WO2019164462A1 - Système d'osmose inverse multi-étage et processus de récupération d'eau élevée à partir de solutions aqueuses - Google Patents

Système d'osmose inverse multi-étage et processus de récupération d'eau élevée à partir de solutions aqueuses Download PDF

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WO2019164462A1
WO2019164462A1 PCT/TR2018/050063 TR2018050063W WO2019164462A1 WO 2019164462 A1 WO2019164462 A1 WO 2019164462A1 TR 2018050063 W TR2018050063 W TR 2018050063W WO 2019164462 A1 WO2019164462 A1 WO 2019164462A1
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subunit
stage
reverse osmosis
retentate
unit
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PCT/TR2018/050063
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English (en)
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Mehmet Goktug AHUNBAY
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Istanbul Teknik Universitesi
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Priority to PCT/TR2018/050063 priority Critical patent/WO2019164462A1/fr
Priority to SG11201900705PA priority patent/SG11201900705PA/en
Publication of WO2019164462A1 publication Critical patent/WO2019164462A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • 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
    • B01D61/029—Multistep processes comprising different kinds of membrane processes selected from reverse osmosis, hyperfiltration or 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
    • B01D61/025—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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/12—Controlling or regulating
    • 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
    • C02F1/442—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
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • 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
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/251—Recirculation of permeate
    • B01D2311/2512—Recirculation of permeate to feed side
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/02—Elements in series
    • B01D2317/022—Reject series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/02—Elements in series
    • B01D2317/025—Permeate series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/06—Use of membrane modules of the same kind
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/08—Use of membrane modules of different kinds
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • This invention relates to a system and a process of reverse osmosis for product recovery from an aqueous solution, in particular recovery of potable water from saltwater.
  • RO Reverse osmosis
  • the International Patent Application Numbered WO2015152823 in the state of the art discloses an apparatus for reverse osmosis, the apparatus comprising: a single- stage reverse osmosis (SSRO) unit; and a counter-current membrane cascade with recycle (CMCR) unit comprising a plurality of stages of reverse osmosis including at least a first stage and a second stage wherein permeate from the first stage is configured to be introduced as feed to the second stage; wherein retenate from the SSRO unit is configured to be introduced as feed to the first stage, and wherein product obtained using the apparatus comprises permeate from the SSRO unit and permeate from a last stage of the CMCR unit.
  • SSRO single- stage reverse osmosis
  • CMCR counter-current membrane cascade with recycle
  • U.S. Patent Application No. US2015014248 discloses methods and systems for generating strong brines are disclosed in which a feed stream and a draw inlet stream are passed through a forward osmosis membrane to create a concentrate and a draw outlet stream.
  • the draw outlet stream is passed through a reverse osmosis membrane to create a reverse osmosis permeate flow and a reverse osmosis retentate flow
  • the reverse osmosis retentate flow is passed through a first nanofiltration membrane to create a first nanofiltration permeate flow and a first nanofiltration retentate flow
  • the first nanofiltration retentate flow is passed through a second nano filtration membrane to create a second nanofiltration permeate flow and a second nanofiltration retentate flow.
  • the process is repeated through a third nanofiltration membrane.
  • the process may be repeated through a third nanofiltration membrane.
  • the U.S. Patent Application Numbered US 9427705 in the state of the art discloses a method of solvent recovery includes using a plurality of solvent recovery units to recover solvent from a dilute solution.
  • the solvent recovery units can include a plurality of reverse osmosis or forward osmosis membrane systems arranged in series. For reverse osmosis, at least some of the concentrate in a last reverse osmosis unit of the series is recycled back to the permeate of that unit to provide a mixed permeate. The mixed permeate is then passed successively to the permeate side of each preceding reverse osmosis unit in the series.
  • a draw solution is passed sequentially from the permeate side of each unit to the permeate side of the preceding unit.
  • the draw solution may be prepared by concentrating part of the concentrate stream by evaporation and recycling it back as a draw solution.
  • U.S. Patent Application No. US2013118978 discloses a water treatment system combines a microfiltration or ultrafiltration membrane system with a downstream reverse osmosis membrane system.
  • the MF or UF system has multiple trains of immersed membrane modules.
  • the trains are connected to a common permeate pump.
  • the permeate pump discharges directly into the inlet of an RO feed pump.
  • the membrane trains are each subjected to the same suction.
  • the permeate pumps are operated to provide the required flow to the RO feed pump at or above the minimum inlet pressure of the RO feed pump.
  • the specific energy consumption (SEC) for producing potable water from sea water is relatively high.
  • SEC specific energy consumption
  • the theoretical gross SEC required by a conventional single-stage RO (SSRO) is 3.086 kwh/m (kilowatt hours of energy per cubic meter of product water) using a membrane with a salt rejection of 0.993 at a pressure of 55.5 bar with a water recovery of 50%.
  • SSRO single-stage RO
  • an SSRO requires a pressure greater than 79.3 bar, which is above the operating limits of the typical commercial membranes.
  • the aim of this invention is to realize a system for reverse osmosis wherein overall water recovery of the system greater than 55% can be achieved while operating each stage with a stage recovery less than or equal to 50%, that is while mantaining the safety factor, which is defined as the ratio of the retentate flow rate to the permeate flow rate for the same membrane stage, less than or equal to one.
  • Another aim of this invention is realize a system for reverse osmosis wherein overall water recovery of the system greater than 55% can be achieved while reducing the required osmotic pressure differential below than what is required in a conventional SSRO for the same overall water recovery.
  • the process in the present invention combines a primary water recovery (PWR) unit (1 A) with a secondary water recovery (SWR) unit (5 A) comprising a downstream RO subunit (2A), a nanofiltration (NF) subunit (3 A) and an upstream RO subunit (4A).
  • the PWR unit (1A) and each of the subunits within the SWR unit (5A) may comprise a plurality of membrane stages in series configuration wherein each membrane stage receives the retentate of the subsequent stage as feed.
  • the PWR unit (1A) sends its retentate stream as feed to the SWR unit (5A) by introducing into the high-pressure side of the downstream RO unit (2H).
  • Fig. 1 is a general schematic illustration of the present invention
  • Fig. 2 is a schematic illustration of four-stage embodiment of the present invention
  • Fig. 3 is a schematic illustration of five -stage embodiment of the present invention
  • Fig. 4 is a graph of net specific energy consumption (SECnet) as a function of the OPD in the downstream RO stage“R2” (Dpk 2 ) for 65% and 75 percent overall water recoveries in 4-stage (dashed lines) and 5-stage (solid lines) embodiments of the present invention.
  • SECnet net specific energy consumption
  • the system described in the invention comprises a primary water recovery (PWR) unit (1A) with a secondary water recovery (SWR) unit (5 A) as shown in Figure 1; wherein the PWR unit (1A) comprises one single RO stage or a plurality of RO stages in series configuration wherein the retentate of the preceding RO stage is fed to the high-pressure side of the subsequent RO stage; wherein the SWR unit (5A) comprises one downstream RO subunit (2A), one NF subunit (3A) and one upstream RO subunit (4A), wherein downstream is defined as the direction of the retentate flow from the NF subunit (3 A) and upstream is defined as the opposite direction of the retentate flow from the NF subunit (3 A); wherein the rententate of the PWR unit (1A) is introduced to the SWR unit (5A) as feed to the high-pressure side of the downstream RO subunit (2H); wherein the rententate of the downstream RO subunit (2A) is introduced as feed to the high-pressure side of the NF subunit (3H); wherein
  • the process provided in the present invention comprises the steps of: introducing a feed of aqueous solution into a PWR unit (1A) comprising at least a single RO stage; introducing retentate from the PWR unit (1A) into high-pressure side of a downstream RO subunit (2H) within a SWR unit (5 A) comprising a downstream RO subunit (2A), an NF subunit (3A) and an upstream RO subunit (4A); introducing retentate from the downstream RO subunit (2A) into high-pressure side of the NF subunit (3H); introducing permeate from the NF subunit into high- pressure side of the upstream RO subunit (4H); introducing retentate from the upstream RO subunit (4A) as feed to the high-pressure side of the downstream RO subunit (2H); and collecting as product permeates from all RO stages.
  • One embodiment of this invention involves operating the NF subunit (3A) at the same pressure as the retentate stream leaving the downstream RO subunit (2A) and not employing any interstage pumping on the high-pressure (retentate) side of the NF subunit (3H). This is done by using NF membranes with decreasing salt rejection in the direction of retentate flow. i.e. by using a membrane in stage Nl that passes more salt than the highly salt rejecting membranes used in the downstream RO subunit (2A); and by using a membrane with lower salt rejection than the preceding stage in each of the subsequent NF stages.
  • the OPD in PWR unit (1A) is significantly lower than OPD in the downstream RO subunit (2A). Since the recycling permeate leaving the NF subunit is blended with the saltwater feed to be introduced into the downstream RO subunit (2A). Pumping requirement for the recycling permeate will be significantly reduced, resulting in a further lower SEC.
  • Fig. 2 shows a four-stage embodiment of the invention, wherein the PWR unit comprises one single RO stage (Rl); and the downstream RO subunit comprises one RO stage (R2), the NF subunit comprises one NF stage (Nl) and the upstream RO subunit comprises one RO stage (R3), within the SWR unit.
  • the feed of aqueous solution is fed to the high-pressure (retentate) side (R1H) of stage Rl .
  • the retentate stream leaving stage Rl is introduced into the high-pressure side (R2H) of RO stage R2.
  • the retentate stream leaving stage R2 is introduced into the high- pressure side (N1H) of NF stage Nl, wherein the rententate of the stage Nl is discharged as concentrate stream and the permeate of stage Nl is recycled to be introduced as feed to the high-pressure side (R3H) of the upstream RO stage R3, wherein the retentate stream leaving stage R3 is blended with the feed stream at mixing point MP1 to be introduced into the high-pressure side (R2H) of stage R2.
  • the permeate of RO stages Rl, R2 and R3 are combined at mixing point MP2 to be collected as product water.
  • Fig 3. shows a five-stage embodiment of the invention, wherein the PWR unit comprises one single RO stage (Rl); and the downstream RO subunit comprises one RO stage (R2), the NF subunit comprises two NF stages in series (Nl and N2) and the upstream RO subunit comprises one RO stage (R3), within the SWR unit.
  • the feed of aqueous solution is fed to its high-pressure (retentate) side (R1H) of stage Rl.
  • the retentate stream leaving the stage Rl is introduced into the high- pressure side (R2H) of RO stage R2.
  • the retentate stream leaving stage R2 is introduced into the high-pressure side (N 1H) of NF stage N 1 , wherein the rententate of the stage Nl is introduced as feed to the high-pressure side (N2H) of the second NF stage N2, wherein the rententate of the stage N2 is discharged as concentrate stream.
  • the permeate streams of the stages Nl and N2 are combined at mixing point MP3 to be introduced as feed to the high-pressure side (R3H) of the upstream RO stage R3, wherein the retentate stream leaving stage R3 is blended with the feed stream at mixing point MP1 to be introduced into the high-pressure side (R2H) of stage R2.
  • the permeate of RO stages Rl, R2 and R3 are combined at mixing point MP2 to be collected as product water.
  • the analysis of this five-stage embodiment of the invention involves solving overall material and solute balances for each of the five stages and at three mixing points.
  • the balances over stage Rl constitute 2 equations involving 6 unknowns (Q F , C F , Qo, Co, Qi, Ci)
  • the balances over stage R2 constitute 2 equations involving 6 unknowns (Q 2 , C 2 , Q 3 , C 3 , Q 4 , C 4 )
  • the balances over stage Nl constitute 2 equations involving 4 unknowns (Q 5 , C 5 , Q 6 , C 6 ).
  • the balances over stage N2 constitute 2 equations involving 4 unknowns (Q 7 , C 7 , Q D , C D )
  • the balances over stage R3 constitute 2 equations involving 6 unknowns (Q 8 , C 8 , Q 9 , C 9 , Q 10 , C 10 ).
  • the balances at the mixing point (MP1) constitute 2 equations and no unknowns.
  • the balances at the mixing point (MP2), combining permeates of stages Rl, R2 and R3 constitute 2 equations and 2 unknowns (Qp, Cp).
  • the balances at the mixing point (MP3) combining NF permeates constitute 2 equations and no unknowns. This totals 16 equations that involve 28 unknowns. This implies 12 degrees of freedom in solving the equations for this five-stage embodiment of the invention process.
  • Dp ⁇ 2 Dp N ⁇ , equal OPDs in RO stage R2 and NF stage Nl
  • Dp N ⁇ Dp N2 , equal OPDs in NF stage N 1 and NF stage N2 YNI, recovery in NF stage N 1
  • C 3 Cp, salt concentration in the permeate from RO stage R2
  • C 5 Cp, salt concentration in the permeate from RO stage R3
  • Q2 Q3 + Q4 equation (2)
  • Q4 Q5 + Q6 equation (3)
  • Q6 Q7 + QD equation (4)
  • Qs Q9 + Q10 equation (5)
  • Q2 Qi + Q10 equation (6)
  • Qs Qs + Q 7 equation (7)
  • Qp Qo + Q3 + Q9 equation (8)
  • QFCF QOCO + Q1C1 equation (9)
  • Q 2 CF Q3C3 + Q4C4 equation (10)
  • Q4CF Q5C5 + QeCe equation (11)
  • Q 6 CF Q7C7 + QDCD equation (12)
  • QSCF Q 9 C 9 + Q1 0 C1 0 equation (13)
  • Q2CF Q1C1 + Q10C10 equation (14)
  • QSCF Q5C5 + QTC 7 equation (15)
  • QPCF QOFO + Q3C3 + Q9C9 equation (16)
  • Y Qp / QF equation (17)
  • YRI QO / QF equation (18)
  • YR2 Q3 / Q2 equation (19)
  • YNI Q5 / Q4 equation (20)
  • YN2 Q7 / Q6 equation (21)
  • YR3 Q9 / Qe equation (22)
  • YRI (Ci - C F ) / (Ci - Co) equation (24)
  • YR 2 (C 4 - C 2 ) / (C 4 - C 3 ) equation (25)
  • Y R3 (Cio - C 8 ) / (CIO - C 9 ) equation (26)
  • YNI (C 6 - C 4 ) / (C 6 - Cs) equation (27)
  • Y N2 (C D - C 6 ) / (C D - C 7 ) equation (28)
  • Apki K(Ci - Co) equation (29)
  • DpN2 K(CD - C 7 ) equation (32)
  • Dp ⁇ 3 K(Cio - C9) equation (33)
  • K 0.801 L-bar/g is an empirical constant.
  • Qo QFYRI equation (35)
  • Qi QF - Qo equation (36)
  • Q2 Qi + Q10 equation (37)
  • Q 4 Q 6 / (1 - Y N1 ) equation (38)
  • Ci Dp b i / K + Co equation (47)
  • C 2 (C F - YCp) / (1 - Y) equation (48)
  • C 3 C P equation (49)
  • C 4 ((YNI + Y N2 )C 3 + C D ) / (1+ YNI + Y N2 ) equation (50)
  • C 5 C 6 + C 7 - C D equation (51)
  • C 6 CD - YN 2 (CD - C 7 ) equation (52)
  • SEC (QFA:TI;RI + z ) i(Dti3 ⁇ 42-Dpri) + z ) io(Dp3 ⁇ 42-D7 ⁇ 3 ⁇ 43) + z ) 4 DpN ⁇ + Q AKS2) / r
  • SEC net the net specific energy consumption (SEC net ), which is the energy required per unit of water produced allowing for the recovery of the pressure energy in the retentate via an energy -recovery device (ERD), is given by the following:
  • One benefit of the REPRO invention is that overall water recoveries greater than 55% can be achieved while operating each stage with a stage recovery less than or equal to 50% and maintaining the safety factor in each stage at a value less than or equal to 1.
  • the present invention allows the maximum OPD (OPD max ) to be varied over a wide range in order to achieve a specif ed overall water recovery and specified salt concentration of the product water.
  • the maximum OPD max is determined by the salt concentration difference between the retentate of the downstream RO subunit (2A) that is introduced to the NF subunit (3A) and the permeate of the downstream RO subunit (2A).
  • the OPD max is determined by the salt concentration difference between streams 4 and 3, hence the OPD max is equal to Dp 2 .
  • the OPD max is the same as the OPD of the SSRO stage; and in a two-stage TSRO system, the OPD max is equal to the OPD of the second RO stage.
  • the specific energy consumption and OPD required to obtain overall water recoveries of 65% and 75% are evaluated for the 4-Stage and 5-Stage embodiments of the REPRO inventions.
  • the input parameters are OPD in RO stage“Rl” (Dpki) and fractional water recovery in NF stage“Nl” (YNI).
  • the NF stages Nl and N2 have the same OPD as stage Rl.
  • the OPD in the upstream RO stage“R3” (Dpk 3 ) is set to have the same OPD as stage Rl in both embodiments, hence the retentate of stage R3 can be combined with the retentate of stage Rl in order to be pressurized using a single pump to be introduced to the high-pressure side of stage R2 (R2H).
  • the NF stage “N3” is set to have fractional water recovery (YN2) equal to YNI in stage“Nl” in the 5-stage embodiment.
  • YN2 fractional water recovery
  • the value of YNI is varied between the minimum and maximum given in Table 1 for each case to show the flexibility of the embodiment in setting the OPD in the downstream RO stage“R2” (Dpk 2 ) for a target overall water recovery.
  • the values of Dpio are also provided in Table 1 for each of the cases.
  • the table includes also the required salt rejections of the NF membranes corresponding to minimum and maximum stage recoveries.
  • Figure 4 shows the tradeoff between the net SEC and Dpk 2 required to produce a potable water product containing no more than 350 ppm of salt from a saltwater feed with 35000 ppm salt concentration, as a function of Y NI .
  • the specific energy consumption and OPD required in SSRO are 79.3 bar and 2.922 kWh/m 3 , respectively, for 65% overall water recovery, and are 111 bar and 3.915 kWh/m 3 , respectively, for 75% overall water recovery.
  • the specific energy consumption required in TSRO is 2.256 kWh/m 3 for 65% overall water recovery, and is 2.705 kWh/m 3 for 75% overall water recovery, while the OPD requirements are the same as in SSRO.
  • the TSRO comprises two RO stages in series wherein the retentate of the first stage is introduced into the high-pressure side of a second RO stage wherein the OPD in the second stage (Dpi ⁇ ) is higher than the OPD in the first stage (Dpio).
  • the OPD requirements (Dpk 2) in 4-Stage and 5-Stage REPRO embodiments are ⁇ 60.5 and ⁇ 55.1 bar, respectively, for 65% overall water recovery; and ⁇ 87.2 and ⁇ 79.3 bar, respectively, for 75% overall water recovery, with comparable net SEC values.
  • Table 2 summarizes the OPD, net SEC and stage recoveries for selected overall water recoveries for the two embodiments in comparison to SSRO.
  • the comparisons show that the embodiments of the REPRO of the present invention allow production of potable water with substantially lower OPD values relative to SSRO.
  • Table 2 Comparison of the OPD, net SEC and stage rejections for desalination using SSRO and the 4-Stage and 5-Stage embodiments of the REPRO invention for producing a water product with a salt concentration equal to 350 ppm for a range of saltwater feed concentrations.
  • the OPD in the upstream RO stage“R3” (Dpk 3) is set to have a different OPD than the OPD in stage Rl in both embodiments in order to further reduce the net SEC requirement.
  • the fractional water recovery of stages Nl (YNI) and the OPDs of the RO stage Rl (Dpia) an d upstream RO stage R2 (Dpk 2) are input parameters in solving the model equations as given in Table 3.
  • the NF stages Nl and N2 have the same OPD as stage Rl.
  • the NF stage“N3” is set to have fractional water recovery (YN2) equal to YNI in stage“Nl” in the 5-stage embodiment.
  • the operating practice for RO that is to maintain the safety factor at a value greater than or equal to one in order to minimize membrane scaling, is taken into account.
  • the feed to the upstream RO subunit (4A) is the permeate of the NF subunit (3A) that is relatively free from scale forming ions, it will be possible to operate the upstream RO subunit (4 A) at a safety factor less than one, which corresponds to a fractional stage recovery greater than 0.50.
  • fraction of a retentate stream from any NF stage which needs to be choses optimally, can be recycled to the high-pressure side of that stage in order to maintain the salt concentration in the feed stream to the NF stage at the optimum value if commercial membranes with higher salt rejection are used in that NF stage.

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

Abstract

L'objet de l'invention est de fournir un système et un processus qui permettent la récupération de produit à partir de solutions aqueuses contenant des sels ou des solutés de faible poids moléculaire tels que l'éthanol à un taux de récupération élevé, une faible différence de pression osmotique (OPD) et une faible consommation d'énergie par rapport aux procédés actuels. Des applications particulières de l'invention comprennent la production d'eau potable à partir de sources d'eau à haute teneur en sel telles que l'eau de mer, l'eau saumâtre ou les eaux usées. Le système et le processus associés à la présente invention d'osmose inverse à pression réduite (REPRO) décrit ici atteint la réduction de la SEC, une réduction de l'OPD, et une augmentation de la récupération d'eau potable par l'intermédiaire d'une nouvelle technologie de traitement RO-NF hybride à plusieurs étages.
PCT/TR2018/050063 2018-02-21 2018-02-21 Système d'osmose inverse multi-étage et processus de récupération d'eau élevée à partir de solutions aqueuses WO2019164462A1 (fr)

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PCT/TR2018/050063 WO2019164462A1 (fr) 2018-02-21 2018-02-21 Système d'osmose inverse multi-étage et processus de récupération d'eau élevée à partir de solutions aqueuses
SG11201900705PA SG11201900705PA (en) 2018-02-21 2018-02-21 Multi-stage reverse osmosis system and process for high water recovery from aqueous solutions

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11502323B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
US11502322B1 (en) 2022-05-09 2022-11-15 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

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2186963A1 (fr) * 1996-10-01 1998-04-01 Riad A. Al-Samadi Procede de purification par osmose inverse a rendement eleve
US20130313195A1 (en) * 2012-05-04 2013-11-28 University Of Florida Research Foundation, Inc. Membrane System to Treat Leachate and Methods of Treating Leachate
US20160176728A1 (en) * 2014-12-17 2016-06-23 Stone & Resource Industry R & D Center Method for producing mineral water rich in calcium ions and magnesium ions
WO2016124902A1 (fr) * 2015-02-02 2016-08-11 Surrey Aquatechnology Limited Concentration de saumure

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA2186963A1 (fr) * 1996-10-01 1998-04-01 Riad A. Al-Samadi Procede de purification par osmose inverse a rendement eleve
US20130313195A1 (en) * 2012-05-04 2013-11-28 University Of Florida Research Foundation, Inc. Membrane System to Treat Leachate and Methods of Treating Leachate
US20160176728A1 (en) * 2014-12-17 2016-06-23 Stone & Resource Industry R & D Center Method for producing mineral water rich in calcium ions and magnesium ions
WO2016124902A1 (fr) * 2015-02-02 2016-08-11 Surrey Aquatechnology Limited Concentration de saumure

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11502323B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell and methods of use thereof
US11502322B1 (en) 2022-05-09 2022-11-15 Rahul S Nana Reverse electrodialysis cell with heat pump
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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