or PC5 so that the net pressure differential ΔPN is reversed towards the permeate side, whereby the RO module will perform in alternating manner direct osmosis cleaning and normal RO separation process.
- It will be appreciated that, as the concentrated solution flows along the feed side of the membrane, for example from the rear end towards the front end (
Brine 1 in FIG. 3), and takes up water, its osmotic pressure PO5 diminishes. Thereby, the net driving differential ΔPN diminishes also and the membrane cleaning may become non-uniform if not stop at all. In the following embodiment, the cleaning method of the present invention is improved to overcome this disadvantage. For this purpose, a source of second dilute solution is provided, with osmotic pressure PO4′ lower than PO4. This may be, for example, the rear-end permeate with PO4′≈0.3 bar from thetank 76 shown in FIG. 4. Another high-pressure pump, a cleaning collector and valves (not shown) are added to connect thefront permeate ports 28 of theRO modules 12 to the source of second dilute saline solution. - The operation of the improved method is illustrated in the schematic view of FIG. 6. It differs from the operation shown in FIG. 3 in that the second dilute solution (Rear permeate) is fed to the permeate side via the front-
end permeate port 28 under the same gauge pressure PD4. If, for example, theconcentrated solution Brine 1′ at the front end of the feed side becomes so diluted that its osmotic pressure falls to PO5′=44 bar, then the net driving differential ΔPN will vanish and the water penetration through the membrane will stop. However, by feeding rear permeate through the front-end permeate port 28, we obtain new net differential: - ΔPN′=PC 5−PO 5′−
PD 4+PO 4′≈64−44−33+0.3=−12.7 bar - Thereby, the water penetration and the cleaning process are effectively restored.
- Using the principle of alternating RO and direct osmosis, as described above, the method of the present invention may be simplified to “rinsing” of fouled RO membranes without stopping the operation of the RO module. The “rinsing” method comprises:
- a) lowering the average gauge pressure of the feed PF1 to a level about the osmotic pressure PO1 so that the average net driving differential ΔPN resulting from pressures PO1, PO2, PP2, and PF1 is close to zero;
- b) Varying the instant gauge pressure of the feed PF1′ about the average value PF1, so that the instant net driving differential ΔPN′ is directed alternatively to the feed side and to the permeate side of the membrane. Thereby, when the ΔPN′ is directed to the feed side, the direct-osmosis cleaning process is performed, while when the ΔPN′ is directed to the permeate side, the RO membrane performs normal RO separation;
- b) withdrawing the raw saline solution together with the separated foulant through the rear-end brine port; and
- c) feeding the raw saline solution with the foulant to the ERG.
- It would be appreciated that the simplified “rinsing” method may be performed on all RO modules simultaneously, by a short time interruption of permeate product production. The “rinsing” method is not so efficient as the basic cleaning method of the present invention but it can be applied to the
desalination plant 10 without adding any new equipment. - Another simplified system performing an effective “cyclic” version of the same direct-osmosis cleaning process is illustrated in FIG. 7. The simplified cyclic cleaning system is integrated, as before, in the
desalination plant 10 of FIG. 1, but does not involve connections to next RO stages, and comprises only: - a) a pressure-
exchange vessel 103 storing a limited quantity of permeate from the first-stage RO modules 12; - b) a high-
pressure cleaning collector 105 connecting the permeate ports of theRO modules 12 to the pressure-exchange vessel 103; and - c)
valves 107 adapted to close or open each of the permeate ports to thecleaning collector 105, so as to allow performing of the normal separation process and the simplified cyclic cleaning method on each RO module in turn. - The pressure-
exchange vessel 103 has a feed-water chamber 109 and apermeate chamber 111 divided by aflexible diaphragm 113. Thepermeate chamber 111 is in communication with thecleaning collector 105 while the feed-water chamber 109 is connected to the high-pressure feed collector 34 via a stop-valve 115, and to a drain pipe 119 via a drain valve 117. Thepermeate collector 38 and thevalves 61 connecting it to the RO modules are adapted to work under the high pressure of thefeed collector 34. - The cyclic cleaning process, applied for example to the
RO module 12A, works in the following cleaning cycle: - a) Stop-
valve 61A associated with themodule 12A is closed, whereby themodule 12A quits the normal RO separation process; - b) Stop-
valves water chamber 109 and displaces thediaphragm 113 and the permeate from thechamber 111 towards the permeate side of theRO module 12A. The cleaning sequence is finished when thechamber 111 collapses to a minimum volume or the stop-valve 115 is closed; - Then a reverse sequence is performed:
- c) The stop-
valve 115 is closed while the drain valve 117 and the stop-valve 61A are opened, whereby the RO module resumes the normal RO separation process. A portion of the permeate fills thepermeate chamber 111 and displaces the feed water from thechamber 109 through the drain pipe 119; and - d) The
valve 107A is closed when the pressure-exchange vessel 103 is filled with permeate, whereby the system is ready for a next cleaning cycle. - All the time stop-
valves feed collector 34 to thebrine collector 36 is not interrupted. - At the step (c), the gauge pressures at the feed side and at the permeate side of the membrane are equalized. However, the osmotic pressure in the permeate channel is much lower than in the feed-brine channel, whereby the net driving differential ΔPN is reversed towards the feed side, and the permeate passes back through the membrane separating the foulant therefrom. The mobilized foulant is carried away with the high-pressure flow through the
brine collector 36 and is drained through theERG 17. Due to the high gauge pressure in the permeate channel, the sucked-back water has sufficient energy to reach the remote areas of the membrane. - It will be appreciated that the
diaphragm 113 is needed only to separate the permeate from the feed water in the pressure-exchange vessel 103. Instead, cylinder with a plunger may be used, similar to workexchangers 50. Thevalve 115 may be complemented with a pressure regulator to control the driving differential ΔPN if necessary. The drained feed water may be returned back to the suction side of theHPP 14. The pressure-exchange vessel 103 may use, as a source of high-pressure fluid, not only thefeed collector 34 but also thebrine collector 36. The high-pressure cleaning collector 105 may be connected to either permeate port (front or rear), or to both. - The cyclic process allows cleaning the membranes without depressurization of the RO modules and without stopping the feed-brine flow and the flow towards the energy recovery plant. Advantageously, it does not use another pressure source besides the pressure of the feed flow, and does not require a variable frequency drive or other complicated control of the HPP output. Due to the same reason, the gauge pressure in the permeate channel cannot exceed the gauge pressure in the feed channel, so that the
check valves 58 become unnecessary. The available quantity of permeate for one cleaning cycle is limited by the volume of thepressurization cylinder 103 but the cycle may be repeated as necessary. - Although a description of specific embodiments has been presented, it is contemplated that various changes could be made without deviating from the scope of the present invention. For example, the cleaning method of the present invention may be used for cleaning nanofiltration and ultrafiltration membranes. It can be applied to single RO modules, and can be used with any type of energy recovery device, such as Pelton turbine, Francice turbine, or work exchanger.
Claims (35)
1. A method of cleaning a fouled RO membrane in a module for RO separation, said membrane having a feed side and an opposite permeate side and extending between a front end and a rear end of said module, said module having a front-end feed port and a rear-end brine port in communication with said feed side of the membrane, and at least one permeate port in communication with said permeate side of the membrane, a normal RO separation process in the same module including feeding raw saline solution, which comprises solvent, dissolved salts and a potential foulant, with osmotic pressure PO1, to said front-end feed port at gauge pressure PF1>PO1, collecting weak saline solution called permeate from said permeate port at gauge pressure PP2, and removing residual brine from said rear-end brine port at gauge pressure PB3>PO1, the foulant accumulating at the feed side of the RO membrane, said cleaning method comprising
a) feeding dilute saline solution to the permeate side of the RO membrane under gauge pressure PD4 and osmotic pressure PO4;
b) feeding concentrated saline solution to the feed side of the RO membrane under gauge pressure PC5 and osmotic pressure PO5, a net driving differential ΔPN resulting from pressures PO4, PD4, PO5, and PC5 being directed to the feed side, whereby the solvent is being sucked from the permeate side of the RO membrane to the feed side of the RO membrane, penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface; and
c) withdrawing the concentrated saline solution together with the separated foulant and the penetrated solvent from the feed side of the RO membrane,
wherein
said gauge pressure PC5 is between said pressures PF1 and PO1 in the normal RO process, while said ΔPN directed to the feed side is provided by raising said gauge pressure PD4 with respect to said gauge pressure PP2 in the normal RO process.
2. The method of claim 1 , wherein said concentrated saline solution of step (b) is residual brine supplied from another RO module performing normal RO separation process, or is said raw saline solution.
3. The method of claim 1 , wherein said dilute saline solution of step (a) is the permeate obtained in the same RO module during its normal separation process and stored, or is permeate obtained from another RO module performing normal RO separation process.
4. The method of claim 3 , wherein said concentrated saline solution of step (b) is said raw saline solution and said gauge pressure PD4 is equal to said gauge pressure PC5.
5. The method of claim 4 , wherein said raw saline solution and said permeate are fed to the respective side of the membrane by the same pressure source that provides the gauge pressure PF1 of the normal RO process.
6. The method of claim 1 , wherein said RO module is a first-stage module in a multi-stage desalination plant and said dilute saline solution of step (a) is residual brine obtained in a next-stage separator of the same desalination plant.
7. The method of claim 1 , wherein said permeate side of the RO membrane communicates with said permeate port through a permeate channel, said RO membrane having parts near said permeate channel and parts remote therefrom, and said net driving differential ΔPN is such that it allows said dilute saline solution to reach said remote parts of the RO membrane before said solvent is entirely sucked to the feed side of the membrane through said near parts thereof.
8. The method of claim 1 , wherein said concentrated saline solution is fed to said rear-end brine port at step (b), and is withdrawn from said front-end feed port at step (c).
9. The method of claim 1 , wherein said concentrated saline solution is fed to said front-end feed port at step (b), and is withdrawn from said rear-end brine port at step (c).
10. The method of claim 1 , wherein the feeding at step (b) and the withdrawing at step (c) of the concentrated saline solution are from time to time alternated between said front-end feed port and said rear-end brine port.
11. The method of claim 1 , wherein said gauge pressure PD4 is pulsating.
12. The method of claim 1 , wherein at least one of said gauge pressures PD4 and PC5 is from time to time changed so that said net pressure differential ΔPN is reversed towards the permeate side, whereby the RO module performs, in said time to time, normal RO separation process.
13. The method of claim 1 , wherein said RO module has a front-end permeate port and a rear-end permeate port in communication with said permeate side of the RO membrane, the feeding in said steps (a) and (b) being performed through the same-end port of the respective side, the method further comprising:
a′) feeding a second dilute saline solution to the other-end permeate port under gauge pressure PD4 and osmotic pressure PO4′<PO4, said pressure PO4′ compensating for a fall of the net driving differential ΔPN due to a fall of osmotic pressure at the feed side as the concentrated saline solution flows from said same-end feed port towards said other-end feed port.
14. The method of claim 1 , including adding a cleaning agent to the dilute saline solution of step (a) and/or to the concentrated saline solution of step (b).
15. The method of claim 1 , including d) feeding the concentrated saline solution obtained in step (c) to an energy recovery plant.
16. The method of claim 15 , wherein said RO module is one of a plurality of RO modules, the rest of said plurality of RO modules performing normal RO 25 separation process, said concentrated saline solution of step (b) is a portion of the residual brine removed from said rest of RO modules, and the method is applied in turn to each RO module of said plurality.
17. The method of claim 16 , wherein at least a portion of the removed residual brine from said rest of RO modules is fed to said energy recovery plant at pressure PR, and the step (d) includes boosting the pressure of the concentrated saline solution withdrawn at step (c) up to said pressure PR.
18. A system for cleaning fouled RO membranes according to the method of claim 1 in a desalination plant comprising a plurality of modules for RO separation with said RO membranes connected in parallel and adapted to perform the normal separation process of claim 1 , the desalination plant further comprising a source of said raw solution with high-pressure feed pump; a common high-pressure raw solution feed line connecting the front-end feed ports of the modules to said source of raw solution; a common high-pressure brine collection line connecting the rear-end brine ports of the modules to a first brine discharge outlet; a common permeate collection line connecting the permeate ports of the modules to a product storage tank or a next-stage separator,
said system comprising:
a) a pressurized source of said dilute saline solution providing said pressure PD4;
b) a common high-pressure cleaning line connecting the permeate ports of said modules to said pressurized source of dilute saline solution;
c) a pressurized source of said concentrated saline solution providing said pressure PC5;
d) a first line to connect said source of concentrated saline solution to said feed side of the membrane in each RO module;
e) a second line to withdraw said concentrated saline solution from said feed side of the membrane in each RO module; and
f) a plurality of valves adapted to close or open each of the above ports and common lines so as to allow performing of said normal separation process and said method of claim 1 on each RO module in turn;
19. The cleaning system of claim 18 , wherein said first line is said common high-pressure brine collection line, said second line is a common line connecting front-end feed ports of said RO modules to a second brine discharge outlet, and said system is adapted to use a portion of the collected brine as concentrated saline solution in the step (b) of the method, and to discharge said portion of brine through said second brine discharge outlet in step (c) of the method.
20. The cleaning system of claim 18 , wherein said first line is said common high-pressure raw solution feed line, said second line is said common high-pressure brine collection line, and said system is adapted to use a portion of the raw solution as concentrated saline solution in the step (b) of the method, and to discharge said portion of raw solution through said first brine discharge outlet in step (c) of the method.
21. The cleaning system of claim 18 , wherein said desalination plant is a multi-stage plant, said plurality of RO modules is a first stage thereof, and the desalination plant further comprises
e) a next-stage separator with a next-stage brine outlet and next-stage booster pump in communication with said next-stage brine outlet;
f) a common next-stage brine line connecting the permeate ports of said plurality of modules to said next-stage booster pump; and
g) suitable valves allowing using said next-stage brine as dilute saline solution at step (a) of the method of claim 1 applied in turn to each module of said plurality of modules.
22. The cleaning system of claim 21 , wherein said next-stage separator has an inlet connected to said common permeate collection line, and is adapted to perform separation over the permeate from said first stage, thereby obtaining said next-stage brine.
23. The cleaning system of claim 18 , wherein each one of said plurality of modules has a front-end permeate port and a rear-end permeate port in communication with the permeate side of the RO membrane, said common permeate collection line being connected to said rear-end permeate port of each module, the system further comprising
g) a second source of second dilute saline solution;
h) a common line connecting said front-end permeate ports of said modules to said second source; and
i) a plurality of valves and pumps adapted to close or open each of the above ports and common lines and to feed each of said dilute saline solutions to a predetermined front-end or rear-end permeate port of each of said RO modules in predetermined order and under predetermined pressure.
24. The cleaning system of claim 18 , further comprising a tank with cleaning agent, a line connecting said tank to said source of dilute saline solution, and a feeding means adapted to feed said cleaning agent to said source of dilute saline solution.
25. The cleaning system of claim 18 , further comprising a tank with cleaning agent, a common line connecting said tank to said front-end feed ports of said modules or/and to said rear-end brine ports of said modules, and feeding means adapted to feed said cleaning agent to selected ones of said feed ports together with the concentrated saline solution during step (b) of the cleaning method.
26. The cleaning system of claim 18 , wherein said desalination plant includes an energy recovery plant connected to said first brine discharge outlet, said cleaning system further comprising a booster pump with inlet port connected to said second line and outlet port connected to said common brine collection line.
27. The cleaning system of claim 18 , wherein said pressurized source of dilute saline solution is a permeate storage tank.
28. The cleaning system of claim 27 , wherein said permeate storage tank is pressurized by means of a high-pressure feed pump.
29. The cleaning system of claim 27 , wherein said permeate storage tank is a pressure-exchange vessel having a permeate chamber and a feed chamber divided by a moveable impermeable wall, the permeate chamber being connected to said common high-pressure cleaning line, the feed chamber being connected via a first stop valve to a high-pressure fluid source and via a second stop valve to a discharge line, so that said vessel can be filled with high-pressure fluid to discharge the permeate under high pressure via said cleaning line, and can be filled with permeate to discharge said fluid through said discharge line.
30. The cleaning system of claim 29 , wherein said high-pressure fluid source is said common high-pressure raw solution feed line.
31. The cleaning system of claim 29 , wherein said high-pressure fluid source is said common high-pressure brine collecting line.
32. The cleaning system of claim 29 , wherein said moveable impermeable wall is a flexible diaphragm.
33. The cleaning system of claim 29 , wherein said moveable impermeable wall is a sliding sealed piston.
34. A method of cleaning a fouled RO membrane in a module for RO separation, said membrane having a feed side and an opposite permeate side and extending between a front end and a rear end of said module, said module having a front-end feed port and a rear-end brine port in communication with said feed side of the membrane, and at least one permeate port in communication with said permeate side of the membrane, a normal RO separation process in the same module including feeding raw saline solution, which comprises solvent, dissolved salts and a potential foulant with osmotic pressure PO, to said front-end feed port at gauge pressure PF1>PO1, collecting weak saline solution called permeate with osmotic pressure PO2 from said permeate port at gauge pressure PP2, and removing residual brine from said rear-end brine port, the foulant accumulating at the feed side of the RO membrane, wherein said cleaning method comprises
a) changing said gauge pressure PF1 to a pulsating gauge pressure PF1′ with average value close to said osmotic pressure PO so that a net driving differential ΔPN resulting from pressures PO1, PO2, PP2, and PF1′ would be directed alternatively to the feed side and the permeate side of the membrane, whereby, when said ΔPN is directed to said feed side, the solvent is being sucked from the permeate side of the RO membrane to the feed side of the RO membrane, penetrates into the interface between the membrane and the accumulated foulant, and separates the foulant from the membrane surface, while when said ΔPN is directed to said permeate side, the RO membrane performs normal RO separation; and
b) withdrawing the raw saline solution together with the separated foulant through said rear-end brine port.
35. The method of claim 34 , including
c) feeding the raw saline solution obtained in step (b) to an energy recovery plant.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US11/748,234 US7563375B2 (en) | 2003-01-09 | 2007-05-14 | Direct osmosis cleaning |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IL153870 | 2003-01-09 | ||
IL15387003A IL153870A0 (en) | 2003-01-09 | 2003-01-09 | Direct osmosis cleaning |
IL15758103A IL157581A (en) | 2003-01-09 | 2003-08-26 | Direct osmosis membrane cleaning |
IL157581 | 2003-08-26 |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US11/748,234 Division US7563375B2 (en) | 2003-01-09 | 2007-05-14 | Direct osmosis cleaning |
Publications (1)
Publication Number | Publication Date |
---|---|
US20040134521A1 true US20040134521A1 (en) | 2004-07-15 |
Family
ID=32715247
Family Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US10/718,539 Abandoned US20040134521A1 (en) | 2003-01-09 | 2003-11-24 | Direct osmosis cleaning |
US11/748,234 Expired - Lifetime US7563375B2 (en) | 2003-01-09 | 2007-05-14 | Direct osmosis cleaning |
Family Applications After (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US11/748,234 Expired - Lifetime US7563375B2 (en) | 2003-01-09 | 2007-05-14 | Direct osmosis cleaning |
Country Status (5)
Country | Link |
---|---|
US (2) | US20040134521A1 (en) |
AU (1) | AU2003283788B2 (en) |
ES (1) | ES2288388B1 (en) |
IL (1) | IL157581A (en) |
WO (1) | WO2004062774A2 (en) |
Cited By (20)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2430196A (en) * | 2005-09-28 | 2007-03-21 | Bp Exploration Operating | Cleaning a membrane of a reverse osmosis desalination plant |
WO2007073207A1 (en) * | 2005-12-22 | 2007-06-28 | Statkraft Development As | A method and a system for performing maintenance on a membrane used for pressure retarded osmosis |
US20100038292A1 (en) * | 2008-08-15 | 2010-02-18 | H2O, Inc. | Apparatus for Desalination and Pressure Washing |
NL1038485A (en) * | 2010-08-10 | 2012-07-03 | Boekhoudt | AN INNOVATIVE ENVIRONMENTALLY-FRIENDLY CHEMICAL-FREE OSMOTIC CLEANING PROCESS FOR CLEANING SWRO AND BWRO MEMBRANES IN OPERATION. |
WO2012104684A1 (en) * | 2011-02-01 | 2012-08-09 | I.D.E. Technologies Ltd. | Chemical free and energy efficient desalination system |
WO2014037940A1 (en) * | 2012-09-04 | 2014-03-13 | Israel Aerospace Industries Ltd. | System and method for treatment of water |
US20150060359A1 (en) * | 2012-04-18 | 2015-03-05 | Chang Wang | Spiral wound membrane element and method for cleaning spiral wound membrane sheet |
GB2529179A (en) * | 2014-08-12 | 2016-02-17 | Membrane Recovery Ltd | Forward osmotic and water hammer method of membrane cleaning |
WO2017132301A1 (en) * | 2016-01-29 | 2017-08-03 | Massachusetts Institute Of Technology | Batch pressure-driven membrane liquid separation using pressure exchanger for enhanced efficiency |
WO2017136048A1 (en) * | 2016-02-02 | 2017-08-10 | Trevi Systems Inc. | Osmotic pressure assisted reverse osmosis process and method of using the same |
KR101785354B1 (en) | 2013-06-03 | 2017-10-17 | 아이.디.이. 테크놀로지스 엘티디. | Method of Operating a Pressure-Retarded Osmosis Plant |
WO2018167767A1 (en) * | 2017-03-14 | 2018-09-20 | Desalitech Ltd | Integrated reverse osmosis and membrane cleaning systems for fouling prevention |
ES2708126A1 (en) * | 2017-10-06 | 2019-04-08 | Moro Maria Teresa Bergaz | METHOD FOR THE TREATMENT OF WILD OR SEA WATER THROUGH REVERSE OSMOSIS (Machine-translation by Google Translate, not legally binding) |
CN110184788A (en) * | 2019-06-25 | 2019-08-30 | 德仕科技(深圳)有限公司 | Cleaning system for balanced ring for washing machine salt water injection device |
US20200261850A1 (en) * | 2017-11-06 | 2020-08-20 | Sandymount Technologies Corporation | Flow Control in Large-numbered, Series-coupled Vessels of Reverse Osmosis Systems |
WO2021072345A1 (en) * | 2019-10-11 | 2021-04-15 | Massachusetts Institute Of Technology | Deformation-enhanced cleaning of fouled membranes |
US11117813B1 (en) | 2020-03-18 | 2021-09-14 | Crosstek Membrane Technology | Techniques for managing scale formation in water filtration systems and a reverse osmosis (RO) and nanofiltration (NF) system implementing same |
WO2021188132A1 (en) * | 2020-03-18 | 2021-09-23 | Crosstek Membrane Technology | Techniques for managing scale formation in water filtration systems and a reverse osmosis (ro) and nanofiltration (nf) system implementing same |
US11739968B2 (en) | 2013-03-15 | 2023-08-29 | Google Llc | Controlling an HVAC system using an optimal setpoint schedule during a demand-response event |
WO2024086897A1 (en) * | 2022-10-27 | 2024-05-02 | C2 Water (SPV) Pty Ltd | A method for reducing accumulation of foulants on reverse osmosis membranes and a groundwater desalination system |
Families Citing this family (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU2005254337B2 (en) | 2004-06-21 | 2010-04-15 | Membrane Recovery Ltd | Ro membrane cleaning method |
WO2009037515A2 (en) * | 2007-09-20 | 2009-03-26 | Abdulsalam Al-Mayahi | Process and systems |
US20100155333A1 (en) * | 2008-12-18 | 2010-06-24 | Chevron U.S.A., Inc. | Process for dewatering an aqueous organic solution |
PE20121097A1 (en) * | 2009-07-09 | 2012-09-13 | Ide Technologies Ltd | DESALINATION SYSTEM |
US9457320B2 (en) | 2011-06-20 | 2016-10-04 | King Abdullah University Of Science And Technology | Processes and apparatus for inhibiting membrane bio-fouling |
US9943807B2 (en) | 2011-09-19 | 2018-04-17 | Chen Wang | Spiral wound membrane with bi-directional permeate flow |
WO2014062932A1 (en) * | 2012-10-17 | 2014-04-24 | Nuwater Resources International, Llc | Semipermeable membrane and process using the same |
WO2014068572A2 (en) | 2012-11-01 | 2014-05-08 | Israel Aerospace Industries Ltd. | Manufacture of integrated structures formed of composite materials |
KR101516058B1 (en) * | 2012-12-12 | 2015-04-30 | 현대중공업 주식회사 | Reverse osmosis membrane module-specific pressure controlled osmotic backwash system |
US8983171B2 (en) | 2012-12-26 | 2015-03-17 | Israel Aerospace Industries Ltd. | System and method for inspecting structures formed of composite materials during the fabrication thereof |
CN103908897A (en) * | 2013-01-04 | 2014-07-09 | 天津工业大学 | Separation membrane operation method and system applying separation membrane operation method |
KR101642393B1 (en) | 2013-03-28 | 2016-07-26 | 현대중공업 주식회사 | Reverse osmosis membrane train-specific osmotic backwash system and method |
KR101516080B1 (en) * | 2013-09-30 | 2015-04-30 | 현대중공업 주식회사 | Reverse osmosis membrane train-specific pressure controlled osmotic backwash system and its method |
KR101614390B1 (en) * | 2014-05-19 | 2016-04-22 | 현대중공업 주식회사 | Reverse osmosis membrane module-specific osmotic backwash system |
US10214430B2 (en) | 2015-03-04 | 2019-02-26 | Israel Aerospace Industries Ltd. | Water treatment system and method |
CN110944736A (en) * | 2017-08-03 | 2020-03-31 | 巴斯夫欧洲公司 | Method of cleaning a membrane including drying the membrane |
WO2019116073A1 (en) | 2017-12-11 | 2019-06-20 | I.D.E. Technologies Ltd | Membrane cleaning method and apparatus |
US10947143B2 (en) | 2019-04-01 | 2021-03-16 | Saline Water Conversion Corporation | Desalination brine concentration system and method |
WO2021034332A1 (en) | 2019-08-22 | 2021-02-25 | Saline Water Conversion Corporation | Multi-valent ion concentration using multi-stage nanofiltration |
US11638903B2 (en) | 2019-10-11 | 2023-05-02 | Massachusetts Institute Of Technology | Deformation-enhanced cleaning of fouled membranes |
US11806668B2 (en) | 2021-12-14 | 2023-11-07 | Saline Water Conversion Corporation | Method and system for extraction of minerals based on divalent cations from brine |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4141825A (en) * | 1977-10-31 | 1979-02-27 | Stone & Webster Engineering Corporation | Desalination process system and by-product recovery |
US4961851A (en) * | 1990-04-20 | 1990-10-09 | Barbachano Fernando G R | Self-cleaning reverse osmosis liquid treatment system, method and dual configuration check valve therefor |
US5354466A (en) * | 1992-09-16 | 1994-10-11 | Millipore Corporation | Filtration system with improved backwashing capability |
US5403479A (en) * | 1993-12-20 | 1995-04-04 | Zenon Environmental Inc. | In situ cleaning system for fouled membranes |
US6001254A (en) * | 1995-04-14 | 1999-12-14 | Aquasource | Method of operating and monitoring a group of filter membrane modules, and a group of modules implementing the method |
US6755970B1 (en) * | 1999-06-22 | 2004-06-29 | Trisep Corporation | Back-flushable spiral wound filter and methods of making and using same |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3853756A (en) * | 1973-02-12 | 1974-12-10 | Westinghouse Electric Corp | Reverse pressure cleaning of supported semipermeable membranes |
US5207916A (en) | 1992-05-20 | 1993-05-04 | Mesco, Inc. | Reverse osmosis system |
FR2697172B1 (en) * | 1992-10-26 | 1994-12-02 | Commissariat Energie Atomique | Process for automatic unclogging of an ultrafiltration or microfiltration unit and installation implementing the process. |
EP0768112A1 (en) * | 1995-10-16 | 1997-04-16 | Christ AG | Process and device for producing pure water |
JP2000079328A (en) | 1998-09-07 | 2000-03-21 | Nitto Denko Corp | Cleaning of reverse osmosis membrane module |
FR2811315A1 (en) * | 2000-07-10 | 2002-01-11 | Michel Duflos | Reverse osmosis water purification apparatus does not discharge or recycle water passing across membrane but accumulates it for directing forcefully at membrane to remove impurities |
-
2003
- 2003-08-26 IL IL15758103A patent/IL157581A/en not_active IP Right Cessation
- 2003-11-20 ES ES200550041A patent/ES2288388B1/en not_active Expired - Lifetime
- 2003-11-20 AU AU2003283788A patent/AU2003283788B2/en not_active Ceased
- 2003-11-20 WO PCT/IL2003/000984 patent/WO2004062774A2/en active IP Right Grant
- 2003-11-24 US US10/718,539 patent/US20040134521A1/en not_active Abandoned
-
2007
- 2007-05-14 US US11/748,234 patent/US7563375B2/en not_active Expired - Lifetime
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4141825A (en) * | 1977-10-31 | 1979-02-27 | Stone & Webster Engineering Corporation | Desalination process system and by-product recovery |
US4961851A (en) * | 1990-04-20 | 1990-10-09 | Barbachano Fernando G R | Self-cleaning reverse osmosis liquid treatment system, method and dual configuration check valve therefor |
US5354466A (en) * | 1992-09-16 | 1994-10-11 | Millipore Corporation | Filtration system with improved backwashing capability |
US5403479A (en) * | 1993-12-20 | 1995-04-04 | Zenon Environmental Inc. | In situ cleaning system for fouled membranes |
US6001254A (en) * | 1995-04-14 | 1999-12-14 | Aquasource | Method of operating and monitoring a group of filter membrane modules, and a group of modules implementing the method |
US6755970B1 (en) * | 1999-06-22 | 2004-06-29 | Trisep Corporation | Back-flushable spiral wound filter and methods of making and using same |
Cited By (42)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2430196A (en) * | 2005-09-28 | 2007-03-21 | Bp Exploration Operating | Cleaning a membrane of a reverse osmosis desalination plant |
KR101372901B1 (en) * | 2005-12-22 | 2014-03-10 | 스탯크래프트 에이에스 | A method and a system for performing maintenance on a membrane having semi-permeable properties |
WO2007073207A1 (en) * | 2005-12-22 | 2007-06-28 | Statkraft Development As | A method and a system for performing maintenance on a membrane used for pressure retarded osmosis |
US20090008330A1 (en) * | 2005-12-22 | 2009-01-08 | Statkraft Development As | Method and a System for Performing Maintenance on a Membrane Used for Pressure Retarded Osmosis |
US7972514B2 (en) | 2005-12-22 | 2011-07-05 | Statkraft Development As | Method and a system for performing maintenance on a membrane used for pressure retarded osmosis |
EA015391B1 (en) * | 2005-12-22 | 2011-08-30 | Статкрафт Дивелопмент Ас | A method and a system for performing maintenance on a membrane used for pressure retarded osmosis |
US20100038292A1 (en) * | 2008-08-15 | 2010-02-18 | H2O, Inc. | Apparatus for Desalination and Pressure Washing |
NL1038485A (en) * | 2010-08-10 | 2012-07-03 | Boekhoudt | AN INNOVATIVE ENVIRONMENTALLY-FRIENDLY CHEMICAL-FREE OSMOTIC CLEANING PROCESS FOR CLEANING SWRO AND BWRO MEMBRANES IN OPERATION. |
WO2012104684A1 (en) * | 2011-02-01 | 2012-08-09 | I.D.E. Technologies Ltd. | Chemical free and energy efficient desalination system |
US20130313190A1 (en) * | 2011-02-01 | 2013-11-28 | I.D.E. Technologies Ltd | Chemical free and energy efficient desalination system |
US9802849B2 (en) | 2011-02-01 | 2017-10-31 | I.D.E. Technologies Ltd. | Chemical free and energy efficient desalination system |
US10301206B2 (en) | 2011-02-01 | 2019-05-28 | I.D.E. Technologies Ltd | Chemical free and energy efficient desalination system |
US9162911B2 (en) * | 2011-02-01 | 2015-10-20 | I.D.E. Technologies Ltd. | Chemical free and energy efficient desalination system |
TWI584869B (en) * | 2012-04-18 | 2017-06-01 | 奇異電器公司 | Apparatus and method for bi-directional detect osmosis |
EP2838645A4 (en) * | 2012-04-18 | 2016-06-29 | Gen Electric | Spiral wound membrane element and method for cleaning spiral wound membrane sheet |
US10335739B2 (en) * | 2012-04-18 | 2019-07-02 | Bl Technologies, Inc. | Spiral wound membrane element and method for cleaning spiral wound membrane sheet |
US20150060359A1 (en) * | 2012-04-18 | 2015-03-05 | Chang Wang | Spiral wound membrane element and method for cleaning spiral wound membrane sheet |
WO2014037940A1 (en) * | 2012-09-04 | 2014-03-13 | Israel Aerospace Industries Ltd. | System and method for treatment of water |
US11739968B2 (en) | 2013-03-15 | 2023-08-29 | Google Llc | Controlling an HVAC system using an optimal setpoint schedule during a demand-response event |
KR101785354B1 (en) | 2013-06-03 | 2017-10-17 | 아이.디.이. 테크놀로지스 엘티디. | Method of Operating a Pressure-Retarded Osmosis Plant |
CN107073404A (en) * | 2014-08-12 | 2017-08-18 | 膜回收股份有限公司 | A kind of forward osmosis and the Membrane cleaning method of water slug |
EP3194056A4 (en) * | 2014-08-12 | 2018-04-11 | Membrane Recovery Ltd. | Forward osmotic and water hammer method of membrane cleaning |
US10005040B2 (en) | 2014-08-12 | 2018-06-26 | Membrane Recovery Ltd. | Forward osmotic and water hammer method of membrane cleaning |
AU2015302943B2 (en) * | 2014-08-12 | 2017-08-17 | Membrane Recovery Ltd. | Forward osmotic and water hammer method of membrane cleaning |
GB2529179A (en) * | 2014-08-12 | 2016-02-17 | Membrane Recovery Ltd | Forward osmotic and water hammer method of membrane cleaning |
US20170216774A1 (en) * | 2016-01-29 | 2017-08-03 | Massachusetts Institute Of Technology | Batch Pressure-Driven Membrane Liquid Separation Using A Pressure Exchanger for Efficiency |
WO2017132301A1 (en) * | 2016-01-29 | 2017-08-03 | Massachusetts Institute Of Technology | Batch pressure-driven membrane liquid separation using pressure exchanger for enhanced efficiency |
WO2017136048A1 (en) * | 2016-02-02 | 2017-08-10 | Trevi Systems Inc. | Osmotic pressure assisted reverse osmosis process and method of using the same |
US11198097B2 (en) | 2016-02-02 | 2021-12-14 | Trevi Systems Inc. | Osmotic pressure assisted reverse osmosis process and method of using the same |
EP3595799A4 (en) * | 2017-03-14 | 2021-01-27 | Desalitech Ltd | Integrated reverse osmosis and membrane cleaning systems for fouling prevention |
WO2018167767A1 (en) * | 2017-03-14 | 2018-09-20 | Desalitech Ltd | Integrated reverse osmosis and membrane cleaning systems for fouling prevention |
CN110520209A (en) * | 2017-03-14 | 2019-11-29 | 海水淡化科技有限公司 | Antifouling reverse osmosis and film cleaning systems are integrated for pre- |
ES2708126A1 (en) * | 2017-10-06 | 2019-04-08 | Moro Maria Teresa Bergaz | METHOD FOR THE TREATMENT OF WILD OR SEA WATER THROUGH REVERSE OSMOSIS (Machine-translation by Google Translate, not legally binding) |
WO2019068943A1 (en) * | 2017-10-06 | 2019-04-11 | Bergaz Moro Maria Teresa | Method for treating brackish water or seawater by reverse osmosis |
US20200261850A1 (en) * | 2017-11-06 | 2020-08-20 | Sandymount Technologies Corporation | Flow Control in Large-numbered, Series-coupled Vessels of Reverse Osmosis Systems |
US11826706B2 (en) * | 2017-11-06 | 2023-11-28 | Alfa Laval Copenhagen A/S | Flow control in large-numbered, series-coupled vessels of reverse osmosis systems |
CN110184788A (en) * | 2019-06-25 | 2019-08-30 | 德仕科技(深圳)有限公司 | Cleaning system for balanced ring for washing machine salt water injection device |
WO2021072345A1 (en) * | 2019-10-11 | 2021-04-15 | Massachusetts Institute Of Technology | Deformation-enhanced cleaning of fouled membranes |
US11117813B1 (en) | 2020-03-18 | 2021-09-14 | Crosstek Membrane Technology | Techniques for managing scale formation in water filtration systems and a reverse osmosis (RO) and nanofiltration (NF) system implementing same |
WO2021188132A1 (en) * | 2020-03-18 | 2021-09-23 | Crosstek Membrane Technology | Techniques for managing scale formation in water filtration systems and a reverse osmosis (ro) and nanofiltration (nf) system implementing same |
US11697602B2 (en) | 2020-03-18 | 2023-07-11 | Ctx, Llc | Techniques for managing scale formation in water filtration systems and a reverse osmosis (RO) and nanofiltration (NF) system implementing same |
WO2024086897A1 (en) * | 2022-10-27 | 2024-05-02 | C2 Water (SPV) Pty Ltd | A method for reducing accumulation of foulants on reverse osmosis membranes and a groundwater desalination system |
Also Published As
Publication number | Publication date |
---|---|
WO2004062774A2 (en) | 2004-07-29 |
WO2004062774A3 (en) | 2004-09-30 |
US7563375B2 (en) | 2009-07-21 |
US20070246425A1 (en) | 2007-10-25 |
AU2003283788A1 (en) | 2004-08-10 |
AU2003283788B2 (en) | 2008-12-18 |
ES2288388A1 (en) | 2008-01-01 |
IL157581A (en) | 2004-08-31 |
ES2288388B1 (en) | 2008-12-01 |
IL157581A0 (en) | 2004-03-28 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US7563375B2 (en) | Direct osmosis cleaning | |
US9932250B2 (en) | Membrane filtration system | |
US7658852B2 (en) | RO membrane cleaning method | |
RU2363663C2 (en) | Device for continuous water demineralisation in closed circuit at alternate pressure in one tank | |
JP6762258B2 (en) | Reverse osmosis treatment system and reverse osmosis treatment method | |
KR102266110B1 (en) | Pressure-reduced saline water treatment system | |
US8795527B2 (en) | Filtration system | |
US7892429B2 (en) | Batch-operated reverse osmosis system with manual energization | |
US7662290B2 (en) | Integrated water decontamination plant and well pump arrangement | |
US20110290728A1 (en) | SWRO Pressure Vessel and Process That Increases Production and Product Quality and Avoids Scaling Problems | |
US10293306B2 (en) | Method and system for performing a batch reverse osmosis process using a tank with a movable partition | |
CN106428504A (en) | Small reverse osmosis seawater desalting device | |
Stover et al. | Low-energy consumption with closed-circuit desalination | |
US8377302B2 (en) | Continuous process batch-operated reverse osmosis system with in-tank membranes and circulation | |
RU2323036C2 (en) | Method and device for concentrating water solutions of biology-active agents | |
KR101806144B1 (en) | Desalination system using controlled forward osmosis and reverse osmosis | |
RU2701342C1 (en) | Method for desalination of water using reverse osmosis and device for its implementation | |
CN114920328A (en) | Seawater desalination system | |
WO2019116073A1 (en) | Membrane cleaning method and apparatus | |
GB2557610A (en) | Membrane cleaning method and apparatus | |
JP2002126457A (en) | Filtration equipment |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: I.D.E. TECHNOLOGIES LTD., ISRAEL Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:LIBERMAN, BORIS;REEL/FRAME:014736/0615 Effective date: 20030908 |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |