WO2005120688A1 - Cooling apparatus - Google Patents
Cooling apparatus Download PDFInfo
- Publication number
- WO2005120688A1 WO2005120688A1 PCT/GB2005/002307 GB2005002307W WO2005120688A1 WO 2005120688 A1 WO2005120688 A1 WO 2005120688A1 GB 2005002307 W GB2005002307 W GB 2005002307W WO 2005120688 A1 WO2005120688 A1 WO 2005120688A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- solution
- membrane
- solvent
- water
- evaporative cooling
- Prior art date
Links
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
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0023—Accessories; Auxiliary operations
-
- 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
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F25/00—Component parts of trickle coolers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
- F28C2001/006—Systems comprising cooling towers, e.g. for recooling a cooling medium
-
- 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
- Y02B—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO BUILDINGS, e.g. HOUSING, HOUSE APPLIANCES OR RELATED END-USER APPLICATIONS
- Y02B30/00—Energy efficient heating, ventilation or air conditioning [HVAC]
- Y02B30/70—Efficient control or regulation technologies, e.g. for control of refrigerant flow, motor or heating
Definitions
- the present invention relates to a method and apparatus for introducing a solution into a cooling apparatus.
- the present invention relates to a method and apparatus for removing heat from a heat source .
- Heat exchangers are often used to remove excess heat from industrial processes.
- Typical heat exchangers include shell and tube-type heat exchangers, which comprise a length of tubing partially enclosed within a housing or shell.
- An industrial process stream containing excess heat is introduced into the tubing, whilst a coolant, such as water, is passed through the shell via a separate inlet and outlet.
- the water removes excess heat from the process stream.
- the water exiting the shell is at a higher temperature than the coolant entering the shell.
- the heated water stream is cooled in a cooling tower before it is recirculated back through the shell . In this way, heat removal can be carried out in a continuous manner.
- blowdown To replace the total water loss from the system, makeup water is introduced.
- the make-up water is treated with, for example, scale inhibitors, corrosion inhibitors, biocides and dispersants. These additives tend to be expensive and have to be added continuously to the make-up water, adding to the cost of the overall process.
- the water quality of the cooling system has a significant effect on the thermal efficiency and life of the cooling tower and heat exchangers.
- the selective nature of the membrane prevents undesirable solute (s) and other containments in the first solution from passing into the second solution.
- the first solution may be an impure aqueous stream, such as seawater, brackish water, river water and waste streams from, for example, an industrial or agricultural process.
- water is selectively allowed to pass across the membrane to dilute the second solution.
- the second solution may comprise seawater, brackish water and industrial process streams.
- Suitable industrial process streams may be derived from, for example, the salty residues of desalination plants, such as thermal desalination and/or reverse osmosis plants, and aqueous effluents, such as those typically employed as -make-up water for conventional cooling towers.
- the seawater, brackish water and industrial process streams employed may be concentrated prior to use.
- the seawater, brackish water and/or industrial process streams employed may be concentrated during the course of the process of the present invention, such that the solution in contact with the membrane in step a) has a higher solute (total dissolved salts) concentration than the first solution.
- the evaporative cooling apparatus may be employed to remove solvent from the second solution by evaporation to produce a concentrated second solution that can be used to draw solvent from the first solution in step a) .
- solutes dissolved in the second solution may be "immobilised".
- the second solution may have a known composition.
- the second solution is formed by introducing a known quantity of a solute into a known quantity of solvent.
- the second solution may consist essentially of a selected solute dissolved in a selected solvent. This second solution may be formed prior to step a) .
- the second solution may have a reduced concentration of suspended particles, biological matter and/or other components that may cause fouling of the cooling system. More preferably, the second solution is substantially free of such components.
- additives such as scale inhibitors, corrosion inhibitors, biocides and/or dispersants are included in the second solution.
- the second solution may be recirculated in a closed-loop, for example, such that it is continuously reused in steps a) and b) . In such an embodiment, the components of the second solution are effectively "immobilised" within the loop.
- solute and/or additives such as scale inhibitors, corrosion inhibitors, biocides and/or dispersants may not be necessary.
- the solvent in the second solution is preferably water.
- the solute (osmotic agent) in the second solution is preferably a water-soluble solute, such as a water-soluble salt.
- Suitable salts include salts of ammonium and metals, such as alkali metals (e.g. Li, Na, K) and alkali earth metals (e.g. Mg and Ca) .
- the salts may be fluorides, chlorides, bromides, iodides, sulphates, sulphites, sulphides, carbonates, hydrogencarbonates, nitrates, nitrites, nitrides, phosphates, aluminates, borates, bromates, carbides, chlorides, perchlorates, hypochlorates, chromates, fluorosilicates, fluorosilicates, fluorosulphates, silicates, cyanides and cyanates .
- One or more salts may be employed.
- the solute of the second solution is a sodium and/or potassium salt.
- step a) of the present invention the first solution is placed on one side of a semi-permeable membrane.
- a second solution having a higher solute concentration (and, therefore, a lower solvent concentration) is placed on the opposite side of the membrane.
- solvent passes across the membrane from the side of low solute concentration (high solvent concentration) to the side of high solute concentration (low solvent concentration) .
- the flow occurs along a concentration gradient.
- high pressures are not required to induce solvent flow.
- a pressure differential across the membrane may be applied, for example, to increase the flux of water.
- the second solution may be at an elevated pressure (osmotic pressure when water is used as a solvent) , even when a pressure is not applied to induce solvent flow from the first solution to the second solution. This is because the flow of solvent from the first solution into the second solution occurs along a concentration gradient.
- This pressure may be used to aid the transfer of the second solution to subsequent processing steps of the present invention. This pressure may be sufficient to transfer the second solution to subsequent processing steps, for example, without the aid of pumps. In one embodiment, excess pressure is converted into mechanical work.
- the pressure (e.g. osmotic pressure) generated in the second solution may be used to reduce the power consumption and/or increase the heat transfer efficiency of the overall process .
- the solute (osmotic agent) in the third and/or subsequent solution is preferably a water-soluble solute, such as a water-soluble salt.
- Suitable salts include salts of ammonium and metals, such as alkali metals (e.g. Li, Na, K) and alkali earth metals (e.g. Mg and Ca) .
- the salts may be fluorides, chlorides, bromides, iodides, sulphates, sulphites, sulphides, carbonates, hydrogencarbonates, nitrates, nitrites, nitrides, phosphates, aluminates, borates, bromates, carbides, chlorides, perchlorates, hypochlorates, chromates, fluorosilicates, fluorosilicates, fluorosulphates, silicates, cyanides and cyanates.
- One or more salts may be employed.
- the solute of the third and/or subsequent solution is a sodium and/or potassium salt.
- the third and/or subsequent solution may be formed by dissolving a known amount of a sodium and/or potassium salt in water.
- the third and/or subsequent solution is formed by dissolving a sodium chloride in water.
- the third/ and or subsequent solution may be a solution of ammonia and carbon dioxide, with resultant aqueous species: ammonium carbonate, ammonium bicarbonate and ammonium carbamates (see WO 02/060825) .
- the third and/or subsequent solution may be contain the same solute (s) and solvent (s) as the second solution. It may also be possible to use different solutions as the second, third and/or subsequent solutions.
- additives such as scale inhibitors, corrosion inhibitors, biocides and/or dispersants are included in the third and/or subsequent solution.
- the third and/or subsequent solution may be recirculated in a closed-loop, for example, such that it is continuously reused in steps a) and b) .
- the components of the third ⁇ and/or subsequent solution are effectively "immobilised" within the loop.
- solute and/or additives such as scale inhibitors, corrosion inhibitors, biocides and/or dispersants may not be necessary.
- Air-coolers typically comprise a housing containing a porous filler material (e.g. decking or packing).
- the second solution is introduced into the air-cooler and wets the filler material.
- some of the solvent (e.g. water) of the second solution evaporates.
- the loss of heat by evaporation (evaporative cooling) lowers the temperature of the air.
- the air emerging from the air cooler may be used as a coolant for, for example, a heat exchanger. Alternatively, the emerging air may be used to cool an enclosed space, such as a room.
- Cooling towers typically contain a porous filler material, known as decking (packing).
- decking packing
- the second solution is introduced into the top of the cooling tower and drips down through the decking, whilst a coolant, such as air, is blown through the decking, causing some of the solvent of the second solution to evaporate.
- evaporative cooling lowers the temperature of the remaining second solution.
- Any suitable cooling tower may be employed in the process of the present invention.
- suitable cooling towers include natural draft and mechanical draft cooling towers.
- the second solution may be used to remove excess heat from a heat source (step d) .
- the present invention provides a method for removing heat from a heat source.
- Step d) may be carried out before and/or after the second solution is introduced into the evaporative cooling apparatus in step b) provided that the second solution used in step (d) is at a lower temperature than the heat source.
- step d) is carried out before and/or after the second solution is cooled in a cooling tower in step b) .
- the second solution is used as a coolant in a heat exchanger to remove heat from an industrial process stream, such as steam from a power plant .
- the heat exchanger may be a shell-and-tube-type heat exchanger, which comprises a length of tubing partially enclosed within a housing or shell.
- the industrial process stream is introduced into the tubing, whilst the second solution is passed through the shell via a separate inlet and outlet.
- the second solution removes excess heat from the process stream.
- the second solution exiting the shell is at a higher temperature than the second solution entering the shell.
- the second solution may be reused in step a) .
- the overall concentration of solute in the second solution in contact with the selectively permeable membrane should be higher than the concentration of solute in the first solution, so that solvent from the first solution will pass across the selectively permeable membrane into the second solution.
- the removal of solvent from the second solution is controlled to ensure that the second solution in contact with the selectively permeable membrane has a desired concentration.
- the second solution may be cooled prior to reuse in step a) (e.g. in a cooling tower) .
- step c) the solution used in steps a) , b) and, optionally, d) may be recirculated in a closed loop.
- additional components such as solvents, solutes and additives selected from, for example, scale inhibitors, corrosion inhibitors, biocides and/or dispersants may be added to the closed loop.
- Any suitable selectively membrane may be used in the process of the present invention.
- An array of membranes may be employed. Suitable membranes include cellulose acetate (CA) and cellulose triacetate (CTA) (such as those described in McCutcheon et al . , Desalination 174 (2005) 1-11) and polyamide (PA) membranes.
- the membrane may be planar or take the form of a tube or hollow fibre. Thin membranes may be employed, particularly, when a high pressure is not applied to induce solvent flow from the first solution to the second solution. If desired, the membrane may be supported on a supporting structure, such as a mesh support.
- the flow of solvent across a selectively membrane is generally influenced by thermal conditions.
- the solutions on either side of the membrane may be heated or cooled, if desired.
- the solutions may be heated to higher temperatures of 40 to 90°C, for example, 60 to 80°C.
- the solutions may be cooled to -20 to 40°C, for example, 5 to 20°C.
- the solution on one side of the membrane may be heated, while the other side cooled.
- the heating or cooling may be carried out on each solution independently. Chemical reactions may also be carried out on either side of the membrane, if desired.
- the first and/or second solution may be treated to reduce fouling and scaling of the membrane. Accordingly, anti-scaling and/or anti-fouling agents may be added to one or both solutions.
- pressure may be applied to the first solution side of the membrane to increase the rate of flux of water across the membrane. For example, pressures of 1 x 10 5 Pa to 5 x 10 5 Pa [1 to 5 bar] may be applied, preferably pressures of 2 x 10 5 Pa to 4 x 10 5 Pa [2 to 4 bar] .
- the pressure on the second solution side of the membrane may be reduced. For example the pressure may be less than 1 x 10 5 Pa [1 bar] , preferably less than 0.5 x 10 5 Pa [0.5 bar].
- an apparatus for introducing a solution into an evaporative cooling apparatus comprising a housing comprising a selectively permeable membrane for separating a first solution from a second solution having a higher solute concentration than the first solution, said membrane being configured to selectively allow solvent to pass from the first solution-side of the membrane to the second solution-side of the membrane, an evaporative cooling apparatus, and means for removing second solution from the housing, and means for introducing the second solution into the evaporative cooling apparatus.
- the apparatus of the present invention may further comprise a heat exchanger.
- Figure 1 is a schematic diagram of an apparatus according to a first embodiment of the present invention.
- Figure 2 is a schematic diagram of an apparatus according to a second embodiment of the present invention.
- Figure 3 is a schematic diagram of an apparatus according to a third embodiment of the present invention.
- Figure 4 is a schematic diagram of an apparatus according to a fourth embodiment of the present invention.
- an apparatus 10 for producing a cool stream of air comprises a housing 12 and an air cooler 14.
- the housing 12 comprises a selectively- permeable membrane 16 for separating seawater 18 from a solution 20 formed by dissolving a known amount of sodium chloride in water.
- seawater 18 is circulated through the housing 12 on one side of the membrane 16, whilst sodium chloride solution 20 is circulated through the housing 12 on the opposite side of the membrane 16.
- the sodium chloride solution 20 in contact with the membrane 16 has a higher total dissolved salt (solute) concentration than the seawater 18.
- This concentrated solution 20 is removed from the air cooler 14 via line 26 and- recirculated to the solution-side of the membrane 16 in housing 12 in a closed loop.
- the concentration of the solution 20 in contact with the membrane 16 is higher than that of the seawater 18 on the other side of the membrane 16.
- the apparatus of- Figure 2 is similar to the apparatus of Figure 1. Thus, like numerals have been used to designate like parts. Unlike the apparatus of Figure 1, however, the apparatus of Figure 2 comprises two housings 12a and 12b are used in series.
- the first housing 12a comprises a selectively permeable membrane 16a for separating seawater 18 from a solution 20a formed by dissolving a known amount of sodium chloride in water.
- the second housing 12b comprises a selectively permeable membrane 16b for separating solution 20a from the first housing 12a from a solution 20b formed by dissolving a known amount of sodium chloride in water.
- seawater 18 is circulated through the housing 12a on one side of the membrane 16a, whilst sodium chloride solution 20a is circulated through the housing 12a on the opposite side of the membrane 16a.
- the sodium chloride solution 20a in contact with the membrane 16 has a higher total dissolved salt (solute) concentration than the seawater 18.
- water flows from the seawater-side of the membrane 16 to the solution-side of the membrane 16 by osmosis .
- the flow of water across the membrane 16a dilutes the sodium chloride solution 20a.
- the diluted solution 20a is circulated through the housing 12b on one side of the membrane 16b, whilst sodium chloride solution 20b is circulated through the housing 12b on the opposite side of the membrane 16b.
- the sodium chloride solution 20b in contact with the membrane 16b has a higher total dissolved salt (solute) concentration than the solution 20a.
- the diluted solution 20b is introduced into an air cooler 14 in the manner described with reference to Figure 1.
- the sodium chloride solution 20a becomes increasingly concentrated and this is recirculated to housing 12a.
- the apparatus 100 comprises a housing 110, a heat exchanger 112 and a cooling tower 114.
- the housing 110 comprises a selectively permeable membrane 116 for separating seawater 118 from a solution 120 formed by dissolving a known amount of sodium chloride in water.
- seawater 118 is circulated through the housing 110 on one side of the membrane 116, whilst sodium chloride solution 120 is circulated through the housing 110 on the opposite side of the membrane 116.
- the sodium chloride solution 120 in contact with the membrane 116 has a higher total dissolved salt (solute) concentration than the seawater 118.
- water flows from the seawater-side of the membrane 116 to the solution-side of the membrane 116 by osmosis .
- the flow of water across the membrane 116 dilutes the sodium chloride solution 120.
- This diluted solution 120 is introduced into the cooling tower 114.
- the cooling tower 114 contains a porous filler material, known as decking (not shown) .
- the solution 120 is introduced into the top of the cooling tower 114 and -drips down through the decking, whilst cool air 126 is blown through the decking, causing some of the water from the solution 120 to evaporate.
- the loss of heat by evaporation evaporative cooling
- the remaining solution is more concentrated than the solution entering the cooling tower 114 because of the loss of water by evaporation.
- the cooled solution 120 is introduced into the heat exchanger 112.
- the solution 120 used as a coolant to remove heat from an industrial process stream 124. Heat from the stream 124 is transferred to the solution 120 through the walls of the heat exchanger 112. Thus, the temperature of solution 120 is increased.
- the solution 120 is withdrawn from the heat exchanger 124 via line 128 and reintroduced to the solution-side of the membrane 116 in a closed loop.
- the concentration of the solution 120 in contact with the membrane 116 is higher than that of the seawater 118 on the other side of the membrane 116.
- the apparatus of Figure 4 is similar to the. apparatus of Figure 3. Thus, like numerals have been used to designate like parts. Unlike the apparatus of Figure 3, solution 120 from the housing 110 is introduced into the heat exchanger 112 before it is introduced into the cooling tower 114.
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- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Devices That Are Associated With Refrigeration Equipment (AREA)
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP05750234A EP1781401B1 (en) | 2004-06-11 | 2005-06-10 | Process for introducing a solution into an evaporative cooling apparatus |
AT05750234T ATE534454T1 (en) | 2004-06-11 | 2005-06-10 | METHOD FOR INTRODUCING A SOLUTION INTO AN EVAPORATIVE COOLING SYSTEM |
US11/628,980 US7823396B2 (en) | 2004-06-11 | 2005-06-10 | Cooling apparatus |
ES05750234T ES2374558T3 (en) | 2004-06-11 | 2005-06-10 | PROCESS TO INTRODUCE A SOLUTION IN AN EVAPORATIVE COOLING DEVICE. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
GBGB0413110.8A GB0413110D0 (en) | 2004-06-11 | 2004-06-11 | Cooling apparatus |
GB0413110.8 | 2004-06-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2005120688A1 true WO2005120688A1 (en) | 2005-12-22 |
Family
ID=32732364
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/GB2005/002307 WO2005120688A1 (en) | 2004-06-11 | 2005-06-10 | Cooling apparatus |
Country Status (8)
Country | Link |
---|---|
US (1) | US7823396B2 (en) |
EP (1) | EP1781401B1 (en) |
CN (1) | CN100490950C (en) |
AT (1) | ATE534454T1 (en) |
CY (1) | CY1112272T1 (en) |
ES (1) | ES2374558T3 (en) |
GB (1) | GB0413110D0 (en) |
WO (1) | WO2005120688A1 (en) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2009037515A2 (en) | 2007-09-20 | 2009-03-26 | Abdulsalam Al-Mayahi | Process and systems |
US7608188B2 (en) | 2004-12-03 | 2009-10-27 | Board Of Regents Of The Nevada System Of Higher Education | Vacuum enhanced direct contact membrane distillation |
WO2010067061A1 (en) | 2008-12-08 | 2010-06-17 | Surrey Aquatechnology Ltd. | Process for operating a cooling tower comprising the treatment of feed water by direct osmosis |
US20110198208A1 (en) * | 2008-11-07 | 2011-08-18 | Deutsches Zentrum Fur Luft-Und Raumfahrt E.V. | Method for desalinating water containing salt |
US8029671B2 (en) | 2006-06-13 | 2011-10-04 | Board Of Regents Of The Nevada System Of Higher Education, On Behalf Of The University Of Nevada, Reno | Combined membrane-distillation-forward-osmosis systems and methods of use |
US8083942B2 (en) | 2004-12-06 | 2011-12-27 | Board of Regents of the Nevada System of Higher Education, on Behalf of the Universary of Nevada, Reno | Systems and methods for purification of liquids |
Families Citing this family (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2009102442A1 (en) * | 2008-02-11 | 2009-08-20 | Siemens Water Technologies Corp. | Desalination of water containing high silica content |
US10260761B2 (en) | 2010-05-18 | 2019-04-16 | Energy & Environmental Research Center Foundation | Heat dissipation systems with hygroscopic working fluid |
US10845067B2 (en) * | 2010-05-18 | 2020-11-24 | Energy & Enviornmental Research Center | Hygroscopic cooling tower for waste water disposal |
US10808948B2 (en) | 2010-05-18 | 2020-10-20 | Energy & Environmental Research Center | Heat dissipation systems with hygroscopic working fluid |
EP2686615A2 (en) * | 2011-03-16 | 2014-01-22 | Carrier Corporation | Air conditioning system with distilled water production from air |
CN105026019A (en) * | 2012-11-16 | 2015-11-04 | Oasys水有限公司 | Draw solutions and draw solute recovery for osmotically driven membrane processes |
BR112015019057A2 (en) | 2013-02-08 | 2017-07-18 | Oasys Water Inc | osmotic separation systems and methods |
EP3494090B1 (en) * | 2016-08-04 | 2021-08-18 | Dominion Engineering, Inc. | Suppression of radionuclide deposition on nuclear power plant components |
WO2019132855A1 (en) * | 2017-12-25 | 2019-07-04 | David John Tanner | Ionic air cooling device |
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2004
- 2004-06-11 GB GBGB0413110.8A patent/GB0413110D0/en not_active Ceased
-
2005
- 2005-06-10 WO PCT/GB2005/002307 patent/WO2005120688A1/en active Application Filing
- 2005-06-10 US US11/628,980 patent/US7823396B2/en active Active
- 2005-06-10 EP EP05750234A patent/EP1781401B1/en not_active Not-in-force
- 2005-06-10 ES ES05750234T patent/ES2374558T3/en active Active
- 2005-06-10 CN CNB2005800206268A patent/CN100490950C/en not_active Expired - Fee Related
- 2005-06-10 AT AT05750234T patent/ATE534454T1/en active
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2012
- 2012-02-01 CY CY20121100111T patent/CY1112272T1/en unknown
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PATENT ABSTRACTS OF JAPAN vol. 2003, no. 02 5 February 2003 (2003-02-05) * |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7608188B2 (en) | 2004-12-03 | 2009-10-27 | Board Of Regents Of The Nevada System Of Higher Education | Vacuum enhanced direct contact membrane distillation |
US8083942B2 (en) | 2004-12-06 | 2011-12-27 | Board of Regents of the Nevada System of Higher Education, on Behalf of the Universary of Nevada, Reno | Systems and methods for purification of liquids |
US8216474B2 (en) | 2004-12-06 | 2012-07-10 | The Board Of Regents Of The Nevada System Of Higher Education | Systems and methods for purification of liquids |
US8029671B2 (en) | 2006-06-13 | 2011-10-04 | Board Of Regents Of The Nevada System Of Higher Education, On Behalf Of The University Of Nevada, Reno | Combined membrane-distillation-forward-osmosis systems and methods of use |
WO2009037515A2 (en) | 2007-09-20 | 2009-03-26 | Abdulsalam Al-Mayahi | Process and systems |
WO2009037515A3 (en) * | 2007-09-20 | 2010-04-08 | Abdulsalam Al-Mayahi | Process and systems |
US20110198208A1 (en) * | 2008-11-07 | 2011-08-18 | Deutsches Zentrum Fur Luft-Und Raumfahrt E.V. | Method for desalinating water containing salt |
WO2010067061A1 (en) | 2008-12-08 | 2010-06-17 | Surrey Aquatechnology Ltd. | Process for operating a cooling tower comprising the treatment of feed water by direct osmosis |
US8795532B2 (en) | 2008-12-08 | 2014-08-05 | Surrey Aquatechnology Ltd. | Process for operating a cooling tower comprising the treatment of feed water by direct osmosis |
AU2009326253B2 (en) * | 2008-12-08 | 2015-09-03 | Surrey Aquatechnology Ltd. | Process for operating a cooling tower comprising the treatment of feed water by direct osmosis |
Also Published As
Publication number | Publication date |
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CN100490950C (en) | 2009-05-27 |
ATE534454T1 (en) | 2011-12-15 |
US20070186574A1 (en) | 2007-08-16 |
GB0413110D0 (en) | 2004-07-14 |
CY1112272T1 (en) | 2015-12-09 |
EP1781401A1 (en) | 2007-05-09 |
US7823396B2 (en) | 2010-11-02 |
EP1781401B1 (en) | 2011-11-23 |
ES2374558T3 (en) | 2012-02-17 |
CN1980727A (en) | 2007-06-13 |
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