WO2012102677A1 - Procédé et appareil permettant d'obtenir de l'eau à partir d'une source d'alimentation en eau - Google Patents

Procédé et appareil permettant d'obtenir de l'eau à partir d'une source d'alimentation en eau Download PDF

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Publication number
WO2012102677A1
WO2012102677A1 PCT/SG2012/000020 SG2012000020W WO2012102677A1 WO 2012102677 A1 WO2012102677 A1 WO 2012102677A1 SG 2012000020 W SG2012000020 W SG 2012000020W WO 2012102677 A1 WO2012102677 A1 WO 2012102677A1
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WO
WIPO (PCT)
Prior art keywords
draw solution
forward osmosis
diluted
water
source water
Prior art date
Application number
PCT/SG2012/000020
Other languages
English (en)
Inventor
Darren Delai Sun
Tze Siong Jonathan LEE
Zhaoyang Liu
Original Assignee
Nano-Mem Pte. Ltd.
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Nano-Mem Pte. Ltd. filed Critical Nano-Mem Pte. Ltd.
Publication of WO2012102677A1 publication Critical patent/WO2012102677A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
    • 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
    • B01D61/58—Multistep processes
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/08—Specific process operations in the concentrate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/26—Further operations combined with membrane separation processes
    • B01D2311/2688—Biological processes
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • 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
    • B01D61/027—Nanofiltration
    • 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
    • B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
    • B01D61/364—Membrane distillation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/08—Seawater, e.g. for desalination
    • 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

  • the invention relates to a method and apparatus for recovering or extracting water from an aqueous, and particularly, though not exclusively, relates to recovering fresh water from a source water containing impurities.
  • Fresh water scarcity is now one of the most pressing challenges to civilization worldwide. Expanding population sizes and industrialization are increasing the demand for precious fresh water and energy. Seawater desalination and wastewater reclamation are some of the options explored for increasing fresh water availability.
  • Forward osmosis membrane processes makes use of a natural osmosis phenomenon for transport of water from a feed solution with low solute concentration to a draw solution with high solute concentration across a semi-permeable membrane, using osmotic pressure difference between the feed solution and the draw solution as a driving force to move water across the semi-permeable membrane.
  • draw solute in the draw solution can be separated for reuse while high quality fresh water can be produced.
  • forward osmosis does not require intensive energy input for fresh water production. Meanwhile, forward osmosis offers the advantages of less membrane fouling tendency and high rejection of solutes.
  • a known forward osmosis process involves successful selection of NH4HCO3 as the draw solution. After using this to extract fresh water from seawater through the forward osmosis membrane, a thermal process (58 °C) was applied to boil away the NH3 and C0 2 , leaving fresh water. The NH 3 and CO2 are then recombined to form salt and the process is repeated. Although it was claimed that this approach requires only one-tenth the energy used compared with conventional desalination systems, considerable energy is still required to vaporize the gas constituents (CO2 and NH 3 ) of the draw solute. To lower the energy consumption, this forward osmosis process is only feasible when limited in use to areas near power/incineration plants in order to tap on exhausted heat from such energy sources.
  • the application discloses a hybrid apparatus and process suitable for one or more of seawater desalination, wastewater reclamation and anaerobic biogas production for potential concurrent productions of fresh water and biogas energy, with the advantages of low energy consumption, less membrane fouling and requiring very limited feed water pre-treatment. Systems modeled around this process would have dramatic improvements in energy and cost effectiveness when benchmarked against existing systems.
  • the invention is designed to leverage the phenomenon of forward osmosis.
  • the invention can be used to produce drinking water from seawater or brackish water (desalination), from wastewater (reclamation) or any combination of the above.
  • Wastewater sources are wide-ranging and include anything from municipal sewage to food and pharmaceutical processing wastewaters.
  • the invention can also be used to produce biogas for power generation, wherein wastewater used should contain organic material if power generation is a desired output of using the method and apparatus.
  • an apparatus for recovering water from a source water comprising a forward osmosis unit configured to be supplied with the source water and a draw solution, the forward osmosis unit configured to osmotically transfer water from the source water into the draw solution, wherein output from the forward osmosis unit may comprise diluted draw solution and concentrated source water; and a draw solution concentration unit may comprise at least one nanofiltration unit configured to be supplied with a diluted solution obtained downstream of the forward osmosis unit and to concentrate the diluted solution, thereby producing water.
  • the apparatus may further comprise a further forward osmosis unit configured to be supplied with a further source water and with the diluted draw solution output from the forward osmosis unit, the further forward osmosis unit configured to osmotically transfer water from the further source water into the diluted draw solution, wherein output from the further forward osmosis unit may comprise additionally diluted draw solution and concentrated further source water, wherein the diluted solution concentrated by the draw solution concentration unit may comprise the additionally diluted draw solution, and wherein output of the draw solution from the draw solution concentration unit may be supplied to the forward osmosis unit.
  • the further source water may be provided from a same supply as the source water.
  • the source water may comprise seawater.
  • the apparatus may further comprise at least one bioreactor configured to perform biological reactions on the concentrated further source water.
  • the at least one bioreactor may include at least one of: anaerobic bioreactor configured to produce biogas and an anaerobic bioreactor configured to biodegrade pollutants in the concentrated further source water.
  • the draw solution may comprise a draw solute selected from at least one of: water-soluble inorganic chemicals and water-soluble organic chemicals.
  • the water-soluble inorganic chemicals may include at least one of A1 2 (S0 4 )3, MgS0 4 , Na 2 S0 , K 2 S0 4 , (NH 4 ) 2 S0 4 , Fe 2 (S0 4 ) 3 , AlClj, MgCl 2 , NaCl, CaCl 2 , NH 4 C1, C1, FeCl 3 , A1(N0 3 ) 3 , Mg( 0 3 ) 2 , Ca(N0 3 ) 2 , NaN0 3 , N0 3 , NH 4 HC0 3 , KHC0 3 , NaHC0 3 , KBr and their relative hydrates; and wherein the water-soluble organic chemicals include at least one of methanol, ethanol, acetone, glucose, sucrose, fructose, dextrose, chitosan, dendrimer and 2- ethylimidazole-based chemicals.
  • the draw solution concentration unit may further comprise at least one of: a reverse osmosis membrane unit and a membrane distillation unit.
  • the draw solution concentration unit may further comprise at least two reverse osmosis membrane units connected in tandem and sharing a same feed of diluted draw solution.
  • the draw solution concentration unit may further comprise two nanofiltration units, wherein permeate from a first of the two nanofiltration units may be fed to a second of the two nanofiltration units. Retentate from the second of the two nanofiltration units may be fed to the first of the two nanofiltration units.
  • the draw solution may comprise seawater
  • the apparatus may further comprise a further forward osmosis unit configured to be supplied with a further draw solution and with the diluted seawater output from the forward osmosis unit, the further forward osmosis unit configured to osmotically transfer water from the diluted seawater into the further draw solution, wherein output from the further forward osmosis unit may comprise diluted further draw solution and seawater, wherein the diluted solution supplied to the draw solution concentration unit for production of water may comprise the diluted further draw solution, and wherein output of the further draw solution from the draw solution concentration unit may be supplied to the further forward osmosis unit.
  • a method of recovering water from a source water comprising supplying the source water and a draw solution to a forward osmosis unit; osmotically transferring water from the source water into the draw solution in the forward osmosis unit; outputting diluted draw solution and concentrated source water from the forward osmosis unit; supplying a diluted solution obtained downstream of the forward osmosis unit to a draw solution concentration unit; and concentrating the diluted solution in the draw solution concentration unit, thereby producing water.
  • Supplying the draw solution to the forward osmosis unit may comprise supplying the draw solution from the draw solution concentration unit.
  • Concentrating the diluted solution may comprise subjecting the diluted draw solution to at least one pass of nanofiltration.
  • Concentrating the diluted solution may comprise subjecting the diluted draw solution to two passes of nanofiltration, wherein permeate from the first pass of nanofiltration may be used as a feed source in the second pass of nanofiltration. wherein retentate from the first pass of nanofiltration may be supplied as the draw solution to the forward osmosis unit; and wherein retentate from the second pass of nanofiltration may be supplied as feed to the first pass of nanofiltration.
  • the method may further comprise, prior to step d), supplying the diluted draw solution and a further source water to a further forward osmosis unit; osmotically transferring water from the further source water into the diluted draw solution in the further forward osmosis unit; outputting additionally diluted draw solution and concentrated further source water from the further forward osmosis unit; and wherein the diluted solution supplied to the draw solution concentration unit in step d) may comprise the additionally diluted draw solution output from the further forward osmosis unit.
  • the method may further comprise performing biological reactions on the concentrated further source water in a bioreactor.
  • Performing biological reactions may comprise at least one of: producing biogas and biodegrading pollutants in the concentrated further source water.
  • the draw solution may comprise seawater
  • the method may further comprise, prior to step d), supplying a further draw solution and the diluted seawater output form the forward osmosis unit to a further forward osmosis unit; osmotically transferring water from the diluted seawater into the further draw solution in the further forward osmosis unit; outputting seawater and diluted further draw solution from the further forward osmosis unit, and wherein the diluted solution supplied to the draw solution concentration unit in step d) may comprise the diluted further draw solution.
  • Supplying the further draw solution to the further forward osmosis unit may comprise supplying the further draw solution from the draw solution concentration unit.
  • an apparatus for producing a biogas from a source water comprising a forward osmosis unit configured to osmotically transfer water from the source water into a draw solution, output from the forward osmosis unit may comprise diluted draw solution and concentrated source water; and a bioreactor configured to produce the biogas from the concentrated source water.
  • the draw solution may comprise seawater and the source water may comprise wastewater.
  • a method of producing a biogas from a source water comprising supplying the source water and a draw solution to a forward osmosis unit; osmotically transferring water from the source water into the draw solution in the forward osmosis unit; outputting diluted draw solution and concentrated source water from the forward osmosis unit; and producing the biogas by bioreacting the concentrated source water in a bioreactor.
  • FIG. 1 is a schematic diagram of a first exemplary apparatus for recovering water from a source water
  • FIG. 2. is a schematic diagram of a second exemplary apparatus for recovering water from a source water
  • FIG. 3 is a schematic diagram of a third exemplary apparatus for recovering water from a source water.
  • FIG. 4 is a schematic diagram of an exemplary apparatus for producing biogas from a source water.
  • the apparatus 10 comprises a forward osmosis unit 1 10 configured to receive a source water from a source water supply 1 12 and a draw solution from a draw solution supply 1 13.
  • the forward osmosis unit 110 is configured to osmotically extract or transfer water from the source water into the draw solution.
  • Output from the forward osmosis unit 1 10 thus comprises diluted draw solution and concentrated source water.
  • the apparatus 10 also comprises a draw solution concentration unit 1 30.
  • the draw solution concentration unit 130 comprising at least one nanofiltration unit configured to concentrate a diluted solution obtained downstream of the forward osmosis unit 1 10, thereby producing water 190 and also producing the draw solution that is supplied to the forward osmosis unit 1 10.
  • the draw solution concentration unit 130 comprises a nanofiltration membrane system capable of producing clean drinking water 190 while concentrating the diluted solution.
  • the draw solution may comprises 2 M MgS0 4 while the source water comprises seawater.
  • concentration of the 2 M MgS0 4 draw solution will be diluted due to osmosis of water from the seawater into the draw solution.
  • the diluted draw solution may have a concentration of about 0.8 M.
  • the apparatus 10 also comprises a further forward osmosis unit 120 into which the intermediate or diluted draw solution is channelled, together with a further source water from a further source water supply 122.
  • the further forward osmosis unit 120 is configured to osmotically transfer water from the further source water into the diluted draw solution.
  • the further source water comprises municipal wastewater.
  • concentration of the intermediate or diluted draw solution will be additionally diluted.
  • the additionally diluted draw solution may have a concentration of about 0.2 M.
  • Output of the further forward osmosis unit 120 thus comprises additionally diluted draw solution and concentrated further source water, that is, concentrated waste water.
  • the additionally diluted draw solution is then supplied to the draw solution concentration unit 130 which concentrates it back to 2 M or thereabouts, thereby forming the draw solution that is supplied to the forward osmosis unit 1 10 and at the same time producing water 190.
  • the apparatus 10 preferably also comprises a bioreactor 140 configured for performing biological reactions on the concentrated wastewater.
  • the bioreactor 140 may include an anaerobic reactor configured to produce biogas 142 such as methane for energy production.
  • the bioreactor 140 may include an aerobic bioreactor for biodegrading pollutants in the concentrated wastewater.
  • the aerobic bioreactor may comprise a membrane bioreactor (MBR). Effluent from the bioreactor 140 is preferably channelled back to the further source water supply 122.
  • MLR membrane bioreactor
  • the second exemplar ⁇ ' apparatus 20 similarly comprises a forward osmosis unit 210 configured to receive a source water from a source water supply 220 and a draw solution from a draw solution supply 213.
  • the forward osmosis unit 210 is configured to osmotically transfer water from the source water into the draw solution. Output from the forward osmosis unit 210 thus comprises diluted draw solution and concentrated source water.
  • the apparatus 20 further comprises a draw solution concentration unit 2300, which also serves as the draw solution supply 213.
  • the draw solution concentration unit 230 comprises a 2-pass nanofiitration membrane system, that is, two nanofiitration units 231 , 232 configured to concentrate a diluted solution obtained downstream of the forward osmosis unit 210, thereby producing water and also the draw solution that is supplied to the forward osmosis unit 210.
  • the diluted solution comprises the diluted draw solution output directly from the forward osmosis unit 210.
  • the source water comprises seawater while the draw solution comprises 2 M MgS0 4 .
  • concentration of the 2 M MgS0 draw solution will be diluted.
  • the diluted draw solution may have a concentration of about 1 M.
  • the diluted draw solution is supplied to the draw solution concentration unit 230 having the two nanofiitration units 231 , 232 and concentrated back to 2 M or thereabouts while clean drinking water is produced.
  • the first nanofiitration unit 231 serves to provide a first-pass nanofiitration of the diluted draw solution while the second nanofiitration unit 232 serves to provide a second- pass nano-filtration.
  • the diluted draw solution is first fed through the first-pass nanofiltration membrane or the first nanofiltration unit 231 .
  • 98-99.5% of MgSC>4 draw solute is retained by the first nanofiltration unit 231 , while 0.5-2% of MgS0 4 draw solute permeates through the first nanofiltration unit 232.
  • Retentate from the first pass of nanofiltration by the first nanofiltration unit 231 is supplied to the forward osmosis unit 210 as the draw solution.
  • Permeate solution from the first nanofiltration unit 231 is used as a feed solution of the second-pass nanofiltration membrane or the second nanofiltration unit 232.
  • Retentate from the second nanofiltration unit 232 is fed back to the first nanofiltration unit 231 , while the permeate from the second nanofiltration unit 232 is the desired water produced 290.
  • TDS total dissolved solids
  • the apparatus 30 of the third exemplary embodiment comprises a forward osmosis unit 310 configured to receive a source water from a source water supply 312 and a dra solution from a draw solution supply 313.
  • the forward osmosis unit 310 is configured to osmotically transfer water from the source water into the draw solution. Output from the forward osmosis unit 310 thus comprises diluted draw solution and concentrated source water.
  • the draw solution comprises seawater while the source water comprises wastewater.
  • the apparatus 30 also comprises a further forward osmosis unit 320 which is supplied with the diluted seawater output from the forward osmosis unit 310, and also supplied with a further draw solution from a draw solution supply 31 3.
  • Output of the further forward osmosis unit 320 thus comprises diluted further draw solution and seawater.
  • the further draw solution is provided from a draw solution concentration unit 330 serving as the draw solution supply 313.
  • the draw solution concentration unit 330 comprises at least one nanofiltration unit configured to concentrate a diluted solution obtained downstream of the forward osmosis unit 310, thereby producing clean drinking water 390.
  • the diluted solution obtained downstream of the forward osmosis unit 3 10 comprises the diluted further draw solution output from the further forward osmosis unit 320 and supplied to the draw solution concentration unit 330.
  • the apparatus 30 preferably also comprises a bioreactor 340 configured for performing biological reactions on the concentrated wastewater.
  • the bioreactor 340 includes an anaerobic reactor configured to produce a biogas such as methane for energy production.
  • the biogas may be channelled to an electricity generator 342 for generating electricity 350.
  • the bioreactor 340 may further include an aerobic bioreactor for biodegrading pollutants in the concentrated wastewater. Effluent from the bioreactor 340 is preferably channelled back to forward osmosis unit 310 as part of the source water.
  • the draw solution used in the apparatus 10, 20 or the further draw solution used in the apparatus 30 may alternatively or in addition comprise a draw solute selected from at least one of: water- soluble inorganic chemicals and water-soluble organic chemicals.
  • water-soluble inorganic chemicals include at least one of A1 2 (S0 4 ) 3 , MgS0 4 , " Na 2 S0 4 , K 2 S0 4 , (NH ) 2 S0 4 , Fe 2 (S0 4 ) 3 , A1C1 3 , MgCl 2 , NaCl, CaCl 2 , NH4CI, KC1, FeCl 3 , A1(N0 3 ) 3 , Mg(N0 3 ) 2 , Ca(N0 3 ) 2 , NaN0 3 , KNO 3 , NH 4 HC0 3 , KHC0 3 , NaHC0 3 , KBr and their relative hydrates.
  • the draw solution concentration unit 130, 230, 330 may further comprise at least one of: a reverse osmosis membrane unit and a membrane distillation unit.
  • the draw solution concentration unit 130, 230, 330 may comprise at least two reverse osmosis membrane units connected in tandem and sharing a same feed of diluted draw solution.
  • the at least one membrane distillation unit may comprise multi-stage membrane distillation units.
  • nanofiltration is an energy efficient means of divalent salt removal.
  • Reverse osmosis membranes require hydraulic pressures in excess of the opposing osmotic pressure for water flux to be effected.
  • the characteristically "loose" nature of nanofiltration pores is responsible for a filtration type effect that allows water flux to occur when hydraulic pressures well below osmotic pressures are applied.
  • the present invention is able to both leverage the osmotic pressure gradient through forward osmosis and overcome the same gradient using nanofiltration.
  • an apparatus 40 for producing a biogas.
  • the apparatus 40 similarly comprises a forward osmosis unit 410 configured to receive a source water from a source water supply 412 and a draw solution from a draw solution supply 413.
  • the forward osmosis unit 410 is configured to osmotically transfer water from the source water into the draw solution. Output from the forward osmosis unit 410 thus comprises diluted draw solution and concentrated source water.
  • the source water comprises municipal wastewater while the draw solution comprises seawater.
  • Output of the forward osmosis unit 50 thus comprises diluted seawater and concentrated wastewater. Since vast amounts of seawater are available compared to the size of the apparatus 40, the seawater source 413 approximates an endless sink for a system using the apparatus 40.
  • the apparatus 40 comprises a bioreactor 440 configured for performing biological reactions on the concentrated wastewater.
  • the bioreactor 440 includes an anaerobic reactor configured to produce a biogas such as methane for energy production.
  • the biogas may be channelled to an electricity generator 442 for generating electricity 450.
  • the bioreactor 440 may further include an aerobic bioreactor for biodegrading pollutants in the concentrated wastewater. Effluent from the bioreactor 440 is preferably channelled back to forward osmosis unit 410 as part of the source water.
  • the apparatus 40 is particularly useful for energy production and wastewater remediation.
  • the process itself uses close to zero energy and including the energy production, it is net positive- power generating.
  • the source water can also be brackish water, brine water from seawater desalination, wastewater, surface water, ground water, fruit juice, pharmaceutical solutions, or any combination of the above.
  • the further source water may be provided from a same supply as the source water; for example, both the source water and the further source water may comprise seawater, or. both the source water and the further source water may comprise wastewater.
  • any specific parameters given numerically above can vary and will depend on many variables such as membrane performance, cross flow velocity, osmotic pressure gradient total active membrane surface, temperature and other factors.
  • a batch system is described.
  • a continuous system is also envisaged, in which case the concentrations mentioned above can vary, as well as the other parameters, in order to deliver operator dictated performance.

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  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Nanotechnology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

La présente invention concerne un appareil permettant d'obtenir de l'eau à partir d'une source d'alimentation en eau, ledit appareil comprenant une unité d'osmose directe conçue pour être alimentée par la source d'alimentation en eau et en une solution d'extraction, ladite unité d'osmose directe étant conçue pour permettre un transfert osmotique d'eau depuis la source d'approvisionnement en eau et en direction de la solution d'extraction. L'unité d'osmose directe donne de la solution d'extraction diluée et de l'eau de source concentrée. L'appareil comprend également une unité de concentration de solution d'extraction comprenant au moins une unité de nano-filtration conçue pour être alimentée en solution diluée obtenue en aval de l'unité d'osmose directe et pour concentrer ladite solution diluée, en vue de la production d'eau.
PCT/SG2012/000020 2011-01-24 2012-01-25 Procédé et appareil permettant d'obtenir de l'eau à partir d'une source d'alimentation en eau WO2012102677A1 (fr)

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SG201100521 2011-01-24
SG201100521-2 2011-01-24

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CN103537191A (zh) * 2013-10-24 2014-01-29 哈尔滨工业大学 一种采用膜蒸馏浓缩葡萄糖的方法
CN103663821A (zh) * 2012-09-04 2014-03-26 宁波莲华环保科技股份有限公司 一种海水淡化方法和系统
WO2014144778A1 (fr) * 2013-03-15 2014-09-18 Porifera, Inc. Avancées dans des systèmes de membrane à entraînement osmotique comprenant une purification multi-étages
US9039899B2 (en) 2011-04-25 2015-05-26 Oasys Water, Inc. Osmotic separation systems and methods
WO2015157031A1 (fr) * 2014-04-08 2015-10-15 Oasys Water, Inc. Systèmes et procédés de séparation osmotique
US20160297693A1 (en) * 2013-11-21 2016-10-13 The University Of Manchester Osmosis
CN106186514A (zh) * 2016-07-14 2016-12-07 清华大学 将厕所污水资源化处理的生态厕所系统
US9636635B2 (en) 2012-12-21 2017-05-02 Porifera, Inc. Separation systems, elements, and methods for separation utilizing stacked membranes and spacers
ES2619113A1 (es) * 2015-12-22 2017-06-23 Acciona Agua, S.A. Procedimiento de control de sistema combinado de ósmosis directa y nanofiltración u ósmosis inversa
WO2017152226A1 (fr) * 2016-03-09 2017-09-14 Enrgistream Pty Ltd Procédé et système de traitement des eaux usées et de génération d'électricité
CN108328831A (zh) * 2018-02-02 2018-07-27 北京林业大学 一种反渗透浓盐水的浓缩方法及设备
WO2019008219A1 (fr) * 2017-07-07 2019-01-10 Suomen Malmijalostus Oy Concentration d'eau d'évacuation
US10427957B2 (en) 2013-02-08 2019-10-01 Oasys Water LLC Osmotic separation systems and methods
US11502322B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell with heat pump
US11502323B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
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US11571660B2 (en) 2015-06-24 2023-02-07 Porifera, Inc. Methods of dewatering of alcoholic solutions via forward osmosis and related systems
US11855324B1 (en) 2022-11-15 2023-12-26 Rahul S. Nana Reverse electrodialysis or pressure-retarded osmosis cell with heat pump

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US10280097B2 (en) 2011-04-25 2019-05-07 Oasys Water LLC Osmotic separation systems and methods
CN103663821B (zh) * 2012-09-04 2017-12-22 宁波莲华环保科技股份有限公司 一种海水淡化方法和系统
CN103663821A (zh) * 2012-09-04 2014-03-26 宁波莲华环保科技股份有限公司 一种海水淡化方法和系统
US9636635B2 (en) 2012-12-21 2017-05-02 Porifera, Inc. Separation systems, elements, and methods for separation utilizing stacked membranes and spacers
US10464023B2 (en) 2012-12-21 2019-11-05 Porifera, Inc. Separation systems, elements, and methods for separation utilizing stacked membranes and spacers
US11759751B2 (en) 2012-12-21 2023-09-19 Porifera, Inc. Separation systems, elements, and methods for separation utilizing stacked membranes and spacers
US11090611B2 (en) 2012-12-21 2021-08-17 Porifera, Inc. Separation systems, elements, and methods for separation utilizing stacked membranes and spacers
US10427957B2 (en) 2013-02-08 2019-10-01 Oasys Water LLC Osmotic separation systems and methods
US10500544B2 (en) 2013-03-15 2019-12-10 Porifera, Inc. Advancements in osmotically driven membrane systems including multi-stage purification
WO2014144778A1 (fr) * 2013-03-15 2014-09-18 Porifera, Inc. Avancées dans des systèmes de membrane à entraînement osmotique comprenant une purification multi-étages
US9861937B2 (en) 2013-03-15 2018-01-09 Porifera, Inc. Advancements in osmotically driven membrane systems including low pressure control
CN105142762A (zh) * 2013-03-15 2015-12-09 波里费拉公司 包含多级净化的渗透驱动膜系统的改进
CN103385514A (zh) * 2013-07-03 2013-11-13 佛山中润水处理科技有限公司 用作正渗透驱动液的营养液制备方法
CN103537191A (zh) * 2013-10-24 2014-01-29 哈尔滨工业大学 一种采用膜蒸馏浓缩葡萄糖的方法
US20160297693A1 (en) * 2013-11-21 2016-10-13 The University Of Manchester Osmosis
WO2015157031A1 (fr) * 2014-04-08 2015-10-15 Oasys Water, Inc. Systèmes et procédés de séparation osmotique
US10406482B2 (en) 2014-04-08 2019-09-10 Oasys Water LLC Osmotic separation systems and methods
US11571660B2 (en) 2015-06-24 2023-02-07 Porifera, Inc. Methods of dewatering of alcoholic solutions via forward osmosis and related systems
ES2619113A1 (es) * 2015-12-22 2017-06-23 Acciona Agua, S.A. Procedimiento de control de sistema combinado de ósmosis directa y nanofiltración u ósmosis inversa
US10981116B2 (en) 2016-03-09 2021-04-20 EnrgiStream Pty Etd Process and system for treating waste water and generating power
WO2017152226A1 (fr) * 2016-03-09 2017-09-14 Enrgistream Pty Ltd Procédé et système de traitement des eaux usées et de génération d'électricité
CN106186514A (zh) * 2016-07-14 2016-12-07 清华大学 将厕所污水资源化处理的生态厕所系统
US11541352B2 (en) 2016-12-23 2023-01-03 Porifera, Inc. Removing components of alcoholic solutions via forward osmosis and related systems
WO2019008219A1 (fr) * 2017-07-07 2019-01-10 Suomen Malmijalostus Oy Concentration d'eau d'évacuation
CN108328831B (zh) * 2018-02-02 2020-10-09 北京林业大学 一种反渗透浓盐水的浓缩方法及设备
CN108328831A (zh) * 2018-02-02 2018-07-27 北京林业大学 一种反渗透浓盐水的浓缩方法及设备
US11502322B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell with heat pump
US11502323B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
US11563229B1 (en) 2022-05-09 2023-01-24 Rahul S Nana Reverse electrodialysis cell with heat pump
US11611099B1 (en) 2022-05-09 2023-03-21 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
US11699803B1 (en) 2022-05-09 2023-07-11 Rahul S Nana Reverse electrodialysis cell with heat pump
US11855324B1 (en) 2022-11-15 2023-12-26 Rahul S. Nana Reverse electrodialysis or pressure-retarded osmosis cell with heat pump

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