WO2013172605A1 - Procédé de dessalement d'eau salée à faible énergie et système de dessalement d'eau salée à l'aide d'osmose retardée par pression et d'osmose inverse - Google Patents

Procédé de dessalement d'eau salée à faible énergie et système de dessalement d'eau salée à l'aide d'osmose retardée par pression et d'osmose inverse Download PDF

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WO2013172605A1
WO2013172605A1 PCT/KR2013/004175 KR2013004175W WO2013172605A1 WO 2013172605 A1 WO2013172605 A1 WO 2013172605A1 KR 2013004175 W KR2013004175 W KR 2013004175W WO 2013172605 A1 WO2013172605 A1 WO 2013172605A1
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brine
pressure
pressurized
pro
desalination
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PCT/KR2013/004175
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English (en)
Korean (ko)
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주영길
홍승관
김봉철
김정원
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고려대학교 산학협력단
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Publication of WO2013172605A1 publication Critical patent/WO2013172605A1/fr

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    • 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
    • B01D63/02—Hollow fibre modules
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/06—Energy recovery
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/002—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
    • B01D61/002—Forward osmosis or direct osmosis
    • B01D61/0024—Controlling or regulating
    • 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
    • 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
    • B01D61/04—Feed pretreatment
    • 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
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • 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
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/14—Pressure control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2313/00—Details relating to membrane modules or apparatus
    • B01D2313/24—Specific pressurizing or depressurizing means
    • B01D2313/246—Energy recovery means
    • 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
    • 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 present invention relates to a low energy salt water desalination method and a salt water desalination system using pressure delay osmosis and reverse osmosis, and more specifically, a pressure delay osmosis system that maximizes energy efficiency by effectively combining a pressure delay osmosis process and a reverse osmosis process.
  • the present invention relates to a low energy desalination method and a desalination system using reverse osmosis.
  • Seawater desalination or saltwater desalination refers to obtaining fresh water by removing salts from seawater containing salts.
  • Methods of treating such desalination include evaporation method using water evaporation phenomenon, membrane filtration method using membrane differentiation and selective passage ability, and the membrane filtration method includes reverse osmosis (RO) and electrodialysis in detail. It is divided into electrodialysis.
  • RO reverse osmosis
  • the salt water desalination method using reverse osmosis is a method of extracting fresh water by applying reverse osmosis pressure higher than osmotic pressure to seawater with a semi-permeable membrane interposed therebetween. It is used.
  • the brine in order to separate the salt from the water, the brine starts to be applied to the brine by applying a pressure above the osmotic pressure caused by the dissolved components.
  • the concentration of salts in seawater in brine is generally 30,000-45,000 ppm, and the osmotic pressure induced at these concentrations is 20-30 atm. In other words, in order to obtain a small amount of fresh water from the seawater it is necessary to apply a pressure of 20 atm or more.
  • a high pressure pump is used as a driving force necessary to overcome the high osmotic pressure of seawater and produce fresh water.
  • the energy required to drive the motor of the high pressure pump is about 3 to 5 kWh / m 3 to produce 1 m 3 of fresh water.
  • FIG. 1 is a diagram showing the configuration of the system disclosed in the US Patent Publication US2012 / 0037566.
  • the present invention provides a low energy desalination method and desalination system using pressure delayed osmosis and reverse osmosis, which can maximize energy efficiency more than conventional desalination systems using reverse osmosis, including US Patent Publication No. 2012/0037566. Its purpose is.
  • the purpose of the present invention is to increase the membrane filtration recovery rate compared to the existing brine desalination system, to reduce the amount of brine required to produce the same amount of fresh water, and to lower the cost of pretreatment of brine such as seawater.
  • the first brine and the first fresh water is input to the pressure delayed osmosis process to increase the flow rate of the first brine PRO preprocessing step is output;
  • the second brine is applied to the reverse osmosis process is achieved by a low energy salt water desalination method using pressure delayed osmosis and reverse osmosis, characterized in that it comprises a RO desalination step of producing a second fresh water.
  • the PRO pretreatment step includes: (a1) the first brine is pressurized by a first pressure exchange process and outputted to the first pressurized brine; (a2) generating the PRO output brine in which the first pressurized brine and the first fresh water are input to the pressure delay osmosis process to increase the flow rate of the first pressurized brine; (a3) a portion of the PRO output brine is input to the first pressure exchange process to depressurize through pressure exchange with the first brine to produce a first reduced pressure brine; (a4) may include outputting the remaining of the PRO output brine and the first reduced pressure brine to the second brine.
  • the RO desalination step includes: (b1) the first reduced pressure brine is pressurized by a second pressure exchange process and outputted to the second pressurized brine; (b2) pressurizing the rest of the PRO output brine to a preset reference pressure; (b3) the pressurized PRO output brine and the second pressurized brine are joined to the reverse osmosis process to produce the second fresh water; (b4) a third brine generated through the reverse osmosis process may be input to the second pressure exchange process and pressure exchanged with the first reduced pressure brine.
  • the PRO pretreatment step further comprises (a5) compensating for the pressure of the first pressurized brine such that the pressure of the first pressurized brine matches the reference pressure;
  • the RO desalination step may further include (b5) compensating for the pressure of the second pressurized brine such that the pressure of the second pressurized brine matches the reference pressure.
  • the first brine and the first fresh water is input to the first brine by a pressure delayed osmosis process PRO pretreatment unit for increasing the flow rate of the output to the second brine; It can also be achieved by a low-energy brine desalination system using a concentration difference between the brine and fresh water, characterized in that it comprises a RO desalination unit to enter the second brine to generate a second fresh water by reverse osmosis desalination process.
  • the PRO pre-treatment unit is a first pressure exchange unit for pressurizing the first brine through a pressure exchange process to output the first pressurized brine, the first pressurized brine and the first fresh water is input to the pressure delay osmosis process
  • a PRO process unit for increasing the flow rate of the first pressurized brine to produce a PRO output brine, and a PRO branch for branching the PRO output brine to the first pressure exchange unit and the RO desalination unit, respectively;
  • the first pressure exchanger receives a portion of the PRO output brine branched through the PRO branch and exchanges the pressure with the first brine to reduce the pressure of the first pressurized brine and the PRO output brine to which the first brine is pressurized. Producing first reduced pressure saline;
  • the PRO preprocessor may output the remaining of the PRO output brine and the first reduced pressure brine branched through the PRO branch to the second brine.
  • the RO desalination unit may further include a second pressure exchange unit configured to pressurize the first reduced pressure brine through pressure exchange to output a second pressurized brine, and a RO pumping unit configured to pressurize the rest of the PRO output brine at a predetermined reference pressure.
  • An RO process unit applied to the process to generate the second fresh water and the third brine;
  • the second pressure exchange unit may receive the third brine and exchange pressure with the first reduced pressure brine to generate the second pressurized brine to which the first reduced pressure brine is pressurized.
  • the PRO pretreatment unit further includes a PRO pressure compensator configured to compensate the pressure of the first pressurized brine such that the pressure of the first pressurized brine matches the reference pressure;
  • the RO desalination unit may further include an RO pressure compensator configured to compensate the pressure of the second pressurized brine such that the pressure of the second pressurized brine matches the reference pressure.
  • FIG. 2 is a view showing the configuration of a low-energy brine desalination system according to the present invention
  • FIG. 3 is a view for explaining a low energy desalination method according to the present invention.
  • FIG. 4 is a view showing the contents shown in Fig. 3 of the US Patent Publication US2012 / 0037566.
  • PRO pretreatment unit 11 the first pressure exchange unit
  • the present invention is a low-energy brine desalination method using pressure delayed osmosis and reverse osmosis, in a low-energy brine desalination method using pressure delayed osmosis and reverse osmosis, wherein the first brine and the first fresh water are input to the pressure delayed osmosis process.
  • the second brine is subjected to a reverse osmosis process to include a RO desalination step to produce a second fresh water.
  • the low energy desalination system according to the present invention includes a PRO pretreatment unit 10 and a RO desalination unit 30.
  • the PRO preprocessor 10 receives the first brine SW1 and the first fresh water IW1 I.
  • the PRO pretreatment unit 10 increases the flow rate of the first brine (SW1) and the first fresh water (IW1 I ) by increasing the flow rate of the first brine (SW1) by a pressure retarded osmosis (PRO) process.
  • the RO desalination unit 30 receives the second brine, and desalination of the second brine by a reverse osmosis (RO) desalination process to generate a second fresh water (IW2).
  • RO reverse osmosis
  • the PRO pretreatment unit 10 may include a first pressure exchange unit 11, a PRO process unit 12, and a PRO branch unit 15.
  • the first pressure exchange unit 11 pressurizes the first brine SW1 through a pressure exchange process and is output as the first pressurized brine.
  • the first brine SW1 is input to the low pressure input terminal of the first pressure exchange unit 11, and the first pressurized brine is output to the high pressure output terminal through a pressure exchange process.
  • the PRO output brine pressure-exchanged with the first brine (SW1) is supplied through the PRO branch portion 15 is input to the high-pressure input terminal of the first pressure exchange unit 11, a detailed description thereof will be described later.
  • the PRO process unit 12 generates a pressure delayed osmosis between the first pressurized brine and the first freshwater IW1 I to transmit a portion of the first freshwater IW1 I to the first pressurized saline side and the remaining first freshwater ( IW1 O exits from the PRO process section 12. Accordingly, the PRO output brine in which the flow rate of the first pressurized brine is increased and thus the osmotic pressure is reduced is generated by the PRO process unit 12.
  • the first fresh water IW1 I is withdrawn by the fresh water intake pump 17 and flows into the PRO process unit 12.
  • the PRO branching section 15 branches the PRO output brine produced by the PRO process section 12 to the first pressure exchange section 11 and the RO desalination section 30, respectively. That is, a part of the PRO output brine output from the PRO process unit 12, for example, 50% is delivered to the first pressure exchange unit 11, and the remaining 50% is delivered to the RO desalination unit 30.
  • the PRO output brine branched from the PRO branch unit 15 and delivered to the first pressure exchange unit 11 is input to the high pressure input terminal of the first pressure exchange unit 11 and input to the low pressure input terminal. ) And a pressure exchange process.
  • the first brine SW1 inputted to the low pressure input stage is pressurized by being exchanged with the PRO output brine inputted to the high pressure input stage, and is outputted by switching to the first pressurized brine through the high pressure output stage.
  • the PRO output brine input to the high pressure input stage is pressure-reduced by being exchanged with the first brine SW1 input to the low pressure input stage, and is converted to the first reduced pressure brine through the low pressure output stage.
  • the second brine output by the PRO pre-processing unit 10 is branched through the PRO branch 15 and the PRO output brine delivered to the RO desalination unit 30, the first pressure exchange unit And a first reduced pressure brine output through the low pressure output stage of (11).
  • RO desalination unit 30 As shown in Figure 2, the second pressure exchange unit 31, RO pumping unit 33, RO confluence unit 35 and RO process unit 32 ) May be included.
  • the second pressure exchange unit 31 pressurizes the first reduced pressure brine delivered from the first pressure exchange unit 11 of the PRO pretreatment unit 10 through pressure exchange to output the second pressurized brine. Will be described later.
  • the RO pumping unit 33 presses the PRO output brine remaining from the PRO pretreatment unit 10 to a predetermined reference pressure and outputs the result to the RO confluence unit 35.
  • the RO confluence unit 35 merges the PRO output brine pressurized by the RO pumping unit 33 and the second pressurized brine output from the second pressure exchange unit 31 and transmits the resultant to the RO process unit 32.
  • the RO process part 32 applies the PRO output brine (the state pressurized by the RO pumping part 33) and the second pressurized brine joined through the RO confluence part 35 to the reverse osmosis process to perform the second fresh water. (IW2) and a second brine.
  • the second freshwater (IW2) generated through the RO process unit 32 is a part of the brine is generated through the reverse osmosis membrane from the brine mixed with the PRO output brine and the second pressurized brine through the reverse osmosis process, It is fresh water produced by the low energy desalination system according to the invention.
  • the third brine generated by the RO process unit 32 is input to the high pressure input terminal of the second pressure exchange unit 31 to exchange pressure with the first reduced pressure brine.
  • the first reduced pressure saline delivered from the first pressure exchange unit 11 of the PRO pretreatment unit 10 is input to the low pressure input terminal of the second pressure exchange unit 31, and the RO process unit 32 is provided.
  • the third brine from is input to the high pressure input of the second pressure exchange section 31.
  • the first reduced pressure brine and the third brine are pressure-exchanged in the second pressure exchange unit 31, and the first reduced pressure brine is pressurized and output through the high pressure output terminal of the second pressure exchange unit 31 as the second pressurized brine.
  • the third brine is reduced in pressure and output through the low pressure output terminal of the second pressure exchange unit 31.
  • the PRO pretreatment unit 10 may include a PRO pressure compensator 14 for compensating the pressure of the first pressurized brine such that the pressure of the first pressurized brine matches the reference pressure.
  • a PRO pressure compensator 14 for compensating the pressure of the first pressurized brine such that the pressure of the first pressurized brine matches the reference pressure.
  • the RO desalination unit 30 may include a RO pressure compensator 34 for compensating the pressure of the second pressurized brine such that the pressure of the second pressurized brine matches the reference pressure.
  • a RO pressure compensator 34 for compensating the pressure of the second pressurized brine such that the pressure of the second pressurized brine matches the reference pressure.
  • FIG. 2 Reference numerals 1 to ⁇ shown in FIG. 2 are for explaining the saline or fresh water before and after the passage of each component of the low energy saline desalination system according to the present invention, where 1 is the first brine (SW1), 2 is the first 1 pressurized brine, 3 is the first pressurized brine passing through the PRO pressure compensator 14, 4 is the PRO output brine, 5 is branched by the PRO branch 15 of the PRO output brine, the first pressure exchange section 11 PRO output saline directed to), 6 is PRO output saline branched by PRO branching portion 15 of the PRO output brine and directed to RO pumping section 33 of RO desalination section 30, 7 RO pumping section 33 PRO output brine pressurized by 8, the first pressure-saving saline output through the low pressure output terminal of the first pressure exchange unit 11, 9 is the second pressurized output through
  • 1 is the first brine (SW1)
  • 2 is the first 1 pressurized brine
  • 3 is the first pressurized brine passing
  • the first brine SW1 is withdrawn by the brine intake pump 16 (S11). Then, the first brine (SW1) withdrawn is input to the low pressure input stage of the first pressure exchanger, is pressurized through a first pressure exchange process with the PRO output brine is output through the high pressure output stage to the first pressurized brine (S11). .
  • the first pressurized brine output from the high pressure output terminal of the first pressure exchanger may be compensated to match the reference pressure through the PRO pressure compensator 14.
  • the first pressurized brine whose pressure is compensated for through the PRO pressure compensator 14 is input to the PRO process unit 12 and is output as the PRO output brine whose flow rate is increased through the pressure delay osmosis process (S12).
  • PRO output brine is branched and moved to the RO pumping part 33 side of the first pressure exchange part 11 and the RO desalination part 30 by the PRO branching part 15.
  • PRO output brine to the pressure is exchanged with the first brine (SW1) through a first pressure exchange process is output to the first reduced pressure brine is directed to the second pressure exchange unit (31).
  • the PRO output brine directed to the RO pumping part 33 is pressurized to the reference pressure by the RO pumping part 33 (S13) to be directed to the RO process part 32.
  • the second pressure exchange process is performed (S14), the first pressure-saving saline output through the first pressure exchange process in step S11 of the second pressure exchange unit 31 It is input through the low pressure input stage, the third brine generated in the RO desalination process (S15) is input through the high pressure input stage and is mutually pressure exchanged.
  • the second pressurized brine outputted through the high pressure output terminal of the second pressure exchange unit 31 is joined to the RO output unit 32 by joining the PRO output brine pressurized in step S13 and the RO confluence unit 35.
  • the second freshwater IW2 is generated through the RO desalination process, ie, reverse osmosis desalination, and the remaining brine is directed to the second pressure exchange unit 31 as the third saline solution.
  • Figure 4 shows the contents shown in Fig. 3 of the above-described United States Patent Publication No. US2012 / 0037566.
  • the fresh water (H 2 O) generated by the system disclosed in the U.S. Patent Publication has a pressure (P) and an osmotic pressure ( ⁇ ) of '0', and a flow rate (Q) of '1'. .
  • the pressure (P), osmotic pressure ( ⁇ ), and salt water at the main location of the low energy saline desalination system according to the present invention based on the flow rate of fresh water (H 2 O) generated through the system disclosed in the U.S. Patent Publication
  • the flow rate Q is summarized in [Table 1].
  • the low-energy brine desalination system proposes the configuration of the PRO pressure compensator 14 and the RO pressure compensator 34, which is also necessary for the compensation of the pressure lost in the U.S. Patent Publication. It will be readily appreciated by those skilled in the art that the low energy saline desalination system according to the present invention is more efficient than the system disclosed in the U.S. Patent Publication, provided in the form of a pump and taking into account the magnitude of the pressure lost.
  • the present invention is effectively combined with a pressure delayed osmosis process and a reverse osmosis process, and is applied to a low energy saline desalination system using pressure delayed osmosis and reverse osmosis which maximizes energy efficiency.

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

Abstract

La présente invention concerne un procédé de dessalement d'eau salée à faible énergie et un système de dessalement d'eau salée à l'aide d'osmose retardée par pression et d'osmose inverse. Selon la présente invention, le procédé de dessalement d'eau salée à faible énergie à l'aide d'osmose retardée par pression et d'osmose inverse, comprend : une étape de traitement par PRO d'introduction d'une première eau salée et d'une première eau douce dans un procédé d'osmose retardée par pression et de sortie d'une seconde eau salée avec un flux augmenté par le flux de ladite première eau salée ; et une étape de dessalement par RO d'application de ladite seconde eau salée à un procédé d'osmose inverse pour produire une seconde eau douce. Par conséquent, il est possible de rendre maximal un rendement énergétique par combinaison de façon efficace d'un procédé d'osmose retardée par pression et d'un procédé d'osmose inverse.
PCT/KR2013/004175 2012-05-15 2013-05-14 Procédé de dessalement d'eau salée à faible énergie et système de dessalement d'eau salée à l'aide d'osmose retardée par pression et d'osmose inverse WO2013172605A1 (fr)

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KR1020120051262A KR101356878B1 (ko) 2012-05-15 2012-05-15 압력 지연 삼투와 역삼투를 이용한 저에너지 염수담수화 방법 및 염수담수화 시스템
KR10-2012-0051262 2012-05-15

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WO2017019944A1 (fr) 2015-07-29 2017-02-02 Gradiant Corporation Procédés de dessalement osmotique et systèmes associés
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
US11629072B2 (en) 2018-08-22 2023-04-18 Gradiant Corporation Liquid solution concentration system comprising isolated subsystem and related methods
US11667549B2 (en) 2020-11-17 2023-06-06 Gradiant Corporation Osmotic methods and systems involving energy recovery
EP4289501A1 (fr) * 2022-06-08 2023-12-13 Danfoss A/S Système d'osmose inverse et d'osmose retardée par pression
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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US9895663B2 (en) 2015-09-09 2018-02-20 Kuwait Institute For Scientific Research Integrated reverse osmosis/pressure retarded osmosis system

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US11611099B1 (en) 2022-05-09 2023-03-21 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
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US11699803B1 (en) 2022-05-09 2023-07-11 Rahul S Nana Reverse electrodialysis cell with heat pump
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